- Open Access
Cultivation strategies for production of (R)-3-hydroxybutyric acid from simultaneous consumption of glucose, xylose and arabinose by Escherichia coli
© Jarmander et al.; licensee BioMed Central. 2015
- Received: 11 December 2014
- Accepted: 30 March 2015
- Published: 11 April 2015
Lignocellulosic waste is a desirable biomass for use in second generation biorefineries. Up to 40% of its sugar content consist of pentoses, which organisms either take up sequentially after glucose depletion, or not at all. A previously described Escherichia coli strain, PPA652ara, capable of simultaneous consumption of glucose, xylose and arabinose was in the present work utilized for production of (R)-3-hydroxybutyric acid (3HB) from a mixture of glucose, xylose and arabinose.
The Halomonas boliviensis genes for 3HB production were for the first time cloned into E. coli PPA652ara, leading to product secretion directly into the medium. Process design was based on comparisons of batch, fed-batch and continuous cultivation, where both excess and limitation of the carbon mixture was studied. Carbon limitation resulted in low specific productivity of 3HB (<2 mg g−1 h−1) compared to carbon excess (25 mg g−1 h−1), but the yield of 3HB/cell dry weight (Y3HB/CDW) was very low (0.06 g g−1) during excess. Nitrogen-exhausted conditions could be used to sustain a high specific productivity (31 mg g−1 h−1) and to increase the yield of 3HB/cell dry weight to 1.38 g g−1. Nitrogen-limited fed-batch process design led to further increased specific productivity (38 mg g−1 h−1) but also to additional cell growth (Y3HB/CDW = 0.16 g g−1). Strain PPA652ara did under all processing conditions simultaneously consume glucose, xylose and arabinose, which was not the case for a reference wild type E. coli, which also gave a higher carbon flux to acetic acid.
It was demonstrated that by using E. coli PPA652ara, it was possible to design a production process for 3HB from a mixture of glucose, xylose and arabinose where all sugars were consumed. An industrial 3HB production process is proposed to be divided into a growth and a production phase, and nitrogen depletion/limitation is a potential strategy to maximize the yield of 3HB/CDW in the latter. The specific productivity of 3HB reported here from glucose, xylose and arabinose by E. coli is further comparable to the current state of the art for production from glucose sources.
- Escherichia coli
- 3-Hydroxybutyric acid
- Simultaneous uptake
- Production process
- Nitrogen limitation
Lignocellulosic waste is an abundantly available, low cost and generally unutilized biomass source that can contain up to 70–80% (w/w) carbohydrates . This makes it desirable as a substrate for the various chemicals proposed for production in second generation biorefineries. The relative sugar composition of for example wheat straw after dilute acid pretreatment and enzymatic saccharification is 55.6% (D-)glucose, 37.6% (D-)xylose and 4.1% (L-)arabinose (w/w) . Approximately 40% of the total sugar content is thus composed of pentoses, which current production organisms cannot consume efficiently. For example, wild type Saccharomyces cerevisiae can neither metabolize xylose nor arabinose . Without efficient conversion of the pentoses into biomass and product, the carbon source is in effect only utilized to ~ 60% of its potential. There have been efforts to develop S. cerevisiae strains able to co-ferment glucose and xylose, but the uptake has been either slow or sequential, which leads to residual sugar in the medium [4,5]. In Escherichia coli, on the other hand, it was previously reported  that the ability to absorb pentoses is strain dependent and subjected to a complex sequential uptake chain that is initiated only at low glucose levels in the cultivation medium. In E. coli, the three most abundant sugars of pretreated wheat straw are thus taken up in the order of glucose > arabinose > xylose. This is due to a combination of carbon catabolite repression , inducer exclusion and pentose uptake regulation .
In a previous study, an E. coli strain (named PPA652ara) capable of simultaneous metabolism of glucose, xylose and arabinose under aerobic conditions without leaving any residual sugar in the cultivation medium was designed . This was achieved by deletion of the ptsG gene (EIICBGlc), the preferred inner membrane transporter for glucose. This deletion leads to inactivation of the regulatory mechanism of inducer exclusion, but also to increased production of cAMP, the activator of most sugar metabolism operons. Binding of cAMP to these operons should thus lead to continuous promoter transcription and expression of the respective permeases, thereby abolishing also the catabolite repression control. Pentose uptake in E. coli is regulated by arabinose repression of xylose uptake, and by using a technique of precultivation on arabinose, this regulatory layer could also be removed in PPA652ara.
The strain PPA652ara was intended to be a platform for efficient aerobic production processes of chemicals from lignocellulosic waste. The current work therefore investigates the effect of recombinant product formation on the utilization of mixed sugars by this strain. As such, PPA652ara was used to produce the hydroxyalkanoic acid (R)-3-hydroxybutyric acid (abbreviated 3HB from now on). 3HB is the monomeric unit of poly-(R)-3-hydroxybutyric acid (PHB), a biodegradable polyester that is naturally produced by several microorganisms, however not by E. coli . PHB metabolism is initiated from a condensation of two acetyl-CoA molecules to form acetoacetyl-CoA, catalyzed by the enzyme acetoacetyl-CoA thiolase . Acetoacetyl-CoA is then stereoselectively reduced to (R) or (S)-3HB-CoA by a NAD(P)H dependent acetoacetyl-CoA reductase. PHB synthase lastly catalyzes the polymerization of the monomer to PHB.
The 3HB monomer is an interesting molecule since it contains a chiral center and two active functional groups that can be easily modified: a hydroxyl group and a carboxyl group [11,12]. This allows it to be used as building block in the synthesis of several chiral fine chemicals, pharmaceuticals and copolyesters. 3HB has been produced by both chemical synthesis  and biotechnological processes [12-15]. The biotechnological processes have so far been the most promising due to the advantage of producing an enantiomerically pure product, and the ability to do so without the use of organic solvents. 3HB has been produced in E. coli by expression of genes from wild type PHB producers, predominantly Cupriavidus necator (previously known as Ralstonia eutropha and Alcaligenes eutrophus) by various strategies [16-19]. In these studies, titers of 3HB between 7.3-12.2 g L−1 were achieved from glucose as the carbon source in 24–96 h of cultivation, having volumetric productivities in the range of 0.07-0.50 g L−1 h−1.
In the current work, the aim was to use the platform E. coli PPA652ara to design a production process of 3HB from a mixture of glucose, xylose and arabinose, a typical composition in waste biomass, in which all monosaccharides are consumed. The genes for 3HB production were cloned from the halophilic, naturally PHB-producing bacterium Halomonas boliviensis, which has been shown to be a promising producer of this chemical . To our knowledge, this is the first time that genes from H. boliviensis have been used for recombinant production of 3HB in E. coli. After 3HB production had been verified, the best strategy to enhance 3HB productivity was sought. This was based on different cultivation concepts using nutrient excess in combination with exhaust or limitation strategies.
Validation of 3HB metabolism in E. coli from mixed sugars
3HB production by assorted E. coli strain and plasmid combinations on varied sugar carbon sources
E. coli strain
Final OD 600
(h −1 )
(g L −1 )
(g L −1 OD 600 −1 )
Glc + Xyl + Ara
For the multiple sugar based process design, pJBGT3RX was chosen, and used in the platform strain. This construct was initially cultivated on glucose, xylose and arabinose individually, but also as a mixture (Table 1). When cultivated on xylose or arabinose, the amount of 3HB from PPA652ara (xylose: 0.18 g L−1, arabinose: 0.17 g L−1) was not significantly different from that of the wild type AF1000 cultivated on glucose, confirming that 3HB can be produced from these pentoses with similar efficiency. However, when glucose was used as the single carbon source for PPA652ara, the concentration of secreted 3HB was practically zero. This could possibly be an effect related to the lower specific uptake rate of glucose of PPA652ara, which lacks the primary glucose inner membrane transporter, ptsG, and thus has approximately twice the doubling time of AF1000 (118 min vs. 56 min) on glucose. Nevertheless, the substrate that ultimately will be used is a carbohydrate mixture, and when PPA652ara was cultivated on glucose, xylose and arabinose, it produced 3HB to levels (0.17 g L−1) that were comparable to AF1000 cultivated on glucose.
Carbon-limited process design
Byproduct formation for these two strains was however considerably different, and the acetic acid concentrations for AF1000 were over 200% of the values for PPA652ara (peaking at 1.79 g L−1 vs. 0.78 g L−1 at dilution rate 0.5 h−1). This is not desirable and will be a drawback for the use of the parental strain. As catabolite repression was found to require relatively high glucose fluxes, the conclusion from carbon-limited growth is that both strains can effectively run at the same maximum feed rate for simultaneous sugar uptake and the reduced acetic acid accumulation appears to be the only explicit benefit in using PPA652ara over a wild type E. coli in sugar-limited processes.
Process design with excess of carbon
In correlation with the results of Figure 3, PPA652ara produces significantly less of the by-product acetic acid than AF1000, although a high overflow metabolism at sugar excess is expected for both strains. For the platform strain, the acetic acid is also completely reabsorbed. AF1000 did have a higher q3HB than PPA652ara (on average 68 mg g−1 h−1 vs. 25 mg g−1 h−1), which was reflected in the higher final titer of 3HB at 0.51 g L−1, compared to 0.31 g L−1 for PPA652ara. Also, the specific uptake rate of sugar (qS) was higher for AF1000 solely on glucose than the qS total (the combined specific uptake rate of glucose, xylose and arabinose) for PPA652ara (on average 1.00 g g−1 h−1 vs. 0.70 g g−1 h−1). From this experiment, it is clear that a non-limited sugar flux is necessary for high specific productivity of 3HB, as both AF1000 and PPA652ara display q3HB values that are several magnitudes greater than in sugar-limited continuous mode.
Process design with excess of carbon and nitrogen exhaustion
During nitrogen depletion, production of 3HB continued for both strains at a steady rate, with titers of 0.64 g L−1 for AF1000, and 0.54 g L−1 for PPA652ara in the nitrogen depletion phase. For PPA652ara, this is a distinct improvement in productivity compared to the results of the batch cultivation with excess of carbon and nitrogen (Figure 4). The mean values of q3HB decayed over time for both strains in the nitrogen depletion phase, which is to be expected, as nitrogen is not refilled in the process. The two strains showed very similar mean values of q3HB at 29 mg g−1 h−1 for AF1000 and 31 mg g−1 h−1 for PPA652ara. For PPA652ara, this is an improvement of 25% over the previously mentioned batch cultivation, but for AF1000, it is instead a considerable decrease of approximately 60%. As expected, the values of qS total were much lower in this experiment (on average approximately 0.2 g g−1 h−1 for AF1000, and 0.3 g g−1 h−1 for PPA652ara). It is also noteworthy that acetic acid continues to be produced in the nitrogen depletion phase, with PPA652ara producing the most (0.48 g L−1 for AF1000 vs. 0.54 g L−1 for PPA652ara).
Nitrogen limited fed-batch cultivation
The experiment performed in Figure 5 allowed us to deduce that it is possible to maintain a high specific productivity of 3HB from a mixture of glucose, xylose and arabinose without increasing the cell mass substantially by depleting nitrogen. In order to avoid a decaying production rate of 3HB, it is likely that nitrogen needs to be replenished. It is however probably not desirable to use a high feeding rate, as this allows for more of the carbon to be directed towards cell mass, rather than 3HB.
For both strains, an average growth rate of 0.24 h−1 was achieved in the nitrogen limited fed-batch phase, which was slightly higher than expected. The average qS total values were in turn also approximately the same, at 0.6 g g−1 h−1. Even the 3HB titers attained were very similar for the two strains, at 1.84 and 1.87 g L−1 respectively for AF1000 and PPA652ara. The acetic acid concentration was however much higher for AF1000 at 2.66 g L−1, to compare with 0.77 g L−1 for PPA652ara. The specific productivity of 3HB in the fed-batch phase was further higher for both strains than during nitrogen depletion (Figure 5), with average values of 45 mg g−1 h−1 (55% increase) and 38 mg g−1 h−1 (22% increase) achieved for AF1000 and PPA652ara respectively. Even though the specific productivities of 3HB increased during nitrogen-limited fed-batch, feeding nitrogen into the bioreactor did not significantly reduce their time-dependent decay. These results instead resemble what has been seen in the past for induced expression systems building on substrate induced promoters , which after a short time show clear saturation kinetics. The use of a constitutive promoter could possibly result in a more stable specific productivity of 3HB.
Comparison of process modes
Comparison of production of 3HB by E. coli AF1000 and PPA652ara by varied cultivation techniques
mean q S total
mean q 3HB
(g L −1 )
(g L −1 )
(g L −1 )
(g L −1 )
(g g −1 h −1 )
(mg g −1 h −1 )
(g g −1 )
(g g −1 )
(g g −1 )
Glc + Xyl + Ara
Glc + Xyl + Ara
Glc + Xyl + Ara
Glc + Xyl + Ara
Glc + Xyl + Ara
The fluctuating level of CoA in the cell during different cultivation conditions is one plausible explanation for the big variance seen in the Y3HB/CDW. This would be due to inhibition of acetoacetyl-CoA thiolase by high levels of CoA , which is likely during exponential growth in batch experiments. In batch mode, the majority of the carbon would thus be directed towards biomass by the competing enzyme citrate synthase in the TCA cycle. When nitrogen is depleted, the concentration of CoA is however expected to be low, and the activity of acetoacetyl-CoA thiolase should therefore increase. In addition, the intracellular concentration of NADH and/or ATP is expected to go up during nitrogen starvation, which in turn leads to inhibition of citrate synthase. The end result is increased 3HB secretion during nitrogen depletion, which is what was seen in the experiments. Since the nitrogen-limited fed-batch cultivations resulted in significantly reduced Y3HB/CDW compared to nitrogen-depletion, this gives that citrate synthase likely was much more active during the fed-batch conditions. If nitrogen needs to be restocked during the 3HB production phase, it should therefore likely be fed at a rate lower than 0.2 h−1 in order to avoid unwanted biomass formation.
To our knowledge, the highest volumetric productivity of 3HB that has been reported for recombinant E. coli is 12.2 g L−1 achieved in 24 h from glucose, which is equal to 0.50 g L−1 h−1 . To achieve the same result with PPA652ara under nitrogen depletion, the cell growth phase should be extended to approximately 16 g L−1 CDW. This is quite possible by use of standard E. coli cultivation protocols and the realistic limit of the biomass is probably much higher . PPA652ara thus seems a promising candidate strain for production of chemicals from sugar mixtures of comparable productivity as the current state of the art E. coli from glucose.
In this work, the E. coli platform strain PPA652ara was used to successfully produce 3HB from a mixture of glucose, xylose and arabinose, in which all sugars were being consumed. In addition, simultaneous consumption of the sugars by PPA652ara resulted in less acetic acid being produced than by the wild type strain AF1000, from a sequential sugar uptake. In order to obtain a high specific productivity of 3HB in combination with a high yield of 3HB/CDW, carbon needed to be available in excess and another essential nutrient, such as nitrogen, limited. The specific productivity of 3HB reported here by strain PPA652ara from a mixture of glucose, xylose and arabinose, is further comparable to the values achieved by E. coli from glucose in the current state of the art.
Bacterial strains and plasmids
The E. coli strains used in this work were AF1000 (MC4100, relA1 + )  and PPA652ara (MC4100, relA1 + , ΔptsG::Km, adapted to growth on L-arabinose) . The 3HB production plasmids pJBGT3RX and pJBGRXT3 were constructed from pKM1D, a pACYC184-derived low copy number plasmid with ori p15A, a lacUV5 promoter, a multiple cloning site, the lacIq repressor and a chloramphenicol resistance gene. From H. boliviensis, the two genes needed to produce 3HB, t3 (acetoacetyl-CoA thiolase) and rx (acetoacetyl-CoA reductase) were amplified by PCR with complimentary tails for cloning between the HindIII and SacI sites on pKM1D. The plasmid was digested by HindIII and SacI, and the two genes were cloned by the SLIC method  in two alternate gene orders, either thiolase-reductase (in pJBGT3RX) or reductase-thiolase (in pJBGRXT3).
Batch cultivation in shake flask
E. coli cells harboring pJBGT3RX or pJBGRXT3 were taken from a glycerol stock stored at −80°C and used to inoculate sterile baffled 1000 mL shake flasks containing 100 mL cultivation medium. The cells were cultivated at 37°C and 180 rpm shaking until the stationary phase was reached, at which time the production of 3HB was evaluated. Production of 3HB was induced by the addition of 200 μM IPTG at an optical density at 600 nm (OD600) of 0.2.
Continuous cultivation in bioreactor
E. coli cells harboring pJBGT3RX were taken from a glycerol stock stored at −80°C and used to inoculate sterile baffled 1000 mL shake flasks containing 100 mL cultivation medium. The cells were cultivated overnight at 37°C and 180 rpm and were used to inoculate a sterile 3 L stirred tank bioreactor (STR) containing 2 L cultivation medium. A cultivation temperature of 37°C was used in the reactor and dissolved oxygen (DO) was maintained at above 30%. Antifoam was added when required. Once the cells had consumed the sugar in the medium, the inlet feed was started and continuous mode was sustained through a weight-based efflux of cell culture. At least 4 residence times were allowed to pass before the reactor was sampled after any conditions were changed. Each dilution rate was analyzed in duplicate. For production of 3HB, IPTG was present in the cultivation medium from the start at a concentration of 200 μM.
Batch and fed-batch cultivation in bioreactor
E. coli cells harboring pJBGT3RX were taken from a glycerol stock stored at −80°C and used to inoculate a sterile 10 L STR containing 6 or 7 L cultivation medium. The cells were cultivated at 37°C and DO was maintained at above 30%. Antifoam was added when required. Production of 3HB was induced by the addition of 200 μM IPTG at an OD600 of 0.2. For fed-batch cultivations, feeding was initiated once ammonia was depleted. Samples for OD600, cell dry weight, glucose, xylose, arabinose, ammonia, 3HB and acetic acid were taken regularly during the bioreactor cultivations.
The cultivation medium used was a minimal salt medium consisting of (for non-nitrogen limited cultures, per liter): 5.00 g (NH4)2SO4, 1.60 g KH2PO4, 6.60 g Na2HPO4●2 H2O, 0.50 g (NH4)2-H-Citrate. For nitrogen limited cultures, the following composition was used (per liter): 1.00 g (NH4)2SO4, 1.60 g KH2PO4, 6.60 g Na2HPO4●2 H2O, 0.65 g Na3-(Citrate)3. The minimal medium was after sterilization supplemented with 1 mL L−1 trace element stock solution and 1 mL L−1 1 M MgSO4, both sterile filtered (0.2 μm, VWR collection). The trace element stock solution contained the following components (per liter): 0.50 g CaCl2●2 H2O, 16.70 g FeCl3●6 H2O, 0.18 g ZnSO4●7 H2O, 0.16 g CuSO4●5 H2O, 0.15 g MnSO4●4 H2O, 0.18 g CoCl2●6 H2O, 20.10 g Na-EDTA. Sugar stock solutions were sterilized separately and added to the minimal medium after autoclaving. Sugar was added to the shake flask cultivations in excess, with an initial concentration of 5.00 g L−1 of D-glucose, D-xylose or L-arabinose, or a combination of all three in equal concentrations (1.66 g L−1). In the bioreactor cultivations, the sugar concentrations in the medium were 8.20 g L−1 D-glucose, 5.95 g L−1 D-xylose and 0.85 g L−1 L-arabinose (corresponds to the relative ratios of a lignocellulose hydrolyzate). In the continuous cultivations, the feed consisted of the finalized cultivation medium. In the fed-batch cultivations, the feed solution consisted of 100.00 g L−1 (NH4)2SO4, 206.78 g L−1 D-glucose, 150.04 g L−1 D-xylose and 21.43 g L−1 L-arabinose (same sugar ratio as in the starting medium). In all bioreactor cultivations, pH was kept constant at 7.0. In the continuous cultivations, as well as the non-nitrogen-limited batch cultivations, pH was titrated with NH3. In the nitrogen-limited cultivations, pH was titrated with NaOH.
Cell growth analysis
OD600 was measured to monitor cell growth in all cultivations. Samples were withdrawn and diluted in saline solution (0.9% NaCl w/v) to an estimated OD600 of 0.1-0.2 and the OD600 was then measured in a spectrophotometer (Genesys 20, Thermo scientific). Cell growth was also monitored through measurement of the cell dry weight (CDW). Samples of 5 mL cell culture were withdrawn in triplicates into preweighed, dry glass tubes, which were centrifuged at 2000 g in a tabletop centrifuge (CompactStar CS4, VWR) for 5 min. The pellets were washed with 5 mL saline solution and re-centrifuged at 2000 g for 5 min. The supernatant was removed and the cell pellets were dried over night at 105°C. The following day, the dry pellets were allowed to cool to ambient temperature in a desiccator, after which they were weighed.
Sugar and ammonia analysis, and calculation of rates
For continuous cultivations, a sample of 2 mL cell culture was withdrawn into a preweighed syringe containing 2 mL cold (~4°C) perchloric acid at a concentration of 0.13 M to stop metabolism . The sample was thereafter transferred to a tube and was centrifuged at 2000 g for 10 min. 3.5 mL of the supernatant was neutralized with 75 μL saturated (~500 g L−1) potassium carbonate. The sample was then allowed to precipitate for 15 min on ice, after which it was centrifuged at 2000 g for 5 min. The supernatant was filtered (0.45 μm, VWR collection) and frozen at −20°C until analysis. For batch and fed-batch cultivations, a sample of 2 mL cell culture was automatically and rapidly withdrawn (<0.1 s) into a preweighed tube containing 2 mL of the same cold perchloric acid as mentioned above. Subsequent centrifugation, neutralization, centrifugation, filtration and storage steps were identical to those performed for the continuous cultivations. The sugar concentrations were determined by the use of commercially available enzymatic kits (Boehringer Mannheim Cat No. 716251, Megazyme D-Xylose Assay Kit Cat No. K-XYLOSE, Megazyme Lactose/Galactose (Rapid) Cat No. K-LACGAR). Ammonia concentrations were determined with the enzymatic kit Megazyme Ammonia Assay Kit (Rapid) Cat No. K-AMIAR. The qS values were calculated as the mean over two consecutive data points, and the parameter qS total accounted for the change in concentration of all three sugars.
3HB and acetic acid analysis, and calculation of rates
The supernatants from the CDW samples were filtered (0.45 μm, VWR collection), stored at −20°C and used for 3HB and acetic acid analysis. The acetic acid concentration in the samples was determined with the enzymatic kit Boehringer Mannheim Cat No. 10148261035. The 3HB concentration in samples was determined with the enzymatic kit Megazyme D-3-Hydroxybutyric Acid Assay Kit Cat No. K-HDBA. This kit is specific to (R)-3-hydroxybutyric acid. The q3HB values were calculated as the mean over three consecutive data points.
Gas chromatographic analysis of 3HB enantiomers
Filtered supernatants were acidified with sulfuric acid and extracted with chloroform. The extracted acids were esterified with 2-propanol and separated on a CP-ChiraSil-DEX CB column with a 40 min temperature gradient, ranging from 45 to 200°C, and detected with a FID detector.
The Swedish International Development Agency (SIDA) and The Swedish Research Council Formas are acknowledged for their financial support.
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