- Open Access
Engineering of Escherichia coli for Krebs cycle-dependent production of malic acid
- Debora Trichez†1View ORCID ID profile,
- Clément Auriol†2, 3,
- Audrey Baylac2,
- Romain Irague1,
- Clémentine Dressaire1,
- Marc Carnicer-Heras1,
- Stéphanie Heux1,
- Jean Marie François1, 2Email author and
- Thomas Walther1, 2, 4
© The Author(s) 2018
- Received: 9 May 2018
- Accepted: 6 July 2018
- Published: 16 July 2018
Malate is a C4-dicarboxylic acid widely used as an acidulant in the food and beverage industry. Rational engineering has been performed in the past for the development of microbial strains capable of efficient production of this metabolite. However, as malate can be a precursor for specialty chemicals, such as 2,4-dihydroxybutyric acid, that require additional cofactors NADP(H) and ATP, we set out to reengineer Escherichia coli for Krebs cycle-dependent production of malic acid that can satisfy these requirements.
We found that significant malate production required at least simultaneous deletion of all malic enzymes and dehydrogenases, and concomitant expression of a malate-insensitive PEP carboxylase. Metabolic flux analysis using 13C-labeled glucose indicated that malate-producing strains had a very high flux over the glyoxylate shunt with almost no flux passing through the isocitrate dehydrogenase reaction. The highest malate yield of 0.82 mol/mol was obtained with E. coli Δmdh Δmqo ΔmaeAB ΔiclR ΔarcA which expressed malate-insensitive PEP carboxylase PpcK620S and NADH-insensitive citrate synthase GltAR164L. We also showed that inactivation of the dicarboxylic acid transporter DcuA strongly reduced malate production arguing for a pivotal role of this permease in malate export.
Since more NAD(P)H and ATP cofactors are generated in the Krebs cycle-dependent malate production when compared to pathways which depend on the function of anaplerotic PEP carboxylase or PEP carboxykinase enzymes, the engineered strain developed in this study can serve as a platform to increase biosynthesis of malate-derived metabolites such as 2,4-dihydroxybutyric acid.
- Malic acid
- Escherichia coli
- Flux analysis
- Metabolic engineering
The four-carbon dicarboxylic acid malate is a Krebs cycle intermediate and a compound of considerable economic interest. It is mainly used as an acidulant in the food and beverage industry, or as a precursor for specialty chemicals [1, 2].
Currently, d/l-malic acid is chemically produced by hydration of maleic anhydride and has an estimated annual market volume of ~ 10 kt/year. However, due to its potential to replace maleic acid as a major building block in the chemical industry, its annual production could rise to ~ 200 kt if a cost-efficient biochemical production process could be developed . Therefore, malic acid has been ranked as one of the 12 top target molecules of biochemical production processes , and much research effort has been invested in recent years to optimize the metabolic network and cultivation conditions of malate-producing organisms.
The filamentous fungus Aspergillus flavus was the first identified natural malate-producing organism . After optimization of cultivation conditions, it accumulated 113 g/l malate with a yield and productivity of 1.26 mol/mol and 0.59 g/(lh), respectively . However, since A. flavus produces toxic aflatoxin, this organism was never employed in industrial production processes. During the search for alternative natural malate-producing organisms, the yeast Zygosaccharomyces rouxii and the filamentous fungi Aspergillus oryzae and Penicillium sclerotiorum were shown to accumulate malate to high levels, reaching 92 g/l at a yield of 1.2 mol/mol for the latter organism [6–8].
In complementary studies carried out in yeast, bacteria, and fungi, it was tried to further increase malate production by rational optimization of the metabolic network. The oxaloacetate (OAA)-yielding carboxylation of either phosphoenolpyruvate (PEP) or pyruvate, followed by direct reduction of OAA to produce malate represents the most efficient metabolic pathway, which has a theoretical yield of 2 mol malate per mol glucose . Therefore, all metabolic engineering endeavors to increase malate production focused on the optimization of this pathway. The overexpression of pyruvate carboxylase, malate dehydrogenase, and malate permease activities in a pyruvate-overproducing Saccharomyces cerevisiae platform strain enabled the accumulation of 59 g/l malate at a yield of 0.42 mol/mol [9–11]. Using a similar strategy, malate production by an A. oryzae strain could be increased to 154 g/l and a yield of 1.38 mol/mol after overexpressing pyruvate carboxylase, and a malate permease . While the optimal function of the processes employing yeast and fungi required aerobic cultivation conditions, anaerobic malate production was demonstrated with Escherichia coli. A strain devoid of all alternative fermentative pathways and evolved for the production of succinate [12, 13] was converted into a malate producer by additionally deleting the genes coding for malic enzyme, fumarate reductase and fumarase activities. The strain accumulated 34 g/l malate with a yield and productivity of 1.42 mol/mol and 0.47 g/(l h), respectively . Malate and succinate production in the evolved strain relied on mutations that conferred increased expression of PEP carboxykinase (Pck) and inactivation of the PTS sugar uptake system [15, 16]. Together, these modifications enabled an ATP-producing carboxylation of PEP and thus increases the energy output of the pathway. The microbial production of malic acid by the use of additional microorganisms and alternative substrates was discussed in detail in two recent reviews [17, 18].
The biosynthesis of malate from glucose via direct reduction of oxaloacetate is redox neutral and produces a maximum of two mole ATP per glucose molecule if PEP is converted into oxaloacetate via the ATP-forming Pck. Thus, in biosyntheses that employ additional reduction steps for the conversion of malate into other target molecules, cofactor supply may become limiting. We recently proposed a synthetic pathway which converts malate into DHB requiring one mol of ATP and two moles of NAD(P)H . These additional cofactors cannot be produced by employing the above-cited conventional pathways for malate biosynthesis. Therefore, we set out to investigate metabolic engineering requirements to enable aerobic malate production via Krebs cycle and glyoxylate shunt, which increases ATP and NADH production at the expense of a decreased maximum malate yield which drops to 1.33 mol/mol .
We show that significant malate production through the Krebs cycle could not be achieved by solely deleting all malate dehydrogenases and malic enzymes, but additionally required the over-expression of a malate-insensitive PEP carboxylase mutant. Malate production was further increased by the inactivation of the acetate pathways, or by the overexpression of a NADH-insensitive citrate synthase mutant. Inactivation of the dicarboxylic acid transporter DcuA strongly reduced malate production arguing for a pivotal role of this permease in malate export. The best strain produced malate from glucose at a yield of 0.82 mol/mol.
Media and cultivation conditions
Strains were grown in Luria–Bertani (LB) broth (containing per liter: 10 g tryptone, 5 g yeast extract, 10 g NaCl, and 50 µg kanamycin sulfate and 25 µg chloramphenicol when necessary)  during strain construction and in starter cultures. All growth and pre-cultures were carried out in defined mineral medium. One liter mineral medium contained 10 g glucose, 18 g Na2HPO4 * 12 H2O, 3 g KH2PO4, 0.5 g NaCl, 2 g NH4Cl, 0.5 g MgSO4 * 7 H2O, 0.015 CaCl2 * 2 H2O, 1 ml of 0.06 mol/l FeCl3 stock solution (prepared in 100 times diluted concentrated HCl), 2 ml of 10 mM thiamine HCl stock solution, 20 g MOPS, 50 µg kanamycin sulfate (and 25 µg chloramphenicol when necessary), and 1 ml of trace element solution (containing per liter: 0.4 g Na2EDTA * 2H2O, 1.8 g CoCl2 * 6 H2O, 1.8 g ZnSO4 * 7 H2O, 0.4 g Na2MoO4 * 2 H2O, 0.1 g H3BO3, 1.2 g MnSO4 * H2O, 1.2 g CuCl2 * H2O). Medium was adjusted to pH 7 and filter-sterilized. Pre-cultures were inoculated at OD of ~ 0.5 from starter cultures that were grown overnight in LB. Growth cultures were inoculated at OD of ~ 0.2 from exponentially growing pre-cultures. When OD of the growth cultures reached 0.6, 1 mM isopropyl β-d-1-thiogalactopyranoside (IPTG) was added. Strains were incubated in 250 ml flasks containing 30 ml medium, and shaken at 200 rpm and 37 °C in a rotary shaker (Infors). Samples were regularly withdrawn to follow growth and metabolite secretion.
Construction of strains and plasmids
Primers and plasmids used in this study
pACT3 expressing wild-type ppc gene from E. coli from weak RBS
pACT3 expressing ppcK620S mutant gene from E. coli from weak RBS
pEXT20 expressing ppcK620S mutant gene from E. coli from strong RBS
pACT3 expressing ppcK620S mutant gene from E. coli from strong RBS
pACT3w-ppcK620S expressing gltAR164L mutant gene from E. coli
Escherichia coli strains used in this study
E. coli K-12 MG1655 F− λ− ilvG- rfb-50 rph-1
F-, Δ(araD-araB)567, ΔlacZ4787(::rrnB-3), λ-, rph-1, Δ(rhaD-rhaB)568, hsdR514 carrying single gene deletions
Δmdh::FRT Δmqo::FRT Δ(ackA-pta)::FRT
Δmdh::FRT Δmqo::FRT Δ(ackA-pta)::FRT ΔmaeB::FRT
Δmdh::FRT Δmqo::FRT Δ(ackA-pta)::FRT ΔmaeA::FRT
Δmdh::FRT Δmqo::FRT Δ(ackA-pta)::FRT ΔmaeA::FRT ΔmaeB::FRT
Sy68 expressing pACT3w-ppcK620S
Sy102 expressing pACT3w-ppcK620S
Sy161 expressing pACT3w-ppcK620S
Sy162 expressing pACT3w-ppcK620S
Sy168 expressing pACT3w-ppcK620S
Sy168 expressing pACT3w-ppcwt
Sy168 expressing pEXT20 s-ppcK620S
Sy168 expressing pEXT20w-ppcK620S
Sy168 expressing pACT3 s-ppcK620S
Δmdh::FRT Δmqo::FRT ΔmaeA::FRT ΔmaeB::FRT
Δmdh::FRT Δmqo::FRT ΔmaeA::FRT ΔmaeB::FRT ΔiclR::FRT
Δmdh::FRT Δmqo::FRT ΔmaeA::FRT ΔmaeB::FRT ΔiclR::FRT ΔackA::FRT
Δmdh::FRT Δmqo::FRT ΔmaeA::FRT ΔmaeB::FRT ΔiclR::FRT ΔackA::FRT ΔpoxB::FRT
Δmdh::FRT Δmqo::FRT ΔmaeA::FRT ΔmaeB::FRT ΔiclR::FRT ΔarcA::FRT
Δmdh::FRT Δmqo::FRT ΔmaeA::FRT ΔmaeB::FRT ΔiclR::FRT ΔarcA::FRT
Δmdh::FRT Δmqo::FRT ΔmaeA::FRT ΔmaeB::FRT ΔiclR::FRT ΔarcA::FRT Δedd-eda::FRT
Δmdh::FRT Δmqo::FRT ΔmaeA::FRT ΔmaeB::FRT ΔiclR::FRT ΔarcA::FRT Δedd-eda::FRT ΔaspA::FRT
The wild-type ppc gene was PCR amplified from genomic DNA the E. coli MG1655 strain using Phusion polymerase (Thermo-Scientific) and the forward and reverse primers ppc_clon_for and ppc_clon_frev respectively. The resulting DNA fragment was ligated into pACT3  using SmaI and XbaI restriction sites to obtain vector pACT3w-ppcwt. The amino acid exchange Lys620Ser was introduced into ppc by site directed PCR mutagenesis using primers ppc_k620s_for and ppc_k620s_rev. The PCR product was DpnI digested and transformed into NEB 5-alpha competent E. coli cells (NEB). The resulting plasmid, pACT3w-ppcK620S was isolated and verified by DNA sequencing to contain the desired mutation. Subcloning into the pEXT20 vector was achieved using SalI and KpnI restriction sites. To replace the original ribosome-binding site (RBS) of pACT3 in front of the ppcK620S gene by a stronger one, ppcK620S was PCR amplified using primers ppc_sRBS_for and ppc_sRBS_for, respectively, and cloned into the pACT3 and pEXT20 vectors using SmaI and XbaI restriction sites. The wild-type gltA gene was PCR-amplified from genomic DNA of the E. coli MG1655 strain using pfu polymerase primers gltA_clon_for and gltA_clon_rev. The resulting DNA fragment was cloned into the pACT3 vector using SacI and HindIII restriction sites. The amino acid exchange R164L was introduced into the gltA gene by site directed PCR mutagenesis using primers gltA_R164L_for and gltA_R164L_rev. The PCR product was DpnI digested and transformed into NEB 5-alpha competent E. coli cells (NEB). The resulting plasmid, pACT3-gltAR164L was isolated and verified by DNA sequencing to contain the desired mutation. For construction of vector pACT3w-ppcK620S-gltAR164L, the mutant gltAR164L gene was amplified from the pACT3-gltAR164L plasmid using Phusion polymerase (Biolabs) and primers gltA_R164L_for_1 and gltA_R164L_for_2. The PCR product was purified and recombined into the pACT3w-ppcK620S vector that was linearized with HindIII and XbaI, using the In-Fusion® HD Cloning Kit (Clontech).
Glucose and extracellular metabolites were quantified on a Dionex Ultimate 3000 HPLC system equipped with a UV and an RI (Shimadzu RID 10A) detector, an Aminex HPX-87H column thermostated at 32 °C, and a “Micro-Guard cation H Refill Cartridge” pre-column. Dilute sulfuric acid (1.25 mM) was used as the mobile phase at an isocratic flow rate of 0.5 ml/min.
Metabolic flux analysis
The strain was grown in batch culture using a 0.5 l fermenter (Multifors Infors HT, The Netherlands) with a working volume of 0.4 l coupled to a Mass Gas Analyzer (Proline Dycor, Ametek process instrument, USA). Cells were cultivated in modified M9 medium adapted for IC-MS/MS analysis  that contained 50 mM glucose (ratio of uniformly labeled to C1-labeled glucose was 1/4), 0.6 mM IPTG and 25 µg/ml chloramphenicol. Temperature, pH, air flow, and stirring speed were maintained at 37 °C, pH 7 (with KOH 1 M), 0.2 l/min and 800 rpm, respectively. Under these conditions, oxygen concentration remained above 50% of saturation throughout the cultivation. The N2, O2, Argon, CO2 concentrations in the bioreactors off-gas were measured on-line using a Mass Gas Analyzer.
Quantification of extracellular metabolites
Culture broth was separated from cells by centrifugation over 0.45 µm pore size membranes (Minisart, Sartorius) and stored at − 20 °C until analysis. To quantify secreted metabolites, clear supernatant was subject to 1H 1D-NMR analysis (Avance 800 MHz spectrometer, Bruker, Germany) carried out at 292 °K, using a 30° pulse and a relaxation delay of 20 s. Trimethylsilyl propionate was used as internal standard.
Quantification of mass isotopologues in intracellular metabolites
Approximately 0.8 ml samples (cells + culture medium) with a cell concentration of 0.4 g/l were manually withdrawn from the bioreactor and directly quenched and extracted by mixing with 3 ml of a mixture of acetonitrile, methanol, and formic acid (0.1 M) (40:40:20 v/v), and incubation at − 20 °C for 1 h. Next, the tubes were moved to − 80 °C until further treatment. Sample evaporation was performed in a rotavapor (Büchi, Switzerland) during approximately 15 h until complete dryness. Afterwards, the samples were dissolved in a 500 μl ultrapure water and stored at − 20 °C until analysis. IC-MS/MS analysis was carried out as described by  to quantify the isotopic enrichment of selected metabolites. The analyzed metabolites were PEP, R5P, S7P, 6PG, G6P, FBP, F6P, 23 PG, Cit, Fum, Mal and Suc. Raw peak areas were corrected for the contribution of all naturally abundant isotopes using the IsoCor software . In addition, label incorporation into secreted acetate and malate was measured using 1H 1D-NMR as described above.
Calculation of fluxes
Intracellular carbon fluxes were calculated from data on mass isotopologue enrichments and production/consumption rates of extracellular metabolites using the Influx_s software .
Efficient malate production requires inactivation of malic enzymes and dehydrogenases, and appropriate expression of malate-insensitive PEP carboxylase
Fermentation products of E. coli MG1655 mutants in mineral medium with glucose as the carbon source
0.32 ± 0.02
0.01 ± 0.01
0.28 ± 0.10
0.48 ± 0.04
0.27 ± 0.02
0.06 ± 0.00
0.17 ± 0.02
0.88 ± 0.15
0.33 ± 0.03
0.06 ± 0.03
0.18 ± 0.01
0.34 ± 0.08
0.27 ± 0.02
0.04 ± 0.00
0.15 ± 0.02
1.31 ± 0.20
Δmdh Δmqo ΔackA-pta
0.23 ± 0.02
0.01 ± 0.00
1.30 ± 0.05
0.21 ± 0.02
Δmdh Δmqo ΔackA-pta ΔmaeA
0.22 ± 0.02
0.03 ± 0.02
0.17 ± 0.02
0.79 ± 0.02
Δmdh Δmqo ΔackA-pta ΔmaeA ΔmaeB
0.16 ± 0.06
0.12 ± 0.04
0.06 ± 0.02
0.24 ± 0.04
1.06 ± 0.25
Δmdh Δmqo ΔackA-pta ΔmaeA ΔmaeB
0.12 ± 0.03
0.13 ± 0.02
0.04 ± 0.01
0.95 ± 0.02
0.69 ± 0.10
Δmdh Δmqo ΔackA-pta ΔmaeA ΔmaeB
0.18 ± 0.01
0.23 ± 0.01
0.03 ± 0.01
0.06 ± 0.03
1.65 ± 0.09
Δmdh Δmqo ΔackA-pta ΔmaeA ΔmaeB
0.13 ± 0.01
0.14 ± 0.03
0.05 ± 0.04
0.96 ± 0.03
0.77 ± 0.08
Δmdh Δmqo ΔackA-pta ΔmaeA ΔmaeB
0.28 ± 0.02
0.37 ± 0.02
0.14 ± 0.01
0.00 ± 0.00
0.64 ± 0.01
Δmdh Δmqo ΔackA-pta ΔmaeA ΔmaeB
0.21 ± 0.00
0.48 ± 0.02
0.11 ± 0.02
0.28 ± 0.05
0.33 ± 0.04
Fermentation products of E. coli mutants in mineral medium with glucose as the carbon source
Additional genotype modifications
0.20 ± 0.06
0.40 ± 0.08
0.09 ± 0.03
0.56 ± 0.03
0.19 ± 0.05
0.42 ± 0.05
0.10 ± 0.04
0.55 ± 0.06
0.21 ± 0.01
0.55 ± 0.02
0.11 ± 0.01
0.01 ± 0.00
0.43 ± 0.00
0.16 ± 0.02
0.30 ± 0.07
0.07 ± 0.03
0.11 ± 0.02
0.29 ± 0.22
ΔiclR ΔackA ΔpoxB
0.22 ± 0.03
0.35 ± 0.00
0.10 ± 0.01
0.56 ± 0.01
0.02 ± 0.00
0.15 ± 0.02
0.53 ± 0.03
0.06 ± 0.04
0.04 ± 0.03
0.38 ± 0.04
0.15 ± 0.02
0.82 ± 0.07
0.06 ± 0.02
0.02 ± 0.04
0.25 ± 0.09
We then tested the impact of expressing the malate-insensitive PpcK620S mutant in strains that were still wild-type for at least one malic enzyme, or that still contained the functional AckA-Pta-dependent acetate pathway. We found that malate yields strongly decreased in strains expressing at least one malic enzyme and did not exceed 0.15 mol/mol (Additional file 1: Table S1), whereas the presence of the AckA-Pta pathway only had a minor impact on the malate yield which was estimated at 0.4 mol/mol (Table 2). Taken together these results show that inactivation of all malate dehydrogenases and malic enzymes together with appropriate expression of a malate insensitive Ppc mutant are necessary and sufficient to enable significant malate production.
Characterization of carbon flux distribution in a malate-producing strain and further genotype optimization
After having identified the major requirements for aerobic malate production in E. coli, we carried out a detailed analysis on the impact of additional genetic modifications on malate production by this organism. Starting from strain Sy502, which carried deletions in both malate dehydrogenases and malic enzymes (Δmdh Δmqo ΔmaeA ΔmaeB) and which had a malate yield of 0.4 mol/mol, we sequentially deleted the transcriptional repressor of the glyoxylate shunt genes (aceA, aceB), encoded by iclR [30, 31], and the enzymes acetate kinase and pyruvate oxidase, encoded by ackA  and poxB , respectively. We observed that the transcriptional derepression of the glyoxylate pathway upon deletion of iclR in strain Sy502 giving rise to strain Sy504 did not result in an increased malate yield. In addition, acetate production remained unchanged when compared to strain Sy502 (Table 2), which is at variance to the behavior of an ΔiclR single mutant that is known to have reduced acetate formation . Nevertheless, we continued to work with strains that carried an iclR deletion to assure complete derepression of the glyoxylate shunt. Deletion of ackA (Sy510) increased malate production by 24% and decreased acetate (Table 2). Deleting poxB alone (Sy508) or together with ackA (Sy512) strongly reduced acetate production, but also resulted in an up to 50% drop of malate production compared to strain Sy510, which was mainly due to an augmented production of pyruvate (Table 2). These results showed that the major metabolic by-product acetate could not be channeled into the Krebs cycle by simply deleting the ackA and poxB-dependent acetate pathways. In addition, the strains that carried the ackA deletion alone or in combination with a deletion of poxB (Sy510, Sy512) exhibited strongly extended lag phases (not shown) which was in agreement with previous studies [35, 36]. The strategy of increasing malate production by directly engineering the acetate pathways was therefore dismissed.
To identify alternative metabolic targets to increase malate production without deleting the acetate pathways we carried out a carbon flux analysis on strain Sy504. The strain was cultivated on 13C-labelled glucose in a bioreactor where glucose consumption and the formation of the metabolic end-products biomass, carbon dioxide, and organic acids were monitored. Samples for the quantification of 13C-label enrichment in individual metabolite pools were withdrawn manually during exponential phase and quantified by IC-MS/MS analysis . In addition, the label incorporation into acetate and malate was measured using 1H 1D-NMR.
As expected, strong differences in carbon flux repartitioning between wild-type strains [34, 38, 39] and the malate-producing strain Sy504 have been observed regarding the metabolic fate of PEP and the solicitation of the Krebs cycle and glyoxylate shunt reactions. Since oxaloacetate cannot be regenerated from malate in strain Sy504, the net-flux from PEP to oxaloacetate, that is, the flux over PEP carboxylase minus the flux over PEP carboxykinase, is on average 60% higher in this mutant than in the corresponding E. coli MG1655 wild-type strains (Additional file 1: Table S2).
While the flux from pyruvate to acetyl-CoA remained largely the same in all strains, acetyl-CoA was utilized very differently in our strain when compared to wild-type cells. Sy504 produced nearly 50% less acetate, and condensed a particularly large fraction of 30 mol% acetyl-CoA with glyoxylate to yield malate. Even in an ΔiclR single mutant, which has a derepressed glyoxylate shunt , nearly two-times less acetyl-CoA is directly converted into malate which indicates a particularly strong solicitation of the glyoxylate shunt in the malate-producing strain. The split ratio of fluxes at the isocitrate lyase (Icl)–isocitrate dehydrogenase (Icd) bifurcation was 5 in strain Sy504 (Additional file 1: Table S2), whereas it was only 0.5 in the ΔiclR mutant  during growth on glucose, and 0.4 during growth of wild type cells on acetate . Even more strikingly, no carbon flux was observed between 2-oxoglutarate and succinate in our malate-producing strain (Fig. 2). Our study did not identify the actual physiological reason for this unexpected behaviour. However, since high flux across the glyoxylate shunt is required to attain the maximum theoretical malate yield of 1.33 mol/mol with the this pathway , this result of the flux analysis made clear that malate production could not be significantly increased by engineering the Icl/Icd node.
Instead, our attention was attracted by the observation that strain Sy504 produced 50% less acetate and 20% more malate in the bioreactor when compared to shake flask cultivations (Table 1, Fig. 2). We hypothesized that better aeration of the fermenter cultures could explain increased malate production in the bioreactor. Oxygen limitation is known to cause both ArcA-mediated repression of genes implicated in respiratory metabolism and accumulation of NADH . We therefore tested the effect of deleting the transcriptional repressor ArcA, and of overexpressing the NADH-insensitive citrate synthase mutant GltAR164L . We found that the deletion of arcA in strain Sy729 which bears the iclR deletion increased the malate yield to 0.53 mol/mol (Table 2). The additional overexpression of GltAR164L in strain Sy731 resulted in a further improved malate yield which amounted to 0.82 mol/mol. It is of note that this increase of malate yield with strain Sy731 was accompanied by a strongly reduced acetate production which dropped to only 0.28 mol/mol without requiring the deletion of any of the acetate-producing pathways. The additional deletion of aspartase, encoded by aspA, did not increase malate production (not shown).
The dicarboxylic acid transporter DcuA is the major malate-exporting permease in the engineered strain
In the present study we investigated the metabolic requirements for Krebs cycle-dependent production of malic acid in E. coli. We found that significant malate production under these conditions required deletion of all malic enzymes and dehydrogenases, and concomitant expression of a malate-insensitive PEP carboxylase. Interestingly, there was almost no gradual increase of malate production upon step-wise introduction of these metabolic modifications, but all genetic modifications had to be present simultaneously to trigger malate production. These results appear to be at variance with data of  who reported aerobic production of malate at a yield of 0.56 mol/mol upon expression of a PEP carboxykinase (Pck) from Mannheimia succiniciproducens in an E. coli pta mutant. It is not clear to us how aerobic malate production could be achieved in this metabolic set-up given that (i) reduction of oxaloacetate (OAA) to malate requires high NADH/NAD ratios which are commonly only achieved under oxygen-limited or anaerobic conditions in E. coli, (ii) Pck-dependent synthesis of OAA from PEP requires high carbon dioxide and PEP concentrations , which are commonly achieved by imposing either anaerobic conditions or sparging with carbon dioxide [11, 15] and by deleting the PEP-consuming phosphotransferase system or inactivating pyruvate kinase [11, 15, 16]. In addition, (iii) our own results show in agreement with the observations made by Zhang et al.  that activity of the malic enzymes prevents significant malate accumulation (Additional file 1: Table S2). The actual reason for these apparent discrepancies remains unclear which may indicate our still incomplete understanding of the metabolic regulation that occurs at the PEP/OAA/malate/pyruvate node in E. coli.
The major metabolic by-product in our aerobic metabolic setup was acetate. Our attempts to reduce acetate secretion by deleting the AckA and/or PoxB-dependent pathways came at the cost of extended lag-phases or even reduced malate production. We therefore set out to engineer strains that produced less acetate despite having functional acetate pathways. Acetate production is mainly regulated by citrate synthase activity. Citrate synthase is allosterically inhibited by high intracellular NADH concentrations, and excess acetyl-CoA is converted to acetate instead of being condensed with oxaloacetate to enter the Krebs cycle in the form of citrate [42, 49, 50]. In agreement with this notion, the deletion of the transcriptional repressor of respiratory enzymes, ArcA, and the overexpression of NADH-insensitive citrate synthase reduced acetate formation by 50% and increased malate production by ~ 90% (when comparing strains Sy504 and Sy731). Together, these results indicated that reducing acetate production via engineering NADH metabolism and citrate synthase was an effective means to improve the performance of malate-producing strains.
We found that malate production by our strains coincided with the accumulation of significant amounts of fumarate. Both compounds accumulated in the supernatant at a molar ratio of approximately 8, which is very similar to the ratio of their intracellular concentrations that was estimated with approximately 12 . Thus, because the malate/fumarate ratio is imposed by the thermodynamic equilibrium of the reversible fumarase reaction, Krebs cycle-dependent malate production will almost inevitably coincide with the formation of fumarate as a co-product. In line with these arguments, we found that the dicarboxylic acid transporter DcuA, which accepts both malate and fumarate as substrates , was responsible for malate secretion. Only replacement of this rather unspecific permease by a highly malate-specific transporter could reduce fumarate secretion during Krebs cycle-dependent malate production.
In summary, Krebs-cycle dependent malate production can be achieved at the cost of lower maximum product yields and significant accumulation of fumarate as a metabolic by-product. These results make this metabolic engineering strategy unattractive when compared to Ppc or Pck-dependent pathways if malate is the actual target molecule. However, if malate is an intermediate product which is further processed to yield derivatives such as DHB , fumarate will not accumulate and the additional cofactors NAD(P)H and ATP which are generated in the Krebs cycle and respiratory chain can be used to increase product yields. Our study has laid the foundation for these microbial product syntheses.
Our study was carried out in aerobic shake flasks on mineral M9 medium. These cultivation conditions are clearly not representative for a fermentation process which enables cost efficient production of malate which would require to carry out the fermentations in bioreactors using low-cost mineral salt medium . Under such conditions, product titers and yields obtained with the strains described in this work may significantly change. However, at the present stage of our analyses we focused on the fundamental genetic requirements for Krebs cycle-dependent malate production, which represents an intermediate stage on the way to the construction of production strains for biosynthesis of malate-derived value-added chemicals such as DHB.
TW and JMF originally conceived the general structure of the project. DT, AB, CD and RI carried out strain engineering. CA and AB performed fermentation process and physiological analysis. MC-H and SH carried out metabolic flux analysis. TW and JMF wrote the manuscript. All authors read and approved the final manuscript.
The authors are grateful to Amélie Vax, Hélène Serrano-Bataille, Florence Calvayrac, and Julie Fredonnet for their technical assistance. We also acknowledge support from MetaToul (Metabolomics & Fluxomics facilities, Toulouse, France, http://www.metatoul.fr), which is part of the national infrastructure MetaboHUB-ANR-11-INBS-0010 (The French National Infrastructure for Metabolomics and Fluxomics, http://www.metabohub.fr).
The authors declare that they have no competing interests.
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This work was supported by the French National Research Agency (ANR programme d’Investissement d’Avenir) ANR-10-BTBR-05-01.
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