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Biotechnology for Biofuels

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Metabolic engineering of Escherichia coli for production of n-butanol from crude glycerol

Biotechnology for Biofuels201710:173

https://doi.org/10.1186/s13068-017-0857-2

©  The Author(s) 2017

Received: 14 March 2017

Accepted: 27 June 2017

Published: 4 July 2017

Abstract

Background

Crude glycerol in the waste stream of the biodiesel production process is an abundant and renewable resource. However, the glycerol-based industry is usually afflicted by the cost for refinement of crude glycerol. This issue can be addressed by developing a microbial process to convert crude glycerol to value-added chemicals. In this study, Escherichia coli was implemented for the production of n-butanol based on the reduced nature of glycerol.

Results

The central metabolism of E. coli was rewired to improve the efficiency of glycerol metabolism and provide the reductive need for n-butanol in E. coli. This was carried out in several steps by (1) forcing the glycolytic flux through the oxidation pathway of pyruvate, (2) directing the gluconeogenic flux into the oxidative pentose phosphate pathway, (3) enhancing the anaerobic catabolism for glycerol, and (4) moderately suppressing the tricarboxylic acid cycle. Under the microaerobic condition, the engineered strain enabled the production of 6.9 g/L n-butanol from 20 g/L crude glycerol. The conversion yield and the productivity reach 87% of the theoretical yield and 0.18 g/L/h, respectively.

Conclusions

The approach by rational rewiring of metabolic pathways enables E. coli to synthesize n-butanol from glycerol in an efficient way. Our proposed strategies illustrate the feasibility of manipulating key metabolic nodes at the junction of the central catabolism. As a result, it renders the intracellular redox state adjustable for various purposes. Overall, the developed technology platform may be useful for the economic viability of the glycerol-related industry.

Keywords

Metabolic engineeringCentral metabolismn-ButanolCrude glycerol

Background

Fossil fuels are afflicted by their unsustainability and excessive emission of greenhouse gas after use, which has overshadowed our daily life. It has inevitably urged the requirement for biofuels from renewable resources as crude oil replacement because they are sustainable and environment-friendly [1]. Among alternative fuels, n-butanol is of particular interest while it possesses a property superior to ethanol in terms of energy density, volatility, and hygroscopicity [2]. Moreover, n-butanol can be transported by the existing infrastructure and readily used to fuel vehicle motors after blended with gasoline [3]. Clostridium species have long been employed for the mass production of n-butanol, known as the acetone–butanol–ethanol (ABE) fermentation process [4]. This fermentation scheme starts with the acidogenesis followed by the solventogenesis. However, this biphasic production pattern is susceptible to the environmental variation and renders the operation of the ABE fermentation technically challenging.

Many surrogate microbes have been successfully illustrated for the n-butanol production after recruitment of the clostridial CoA-dependent pathway for n-butanol [5–8]. In spite of their feasibility, these research efforts are still discouraged by a low production titer. It is recognized that the redox balance of NADH and NAD+ favors the reductive production of n-butanol. The challenge is that the NADH output from glucose catabolism is insufficient to meet the NADH requirement for the synthesis of n-butanol. This issue has been addressed in Escherichia coli by enhancement of the pyruvate dehydrogenase (PDH)- and formate dehydrogenase (FDH)-catalyzed reaction steps in glycolysis. As a result, the approach increases the intracellular NADH level and leads to a higher production titer of n-butanol [9–11]. We have tackled the problem by building a redox-balanced synthetic pathway which is distributed into two E. coli strains [12]. As recognized, the central metabolism consists of fueling pathways that dictate the availability of NADH. Our alternative strategy has therefore rerouted the central pathways involving glycolysis, the pentose phosphate (PP) pathway, and the tricarboxylic acid (TCA) cycle to modulate the intracellular NADH level [13]. Overall, the E. coli strains as engineered in our two approaches enable effective production of n-butanol.

A commercialized bioprocess of n-butanol can be readily realized by a cost-effective feedstock. Biodiesel has been utilized as an alternative fuel for transportation. The annual production yield of biodiesel increases substantially with the pressing need for renewable fuels. Glycerol is a byproduct generated in the production process of biodiesel. The extending market demand has resulted in a large amount of glycerol currently available in the market [14]. The glycerol surplus greatly reduces the price of crude glycerol, which negatively affects the economic viability of the glycerol-producing, oleochemical, and biodiesel industries. The situation is even worsened by the additional cost for disposal of glycerol waste. Therefore, it is appealing to develop a technology platform that converts crude glycerol to the value-added products [15]. Used as a feedstock, glycerol is attractive because it has the highly reduced carbon atoms and enables generation of more reducing equivalents than glucose [16]. This advantage of glycerol makes it more favorable for production of reduced compounds. However, glycerol metabolism is less effective than glucose metabolism in E. coli. In this study, E. coli was engineered for the production of n-butanol from glycerol. This was systematically carried out by manipulation of central metabolism and glycerol catabolism. Consequently, the proposed approach conferred the strain with the ability to produce n-butanol from crude glycerol in an effective manner.

Results and discussion

Microaerobic production of n-butanol from glycerol

Strain BuT-8 harbors a functional pathway for the synthesis of n-butanol (Table 1) [12]. This heterologous CoA-dependent pathway consists of hbd, crt, and adhE2 from Clostridium acetobutylicum, phaA from Cupriavidus necator, and ter from Treponema denticola (Fig. 1). Moreover, it lacks the endogenous adhE, ldhA, pta, and frdA genes responsible for the production of mixed acids. This helps to reduce carbon waste and increase NADH availability. The microaerobic utilization of glycerol in E. coli is far superior to the fermentative metabolism [16]. Therefore, the microaerobic production of n-butanol from crude glycerol was investigated in this study. A producer strain was developed starting with strain BuT-8. It is well recognized that the efficient production of n-butanol requires more available NADH [10]. According to the previous study [16], pflB plays a main role in the oxidation of pyruvate to acetyl-CoA during the microaerobic utilization of glycerol. In contrast to the PflB counterpart, PDH complex (encoded by aceEF-lpdA*) mediates the pyruvate oxidation with concurrent generation of NADH. Therefore, PDH in the strain was enhanced to compete with PflB for more NADH production. In addition, the gluconeogensis involving fba, fbp, and pgi occurs in E. coli during the microaerobic growth on glycerol [16]. Accordingly, zwf and pgl were augmented in the strain to direct the gluconeogenic carbon flux into the PP pathway for generation of NADPH. NADPH was then converted to NADH in the strain equipped with the elevated udhA [17]. Finally, the construction gave rise to strain BuT-12A.
Table 1

The E. coli strains applied in this study

Strain

Characteristic

Source

BuT-8

ΔfrdA ɸ80attB::PλPL-ter λattB::PλPL-crt

ΔadhE::ɸ80attB::PλPL-pha-hbd

ΔldhA::λattB::PλPL-adhE2

12

BuT-12A

as BuT-8 ∆lpdA λattB::PλPL-lpdA *

PλPL-aceEF PλPL-zwf ΔatoD::PλPL-pgl

PλPL-UdhA

This study

BuT-12-2

as BuT-12A PλPL-gldA PλPL-dhaKLM

This study

BuT-12-3

as BuT-12-2 Δzwf

This study

BuT-16

as BuT-12A lacO-gltA

This study

lpdA* the mutant, lpdA exhibiting insensitivity to NADH

Figure 1
Fig. 1

The central metabolic pathways of E. coli connecting glycerol catabolism to n-butanol synthesis. The catabolic route of glycerol includes the glpK-glpD and the gldA-dhaKLM pathways. The heterologous pathway for the synthesis of n-butanol is composed of phaA, hbd, crt, ter, and adhE2 genes (dotted line). The genes involved in the metabolic pathways: aceEF-lpdA*: pyruvate dehydrogenase complex; adhE, aldehyde–alcohol dehydrogenase; adhE2, butyraldehyde–butanol dehydrogenase; crt, crotonse; hbd, 3-hydroxybutyryl-CoA dehydrogenase; ldhA, lactate dehydrogenase; fba, fructose bisphosphate aldolase; fbp, fructose 1,6-bisphosphatase; frdABCD, fumarate reductase; pflB, pyruvate-formate lyase; gltA, citrate synthase; glpF, glycerol facilitator; gldA, glycerol dehydrogenase; dhaKLM, dihydroxyacetone kinase; glpK, glycerol kinase; glpD, glycerol 3-phosphate dehydrogenase; pgi, phosphoglucose isomerase; pgl, lactonase; phaA, acetoacetyl-CoA thiolase; pta, phosphate acetyltransferase; ter, trans-enoyl-CoA reductase; udhA, transhydrogenase; zwf, glucose-6-phosphate dehydrogenase. The undesired genes in the pathways are deleted as marked with “X.” ACE acetate; EtOH ethanol; DHAP dihydroxyacetone phosphate; FDP fructose 1,6-bisphosphate; F6P fructose-6-phosphate; LAC lactate; FOM formate; G6P glucose-6-phosphate; CIT citrate; OAA oxaloacetate; PEP phosphoenolpyruvate; 3-PGA 3-phosphoglyceraldehyde; PYR pyruvate; SUC succinate

Pure glycerol was first used for illustration. The microaerobic production of n-butanol was carried out using the shake-flask culture of strain BuT-12A while strain BuT-8 served as a control. As shown in Fig. 2a, b, strain BuT-12A enabled production of 60% more n-butanol than the control strain (2.1 vs. 1.3 g/L) at 24 h of fermentation. The result leads to productivity of 0.09 g/L-h and the conversion yield of 0.23 g/g (Table 2), which accounts for 57.2% of the theoretical yield (ca. 0.40 g/g glycerol).
Figure 2
Fig. 2

Microaerobic production of n-butanol in strains with the amplification of the fueling pathways. The E. coli strains were grown in M9Y medium containing 20 g/L pure glycerol and the fermentations were carried out for 24 h. The experiments were conducted in triplicate. Keys a the fermentation of strain BuT-8; b the fermentation of strain BuT-12A

Table 2

Summary of the fermentation kinetics for producer strains

Strain

P B

Y B/G

Gene product targeted for manipulation

PDH

Zwf

Pgl

GldA

DhaKLM

GltA

BuT-8

0.054

0.16

W

W

W

W

W

W

BuT-12A

0.09

0.23

+

+

+

W

W

W

BuT-12-2

0.13

0.29

+

+

+

+

+

+

BuT-12-3

0.14

0.32

+

−

+

+

+

W

BuT-16

0.18

0.35

+

+

+

+

+

<

 

0.24*

0.34*

      

The fermentation was carried out with the cell density at OD550 of 0.2. Strain BuT-16 was grown in M9Y medium containing crude glycerol of 20 g/L for 40 h. The others were cultured on pure glycerol of 20 g/L for 24 h. The development course of producer strains for the production of n-butanol was shown in Additional file 1: Fig. S1. Note: W, wild type; +, enhancement; −, absence; <, suppression; P B, n-butanol productivity (g/L/h); Y B/G, conversion yield of n-butanol on glycerol (g/g)

* The fermentation was conducted with the cell density at OD550 of 5 and crude glycerol of 30 g/L for 36 h

Enhancement of the anaerobic glycerol catabolism

As indicated in Fig. 1, two catabolic pathways of glycerol existing in E. coli include the glpK-glpD and the gldA-dhaKLM routes. The former pathway is responsible for the aerobic catabolism of glycerol while the latter route prevails under the anaerobic condition [18]. In addition, the gldA-dhaKLM pathway that mediates the conversion of glycerol to dihydroxyacetone phosphate (DHAP) generates extra NADH. Direction of more glycerol into the gldA-dhaKLM pathway is expected to increase the intracellular NADH, which may favor the n-butanol production. Strain BuT-12-2 was thus obtained by genomic fusion of a strong promoter (PλPL) with gldA and the dhaKLM operon to enhance their expression levels in strain BuT-12A. In comparison with strain BuT-12A, strain BuT-12-2 exhibited a 18-fold more GldA activity (0.306 vs. 0.016 U/mg protein) and a 2.5-fold more DhaKLM activity (0.021 vs. 0.006 U/mg protein). The microaerobic culturing of strain BuT-12-2 was conducted in a similar way. At the end of fermentation, the strain utilized 10.5 g/L glycerol and produced 3 g/L n-butanol at 24 h (Fig. 3). The conversion yield (ca. 0.29 g/g) and productivity (ca. 0.13 g/L/h) for strain BuT-12-2 are increased by 26 and 44% than those for BuT-12A, respectively. For microaerobic utilization of glycerol in E. coli, the glpK-glpD pathway is absolutely required while the glycerol utilization rate can be reduced by 50% in the absence of the gldA-dhaKLM route [16]. In the current case, the significance of the gldA-dhaKLM pathway is acknowledged by its positive contribution to the microaerobic production of n-butanol from glycerol.
Figure 3
Fig. 3

Microaerobic production of n-butanol in the strain with the enhanced glycerol catabolism. Escherichia coli strain BuT-12-2 was engineered by enhancement of the gldA-dhaKLM catabolic route. The strain was grown in M9Y medium containing 20 g/L pure glycerol and the fermentations were carried out for 24 h. The experiments were conducted in triplicate

Restriction of the TCA cycle

Strain BuT-12-2 is engineered with redistribution of carbon flux in central metabolism interconnecting the anaerobic catabolism of glycerol, the oxidative PP pathway, and the oxidative pathway of pyruvate. As revealed in Fig. 1, the synthesis for one molecule of n-butanol requires 4 molecules of NADH and 2 molecules of acetyl-CoA. The gldA-dhaKLM pathway of glycerol catabolism produces 2 molecules of pyruvate and 4 mol of NADH at the expense of 2 molecules of glycerol, which suffices the need of NADH. Extra NADH is generated after a part of carbon flux is driven into the PDH-based route and the oxidative PP pathway. Therefore, strain BuT-12-2 likely possesses a surplus of NADH. Note that the catabolic flux of glycerol bifurcates at the DHAP node where the gluconeogenic and the glycolytic flux move towards the PP pathway and the TCA cycle (Fig. 1), respectively. To address the issue, the PP pathway was first targeted to engineer. In addition to provision of precursors for nucleic acids and aromatic amino acids, the PP pathway generates NADPH for use in the reductive biosynthesis. The PP pathway undergoes the oxidative and nonoxidative routes in response to the intracellular requirement for NADPH [19]. Strain BuT-12-2 with enhanced zwf-pgl mainly assumes the oxidative PP pathway with generation of NADPH which is converted to NADH mediated by UdhA. To change the operation mode in the PP pathway, zwf was deleted in strain BuT-12-2 to obtain strain BuT-12-3. Consequently, the gluconeogenic carbon flux in strain BuT-12-3 is forced through the nonoxidative PP pathway without generation of the reducing equivalent. Strain BuT-12-3 was grown under the microaerobic condition and finally produced 3.4 g/L n-butanol at 24 h (Fig. 4). The result leads to a marginal improvement in the conversion yield and productivity (Table 2). It indicates that the oxidative PP pathway is less significant to provide reducing equivalents for the n-butanol synthesis.
Figure 4
Fig. 4

Microaerobic production of n-butanol in the strain with the gluconeogenic flux via the reductive PP pathway. Escherichia coli strain BuT-12-3 was engineered by the removal of zwf. The strain was grown in M9Y medium containing 20 g/L pure glycerol and the fermentations were carried out for 24 h. The experiments were conducted in triplicate

Next, the TCA cycle was manipulated. The TCA cycle operates in an oxygen-responsive way such that the production level of reducing equivalents varies with either the oxidative or the reductive pathway [19]. To restrict the entry of the carbon flux into the TCA cycle, it is useful to conserve acetyl-CoA (the precursor of n-butanol) and reduce the production of reducing equivalents. According to the previous method [13], the gltA (encoding citrate synthase) cognate promoter P2 was replaced by lacO in strain BuT-12-2 to obtain strain BuT-16. The resulting strain exhibited a 30% lower GltA activity as a result of endogenous LacI-mediated repression. Strain BuT-16 was then cultured and examined for its fermentative performance. Consequently, n-butanol of 4.3 g/L was obtained from 11.5 g/L glycerol at 24 h (Fig. 5a). As compared to strain BuT-12-2, strain BuT-16 displays an increase of around 30 and 40% in the conversion yield and productivity, respectively. Carrying a reduced GltA activity, the glycerol-grown strain BuT-16 grew normally. This is in agreement with the previous study reporting that the growth of E. coli on glucose remains unaffected by a 90% decrease in the GltA activity [20].
Figure 5
Fig. 5

Microaerobic production of n-butanol in the strain with the suppressed TCA cycle. Escherichia coli strain BuT-16 was engineered by suppression of the gltA gene. The strain was grown in M9Y medium containing either 20 g/L pure glycerol or crude glycerol. The fermentations using pure glycerol and crude glycerol were carried out for 24 and 40 h, respectively. The experiments were conducted in triplicate. Keys a the fermentation with pure glycerol; b the fermentation with crude glycerol

At last, the performance of strain BuT-16 using crude glycerol was investigated and the fermentation process was prolonged to obtain the maximum production. The strain consumed all crude glycerol (20 g/L) and produced 6.9 g/L n-butanol at 40 h (Fig. 5b), accounting for the conversion yield of 0.35 g/g and productivity of 0.18 g/L/h. These results are comparable to those on glucose (ca. 0.31 g/g and 0.21 g/L/h) as reported [13]. Consequently, strain BuT-16 greatly reduces the production of byproducts and achieves 5-fold more productivity in comparison with its parent strain BuT-8 (Table 3).
Table 3

Carbon recovery of fermentation products for engineered strains grown on crude glycerol

Strain

Succinate

Ethanol

Lactate

Acetate

Butyrate

Butanol

Total (%)

BuT-8

5.0

9.9

2.3

4.6

10.4

27.3

59.5

BuT-16

0.8

4.2

0.6

2.2

4.5

57.7

70.0

Carbon recovery was calculated as the molar percent of carbon in products per carbon in consumed glycerol. The data for strain BuT-8 were taken at 72 h of fermentation

Production of n-butanol with concentrated cell

The improvement of the n-butanol production was attempted first by using strain BuT-16 (OD550 of 0.2) fed with higher crude glycerol (30 g/L). The strain exhibited a slow consumption of crude glycerol with the productivity reducing to 0.13 g/L/h. This is likely due to the inhibitory effect of the impurity in crude glycerol on the cell [21, 22]. To tackle this problem, the fermentation was carried out using the concentrated cell. As a result, the maximum production titer (8.4 g/L) was obtained with the cell density reaching OD550 of 5 at 36 h (Fig. 6). The result leads to the conversion yield of 0.34 g/g and productivity of 0.24 g/L/h. In addition, the approach with a higher cell density (at OD550 of 10) was implemented for the production of n-butanol. An alternative one was performed with the cell at OD550 of 5 for first 24 h and extra cell was then added to the culture broth (finally reaching OD550 at 10). Consequently, these two approaches exhibited similar fermentation performance and neither of them could further improve the maximum production titer and productivity (Fig. 6). The tolerance threshold of n-butanol for E. coli is strain-dependent and around 8-10 g/L as reported [23, 24]. Therefore, the strain is likely subject to the toxic effect of n-butanol which could disrupt the cell membrane function and abolish the cell metabolism for continuous fermentation. Obviously, such a toxicity-induced inhibitory effect on the cell cannot be circumvented by using the concentrated cell and nutrient supplement [25].
Figure 6
Fig. 6

Production of n-butanol with the high cell density. The fermentation was carried out using E. coli strain BuT-16 at various cell densities in M9Y medium containing 30 g/L crude glycerol. The maximum production of n-butanol was obtained for the case with OD550 of 1 at 48 h and with OD550 of 5 or 10 at 36 h. The fermentation of the strain became sluggish after the peak production. The experiments were duplicated. Keys: 1 OD550 of 1; 2 OD550 of 5; 3 OD550 of 10. Symbols production (gray); productivity (black)

The implementation of enhanced FDH and PDH remains a common strategy to increase intracellular NADH availability for the n-butanol production in glucose-grown E. coli. The results are encouraging in terms of conversion yield and productivity [9–11]. Nevertheless, the super-rich TB medium (mainly 12 g/L tryptone and 24 g/L yeast extract) was employed in these studies and components other than glucose in the medium contributed to 15% of the n-butanol production, which complicates the interpretation of the results [10]. In contrast, n-butanol was merely synthesized from glucose in the M9Y medium as recently illustrated in our studies [12, 13]. With M9Y medium plus glycerol, n-butanol was effectively produced in E. coli by rational rewiring of the central metabolism. This involves the approach to force glycerol catabolism via the gldA-dhaKLM pathway, to channel the glycolytic flux into the pyruvate oxidation route and away from the TCA cycle, and to direct the gluconeogenic flux into the oxidative PP pathway. Consequently, it gives the conversion yield reaching 87% of the theoretical one, the highest value ever reported so far. There are only few studies devoted to the production of n-butanol by genetically modified E. coli strains on TB medium plus pure glycerol [7, 26]. One reported the n-butanol production of 0.55 g/L and the productivity of 22.9 mg/L/h by a producer strain deprived of adhE, ldhA, frdBC, and fnr [7]. The other one reported the n-butanol production of 0.15 g/L and the productivity of 3.2 mg/L/h by a strain which was equipped with FDH and deficient in adhE, ldhA, and frdBC [26]. Nevertheless, the strategy by either evolving our producer strain to tolerate a high concentration of crude glycerol and n-butanol or implementing the production scheme integrated with the in situ removal of n-butanol technology should provide a promising way to further improve the production titer and productivity.

Conclusions

The intracellular redox state in microbes is manifested by the interplay of the carbon flux distributed in the central metabolism. In this study, the catabolic flux of glycerol was modulated by manipulating the fueling pathways in the central metabolism. n-Butanol was highly synthesized as a result of the flux redistribution. It suggests that the DHAP, pyruvate, and acetyl-CoA nodes at the junction of the central metabolic pathways play a vital role in the glycerol-based synthesis of n-butanol. In conclusion, our current study and others propose an appealing way to produce a value-added chemical from crude glycerol [27]. Continued efforts towards the advance of the technology platform may provide a solution to the economic viability of the glycerol-related industry.

Methods

Bacterial culturing

The microaerobic culturing of bacteria essentially followed the previous report [13]. The overnight cultures were grown on Luria–Bertani medium [28] with 2 g/L glycerol. The cell density was determined with a spectrophotometer set at 550 nm (OD550). The seeding cells were inoculated into capped Erlenmeyer flasks (125 mL) containing 50 mL M9Y medium (6 g/L Na2HPO4, 3 g/L KH2PO4, 0.5 g/L NaCl, 1 g/L NH4Cl, 1 mM MgSO4, 0.1 mM CaCl2, and 5 g/L yeast extract) with 20 g/L glycerol. Unless otherwise stated, the initial cell density at OD550 of 0.2 was used to start the shake-flask cultures. The bacterial cultures were maintained in an incubator operated at 100 rpm. Crude glycerol was kindly provided by Yeow Hwa Co., Ltd. (Taichung, Taiwan) with the composition of 67% (w/w) glycerol.

Strain construction

The strains employed in this study are summarized in Table 1. The work for strain construction was carried out with E. coli strain BuT-8 [12]. This strain harbors a genomic copy of the n-butanol synthetic pathway under control of the λPL promoter (PλPL). To endow the strain with enhanced PDH, lpdA of strain BuT-8 was knocked out following the previous report [13]. The PCR DNA containing the partial lpdA inserted with the LE*-kan-RE* cassette was amplified from plasmid pBlue-Ac-lpdA with primers RC12288-RC12290 [13]. By the act of λ Red-mediated recombination, the PCR DNA was directionally integrated and the associated kanamycin-resistant marker (kan) was later removed from the strain’s genome [29]. Furthermore, the NADH-insensitive mutant lpdA (lpdA*) consisting of the E354K mutation was integrated into the strain at the λ prophage attachment site. This was conducted with plasmid pLam-LpdA* carrying PλPL-lpdA* [13]. Lastly, PλPL was fused with the aceEF operon using the PCR DNA amplified from plasmid pPR-aceE with RC12060-RC12086 [13].

In addition, the PCR DNAs were synthesized from plasmids pPR-zwf and pPR-udhA with primers RC11417-RC11418 and RC11419-RC11420 [13], respectively. These DNAs were applied for fusion of zwf and udhA with PλPL to enhance their expression levels in the PP pathway. Meanwhile, pgl was introduced into the strain using plasmid pLoxKm-PL with primers RC13001-RC13293 [13]. To delete zwf, the DNA fragment containing the FRT site-flanked kan (FRT-kan-FRT) cassette was amplified from strain JW1841 (△zwf-777::kan) using primers RC11404 (cagcagagctcgaatggatcgcgttatc) and RC15108 (gtcagagcaggatgattcac). The DNA cassette was then applied to knock out zwf following the reported protocol [29].

Finally, gldA and dhaKLM were fused with PλPL by introduction of PCR DNAs with two homologous extensions into the strain. The PCR DNAs were obtained from plasmid pPL-Gn with primers Gld1-Gld2 and Dha1-Dha2 [29]. Furthermore, the P2 promoter of gltA was replaced with lacO. This was carried out by electroporation of the PCR DNA which was amplified from plasmid pB-gltO-Cm with primers RC13197-RC13201 [13].

Analytical methods

Based on the previous methods [12, 22], glycerol was analyzed using High-Performance Liquid Chromatography equipped with Reflective Index RID-10A (Shimadzu, Japan) while n-butanol was measured by Gas Chromatograph Trace 1300 (Thermo Scientific, USA). Cell-free extract (CFX) was obtained by disrupting bacterial cultures with sonication to recover the supernatant after centrifugation. The total protein content in CFX was then analyzed by using Bio-Rad protein assay kit. The GldA activity was determined by monitoring the reduction of NAD+ at 340 nm at room temperature. The reaction solution (1 mL) contains 100 mM potassium carbonate buffer (pH 7.9), 100 mM glycerol, 33 mM ammonium sulfate, and 1 mM NAD+. The reaction was initiated by adding 100 µL CFX to the reaction solution. Similar to the GldA activity assay, the DhaKLM activity was measured following the reduction of NAD+. The reaction solution (1 mL) consists of 100 mM potassium carbonate buffer (pH 9), 100 mM glycerol, 1 mM MgCl2, 2 mM dithiothreitol, 1 mM PEP, and 1 mM NAD+. The unit (U) of the enzyme activity was defined as μmole/min. The yield of n-butanol on glycerol was calculated as the production amount of n-butanol (g/L) divided by the consumed amount of glycerol (g/L).

Abbreviations

PDH: 

pyruvate dehydrogenase

FDH: 

formate dehydrogenase

PP: 

pentose phosphate

TCA: 

tricarboxylic acid

DHAP: 

dihydroxyacetone phosphate

PλPL : 

λPL promoter

CFX: 

cell-free extract

ACE: 

acetate

EtOH: 

ethanol

FDP: 

fructose 1,6-bisphosphate

F6P: 

fructose-6-phosphate

LAC: 

lactate

FOM: 

formate

G6P: 

glucose-6-phosphate

CIT: 

citrate

OAA: 

oxaloacetate

PEP: 

phosphoenolpyruvate

3-PGA: 

3-phosphoglyceraldehyde

PYR: 

pyruvate

SUC: 

succinate

Declarations

Authors’ contributions

MS constructed bacterial strains and performed fermentation; ZWW analyzed data; CJC and YPC assisted in the design of the study and drafted the manuscript. All authors read and approved the final manuscript.

Acknowledgements

We like to acknowledge Ministry of Science and Technology, Taiwan, for financial support.

Competing interests

The authors declare that they have no competing interests.

Consent for publication

All authors agree to submit the work to the journal.

Funding

This work is supported by Ministry of Science and Technology (MOST 105-2221-E-035-085-MY3 and 105-2622-E-035-013-CC1) and China Medical University (CMU 105-S-50), Taiwan.

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Authors’ Affiliations

(1)
Department of Chemical Engineering, Feng Chia University, Taichung, Taiwan
(2)
Department of Medical Laboratory Science and Biotechnology, China Medical University, Taichung, Taiwan
(3)
Department of Health and Nutrition Biotechnology, Asia University, Taichung, Taiwan
(4)
Department of Medical Research, China Medical University Hospital, Taichung, Taiwan

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