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  • RESEARCH
  • Open Access

Improved ethanol productivity from lignocellulosic hydrolysates by Escherichia coli with regulated glucose utilization

  • 1, 3,
  • 2,
  • 2,
  • 2,
  • 2,
  • 4,
  • 4,
  • 5 and
  • 1, 2Email author
Microbial Cell Factories201817:66

https://doi.org/10.1186/s12934-018-0915-x

  • Received: 9 February 2018
  • Accepted: 24 April 2018
  • Published:

Abstract

Background

Lignocellulosic ethanol could offer a sustainable source to meet the increasing worldwide demand for fuel. However, efficient and simultaneous metabolism of all types of sugars in lignocellulosic hydrolysates by ethanol-producing strains is still a challenge.

Results

An engineered strain Escherichia coli B0013-2021HPA with regulated glucose utilization, which could use all monosaccharides in lignocellulosic hydrolysates except glucose for cell growth and glucose for ethanol production, was constructed. In E. coli B0013-2021HPA, pta-ackA, ldhA and pflB were deleted to block the formation of acetate, lactate and formate and additional three mutations at glk, ptsG and manZ generated to block the glucose uptake and catabolism, followed by the replacement of the wild-type frdA locus with the ptsG expression cassette under the control of the temperature-inducible λ pR and pL promoters, and the final introduction of pEtac-PA carrying Zymomonas mobilis pdc and adhB for the ethanol pathway. B0013-2021HPA was able to utilize almost all xylose, galactose and arabinose but not glucose for cell propagation at 34 °C and converted all sugars to ethanol at 42 °C under oxygen-limited fermentation conditions.

Conclusions

Engineered E. coli strain with regulated glucose utilization showed efficient metabolism of mixed sugars in lignocellulosic hydrolysates and thus higher productivity of ethanol production.

Keywords

  • Ethanol
  • Thermo-regulated glucose utilization
  • Lignocellulosic hydrolysate
  • Escherichia coli

Background

Lignocellulosic biomass holds tremendous potential for sustainable ethanol production to meet the increasing worldwide demand for ethanol, which is currently produced from starch- and sugar-based foodstuff materials [1]. Lignocellulose is composed of various hexose and pentose sugars, such as glucose and xylose [2, 3]. Economic feasibility of ethanol production from biomass, however, remains a challenge, though significant progress has been made in bioconversion of lignocellulose biomass to ethanol since 1970s, including: (1) pretreatment techniques of biomass, (2) enzymes for efficient saccharification, (3) new strains for metabolizing all or most of monosaccharides in lignocellulose hydrolysates, and (4) novel integrated processes for ethanol production and recovery.

Of all the components of lignocellulose-based ethanol production considered, strain development is still one of the most crucial elements for practical commercial process [4]. No single natural microorganism is known to be capable of efficiently converting all sugars from lignocellulose to ethanol [5, 6]. Although engineered ethanologenic Escherichia coli strains have the ability to metabolize various sugars from lignocellulosic biomass, their xylose utilization lags far behind that of glucose due to the preferential use of glucose as carbon and energy source by E. coli, a physiological phenomenon known as carbon catabolite repression (CCR) [7, 8]. Thus, a great deal of effort has been devoted to developing a single microorganism that can consume xylose and glucose simultaneously [914]. For example, to eliminate the CCR effect, strategies to disrupt CCR by inactivating phosphoenolpyruvate:glucose phosphotransferase system (PTS) components have been explored by various researchers [1517].

In the present study, a metabolically engineered E. coli strain with regulated glucose utilization, which uses all monosaccharides from lignocellulose except glucose for cell propagation and all sugars for ethanol production, was constructed. The newly developed strain could utilize xylose, galactose and arabinose but glucose for cell duplication and its glucose catabolism pathway could be re-activated through switching-on transcription of ptsG at elevated temperature after cell duplication completed. A novel bioprocess for ethanol production from biomass was developed. This could provide an alternative route to highly efficient bioconversion of all sugars from biomass hydrolysates to ethanol.

Methods

Strains and plasmids

Strains and plasmids used in this study are listed in Table 1. Primers used in this study are listed in Additional file 1: Table S1. Cultures were stored at − 70 °C in 15% glycerol in the Culture and Information Center of Industrial Microorganism of China Universities at Jiangnan University (CICIM-CU, http://CICIM-CU.jiangnan.edu.cn). Unless otherwise stated, standard molecular biology protocols [18] were used for DNA manipulation.
Table 1

Strains and plasmids used in this study

Strains or plasmids

Genotype/relevant characteristics

Source or references

Strains

 E. coli B0013

Wild isolate

[20]

 E. coli B0013-1030

B0013, Δpta-ackA::difldhA::dif, ΔpflB::dif

[19]

 E. coli B0013-1030H

B0013-1030, xylH*a

[20]

 E. coli B0013-1031H

B0013-1030H, ΔfrdA::dif

This study

 E. coli B0013-1031HPA

B0013-1031H, pEtac-PA

This study

 E. coli B0013-2020H

B0013-1030H, ∆ptsG::dif, ∆glk::dif, ∆manZ::dif

This study

 E. coli B0013-2021H

B0013-2020H ∆frdA::kan-cIts857-pR–pL-ptsG

This study

 E. coli B0013-2021HPA

B0013-2021H, pEtac-PA

This study

Plasmid

 pMD19-T

bla; TA cloning vector

TaKaRa

 pPL-kan

bla, kan, λcIts857, pR pL

[24]

 pT-kan-cIts857-pR–pL-ptsG

bla, kan, frdA::kan-cIts857-pR–pL

This study

 pT-frdA’::kan-cIts857-pR–pL-ptsG

bla, kan, frdA::kan-cIts857-pR–pL-ptsG

This study

 pEtac-PA

kan, pdc and adhB from Zymomonas mobilis

[13]

a xylH* represents reversely mutated xylH ([20])

Escherichia coli B0013-1030 [19] was used as parent strain, in which xylH, encoding membrane component of high affinity xylose transporter [3], is naturally mutated [20]. Its XylH function was restored by homologous replacement of xylH to obtain E. coli B0013-1030H [20]. The ptsG coding for the enzyme IICBGlc of the phosphoenolpyruvate:glucose phosphotransferase system for carbohydrate transport, manZ coding for the IIDMan domain of the mannose PTS permease, and glk coding for glucokinase [16, 21, 22] were disrupted in B0013-1030H to create the glucose-nonutilizing strain E. coli B0013-2020H according to the method described previously [23].

Integration of ptsG expression cassette under control of the temperature-inducible λ pR and pL promoters into the frdA of B0013-2020H to create B0013-2021H was performed according to the method described previously [24]. Briefly, fragment kan-cIts857-pR–pL from plasmid pPL-kan was spliced with ptsG amplified from the chromosomal DNA of B0013 and cloned into pMD19T-vector to construct pT-kan-cIts857-pR–pL-ptsG, in which λ pR and pL promoters was located before start codon of ptsG. The recombinant plasmid was digested with EcoRV and ligated with the fragment containing upstream and downstream homologous arms of frdA to obtain recombinant plasmid pT-frdA’::kan-cIts857-pR–pL-ptsG. The cassette frdA’::kan-cIts857-pR–pL-ptsG was amplified using primers frdA-p1 and frdA-p2, purified and integrated into the locus of frdA in the chromosome of B0013-2020H by electroporation [24] and frdA was simultaneously disrupted. Kanamycin resistant colonies were then selected on plates with 50 μg/ml of kanamycin. Integration of the cassette into frdA was confirmed by colony PCR (1785-bp for the wild-type frdA and 4034-bp after inactivation due to insertion of ptsG with λ pR and pL promoters) and by nucleotide sequencing. The resulting recombinant strain was designated B0013-2021H. The ethanol pathway encoded by pEtac-PA carrying Z. mobilis pdc and adhB [11] was transformed into B0013-2021H to develop ethanologenic recombinant B0013-2021HPA. As a control, B0013-1031HPA was constructed by disrupting frdA in B0013-1030H [24] and by subsequent introduction of pEtac-PA.

Media

Luria–Bertani medium (LB) (5 g/l yeast extract, 10 g/l tryptone, and 5 g/l NaCl) is used for activation and cultivation of strains. Modified M9 medium [24] supplemented with 5 g/l of glucose or xylose was used for strain selection. As for solid medium, agar (15 g/l) is added. Modified M9 medium supplemented with 5 g/l of xylose and 50 g/l of glucose was used for shaking flask fermentation. Glucose and xylose were sterilized separately by autoclaving at 115 °C for 20 min. When it was necessary 100 μg/ml of ampicillin, 30 μg/ml of gentamycin or 50 μg/ml of kanamycin was added into the media.

Fermentation experiments

Shaking flask fermentation was performed in 500-ml flasks containing 100 ml of medium. To prepare inoculum, one single colony from a fresh LB plate was transferred into 50 ml of LB medium in 250-ml flasks and then cultivated at 37 °C, 200 rpm for 10–12 h to an OD600 of 2.0–2.5. Cells were harvested by centrifugation (4300g, 10 min), washed and re-suspended with M9 medium, and then inoculated into 100 ml of fermentation medium to initial cell density of 0.1 at OD600. Fermentation was conducted using a “two-phase-two-temperature” strategy (aerobic cell growth at 34 °C, 200 rpm and then static oxygen-limited fermentation at 42 °C). The flask cultures were first cultivated in shaker at 34 °C, 200 rpm for 12 h and then transferred to static incubation for ethanol fermentation at 42 °C.

Ethanol fermentation experiments in a 7-l bioreactor (Bioflo110; New Brunswick Scientific Co., Inc., Edison, NJ) were accomplished with an initial 3 l working volume. Cells were cultured and collected as mentioned above and inoculated into 250-ml flasks containing 50 ml of modified M9 medium with 5 g/l of xylose to an initial cell density of 0.1 (OD600) and cultivated at 37 °C. Cultures were inoculated into 3 l of modified M9 medium containing 300 ml of corncob hydrolysate syrup. Using “two-phase-two-temperature” strategy as mentioned above, cell growth phase was carried out at 34 °C under aerobic conditions with agitation at 200–1000 rpm and sparging sterile air continuously at a rate of 0.1–1 vvm. When the cell mass reached OD600 of approximately 20, the incubation temperature was raised to 42 °C and maintained for 45 min. And then the oxygen limited fermentation was initiated by stopping air flow and reducing agitation speed to 100 rpm and additional 300 ml of corncob hydrolysate was added at this moment. The same fermentation was carried out with B0013-1031HPA as control except that incubation temperature for cell growth and fermentation was both at 37 °C. The pH was maintained at 7.0 by automatically feeding concentrated NH4OH or 10% H2SO4 (v/v) during the fermentation. The corncob hydrolysate syrup used in this study was prepared based on 70% (w/w) concentrated xylose crystallization mother liquid (Futian Pharmaceutical Company Ltd., China) supplemented with 364 g/l glucose with the volume ratio 1:1. The final syrup contained 266 g/l of glucose, 200 g/l of xylose, 114.5 g/l of arabinose and 27 g/l of galactose.

Analysis of relative expression levels of ptsG using real-time quantitative PCR

Cells grown in LB medium at 34 °C overnight were collected and washed 3 times with cold M9 medium. The cells were then resuspended in cold modified M9 medium containing 5 g/l glucose to OD600 of 0.1 and then incubated for 2 h at 34 or 42 °C. The cells were recovered and total RNA was extracted using the ChargeSwitch® Total RNA Cell Kits (Invitrogen) according to the protocol with on-column DNase digestion. RNA was eluted with Elution Buffer to a sterile microcentrifuge tube. cDNA synthesis was performed using 3 μg of total RNA with PrimeScript Reverse Transcriptase (TaKaRa, Dalian, China) in a 20 μl reaction volume according to the manufacturer’s instructions. Real-time quantitative PCR was performed on Step One System (ABI, USA) to determine mRNA level of ptsG. The PCR reaction system (20 μl) and conditions were according to the method as described [25]. The Ct values were used to quantify the relative expression levels of ptsG by the 2−ΔCt method with the constitutively expressed gapA, encoding glyceraldehyde-3-phosphate dehydrogenase A, as the internal control [26].

Preparation of cell extract and activity assay of phosphoenolpyruvate:glucose phosphotransferase (PTase), pyruvate decarboxylase (PDC) and alcohol dehydrogenase II (ADH II)

Cells grown in LB medium at 34 °C overnight were collected and washed 3 times with sodium chloride solution (0.85%, w/v). The cells were then resuspended in modified M9 medium containing 5 g/l glucose and incubated for 2 h at 34 or 42 °C. The cells were recovered for enzyme activity assay. The cell lysates were prepared according to the method as described previously with some modification [27]. Briefly, about 0.2 g of wet cells were washed with ice-cold sodium chloride solution (0.85%, w/v) and resuspended in 2 ml of 50 mM morpholinepropane-sulfonic acid (MOPS; pH 7.5) buffer containing 10% (v/v) glycerol, 5 mM EDTA, 1 mM benzamidine and 2 mM dithiothreitol. After passage through a French Press Cell (Aminco, USA) and incubation with RNase and DNase for 1 h at room temperature, the solution was centrifuged at 27,000×g and 4 °C for 30 min, and the supernatant was desalted by passing through a PD-10 column (Amersham, GE-Beijing, China).

PTase activity was measured in 50 mM MOPS buffer (pH 7.5) containing 5 mM MgCl2, 10 mM NADH (Sangon Biotech, Shanghai, China) and 100 μg cell extract at 25 °C. The reaction was started by addition of 5 mM glucose, 5 mM phosphoenolpyruvate and 10 U lactate dehydrogenase (Sangon Biotech, Shanghai, China). The concentration of NADH was measured at 340 nm. One unit of PTase activity was defined as the quantity of enzyme required to transform 1 μmol of NADH to NAD+ per minute. PDC and ADH II activities were measured according to the procedure as described previously [13, 28]. Protein concentrations were determined by the method of Bradford with crystalline bovine serum albumin fraction V (Sangon Biotech, Shanghai, China) as described [13, 24].

Analytical methods

Sampling was conducted periodically. Glucose, xylose, arabinose, galactose and ethanol were measured by HPLC according to the method described previously [23] using a HPLC system equipped with Dionex p680 pump (Dionex Corporation, Sunnyvale, CA), a Shodex SH-1011 column (Shodex SH-1011 H610009; Showa Denko K.K., Kawasaki, Japan), and a refractive index detector. The samples were run at 60 °C and eluted at 1.0 ml/min with 0.01 M sulfuric acid. Cell density was monitored turbidimetrically at 600 nm (1 cm light path) using a UNICO UV2000 spectrophotometer. Dry cells weight was calculated using a standard curve (1 OD600 = 0.38 g/l DCW) [24].

Results and discussion

Construction of regulated glucose-utilizing strain E. coli B0013-2021H

To enable controllable glucose utilization by E. coli, glucose-nonutilizing strain E. coli B0013-2020H was successfully constructed by sequentially disrupting ptsG, manZ and glk, which were previously identified to be essential for glucose uptake and metabolism in E. coli [16, 17, 21, 22] (Fig. 1). B0013-2020H failed to grow on glucose (Fig. 1c). Growth characteristics of E. coli B0013-2020H on glucose were also examined by cultivation in M9 medium containing xylose or glucose in shaking flasks at 37 °C and 200 rpm. After cultivation for 12 h, B0013-2020H proliferated to cell density of 3.78 on xylose but failed to grow on glucose (data not shown), indicating that its glucose metabolizing pathway was blocked.
Fig. 1
Fig. 1

Construction and characterization of regulated glucose-utilizing E. coli B0013-2021H. A Modified metabolic pathways of E. coli B0013 and its derivatives; B development flowchart of E. coli B0013-2021H and relatives; C growth characterization of E. coli B0013-2021H on glucose at different temperatures. The cells were cultivated on M9 plates with 5 g/l of glucose at 34 or 42 °C. a: E. coli B0013; b: B0013-1031H; c: B0013-2020H; d: B0013-2021H; D (a) ptsG mRNA fold change quantified by real-time quantitative PCR; (b) Expression level of phosphoenolpyruvate:glucose phosphotransferase in E. coli B0013-2021H at different incubation temperatures; E growth characterization of E. coli B0013-2021H and B0013-1031H. The cells grew in M9 medium supplemented with 5 g/l of glucose at 34, 37 or 42 °C and 200 rpm for 12 h. The cell densities were determined at 600 nm

To restore and artificially regulate glucose utilization of B0013-2020H, a new strain, designated B0013-2021H, was developed in which ptsG was expressed under the control of λ pR and pL promoters, a temperature-inducible switch [24] (Fig. 1b). Growth characteristics of B0013-2021H, B0013-2020H, and the parental strains B0013 and B0013-1031H were compared by cultivating on M9 plates supplemented with glucose at 34 or 42 °C. Both B0013-2021H and B0013-2020H could not grow on glucose at 34 °C, while B0013-2021H, B0013 and B0013-1031H showed robust growth on glucose at 42 °C except B0013-2020H (Fig. 1c). Subsequently, real-time quantitative PCR was employed to determine the mRNA levels of ptsG at 34 or 42 °C. The transcription of ptsG in B0013-2021H was highly induced at 42 °C with more than sixfolds of that in B0013-1031H (Fig. 1Da). The PTase activities in B0013-2021H and B0013-1031H incubated at 34 or 42 °C were further determined. B0013-2021H exhibited trace amounts of PTase activity at 34 °C and about threefolds of higher PTase activity at 42 °C in comparison to that of B0013-1031H (Fig. 1Db), illustrating that the expression of ptsG in B0013-2021H is fully controlled by λ pR–pL promoter.

Growth characteristics of B0013-2021H were further investigated by cultivation in M9 medium with 5 g/l of glucose at 34, 37 or 42 °C and 200 rpm (Fig. 1e). Cell density for B0013-2021H remained unchanged after incubation on glucose for 12 h at 34 °C because ptsG expression was not switched on (Fig. 1e). At 37 °C, B0013-2021H partially restored its growth on glucose with an increase in cell density to OD600 of 2.34, slightly slower growth than that of B0013-1031H (Fig. 1e). When incubation temperature was elevated to 42 °C, B0013-2021H grew more vigorously than B0013-1031H due to the full operation of temperature switch of ptsG at 42 °C (Fig. 1e). The results further confirmed that the expression of ptsG in B0013-2021H was strictly under the control of the temperature-inducible tandem λ pL and pR promoters and elevated incubation temperature switched on the transcription of ptsG in B0013-2021H.

Preferential use of glucose is a major factor limiting economical lignocellulose-based ethanol production. E. coli B0013-2021H with controllable metabolism of glucose provides a simple solution to achieving efficient metabolism of all sugars from lignocellulosic biomass: under aerobic conditions, a relatively low temperature (34 °C) was adopted so that glucose utilization was switched off and the strain utilized all sugars except glucose to grow and the inhibition effect of glucose on other sugars’ utilization was relieved. When the process was shifted to anaerobic conditions, the temperature switch was activated at elevated temperature (42 °C) and thus the expression of ptsG, leading to glucose uptake and catabolism, and efficient production of ethanol by fermenting glucose and other sugars in biomass hydrolysates.

B0013-2021HPA utilized xylose for growth and glucose for ethanol fermentation in shaking flasks

The ethanol synthesis pathway encoded by pEtac-PA was finally introduced into B0013-2021H, resulting in ethanologenic strain B0013-2021HPA (Fig. 1b). As a control, B0013-1031HPA was constructed by deleting frdA in B0013-1030H and the introduction of pEtac-PA (Fig. 1b). At 34 and 42 °C, the activities of PDC in B0013-2021HPA were determined to be 6.8 ± 1.22 U/mg protein and 6.7 ± 1.35 U/mg protein of PDC, respectively, while the activities of ADH II were 3.1 ± 0.65 U/mg protein and 3.2 ± 0.57 U/mg protein, respectively.

To evaluate fermentation performance of B0013-2021HPA, ethanol fermentation was conducted in shaking flasks using a “two-phase-two-temperature” strategy, as described in “Methods”, in M9 medium supplemented with 5 g/l of xylose and 50 g/l of glucose. B0013-2021HPA utilized all of the xylose for growth under aerobic condition at 34 °C whereas glucose concentration remained approximately constant at 50 g/l (Fig. 2). B0013-2021HPA grew to a cell density of 4.9 (OD600) at 12 h and 34 °C and the cultures were then incubated at 42 °C for ethanol fermentation. After 18 h of fermentation, 50 g/l of glucose was exhausted and converted to 24.3 g/l of ethanol (Fig. 2) with the yield of 48.4 g/100 g glucose. Under the same conditions, E. coli B0013-1031HPA mainly consumed glucose for cell growth during the aerobic phase and converted residue glucose and xylose to ethanol during fermentation phase, with the similar yield as that of B0013-2021HPA. Consumption rate of glucose of B0013-1031HPA [2.51 g/(l·h)] was less than that of B0013-2021HPA [3.08 g/(l·h)] because ptsG, under the control of λ pR and pL promoters, in B0013-2021HPA was activated and highly expressed.
Fig. 2
Fig. 2

Ethanol fermentation by E. coli B0013-2021HPA. In 500-ml shaking flasks containing 100 ml of M9 medium with 5 g/l of xylose and 50 g/l of glucose, the cultures were cultivated at 34 °C and 200 rpm during aerobic phase and ethanol fermentation was carried out statically at 42 °C using a “two-phase-two-temperature” strategy. Solid line: B0013-2021HPA; dotted line: B0013-1031HPA. Solid square: xylose; solid circle: glucose; triangle: ethanol; circle: cell mass

E. coli B0013-2021HPA converted mixed sugars to ethanol in bioreactor

Ethanol fermentation performance of B0013-2021HPA on mixed sugars, from corncob hydrolysate for example, was further verified in a 7-l bioreactor with an initial 3 l working volume containing 300 ml of corncob hydrolysate for cell growth and additional 300 ml of corncob hydrolysate was supplemented for ethanol production. The results are summarized in Fig. 3 and Table 2. Significantly, B0013-2021HPA utilized xylose, galactose and arabinose for growth, while glucose was not consumed at all during the aerobic growth at 34 °C and utilization of glucose was initiated after temperature switch to 42 °C. After 12 h of fermentation at 42 °C, the total amount of 260.9 g mixed sugars, including residual glucose and xylose as well as mixed sugars from added corncob hydrolysate were converted to 127.7 g ethanol with the productivity of 4.06 g/(l·h) and sugar consumption rate of 8.28 g/(l·h) (Fig. 3a, Table 2). All these performances are significantly improved in comparison to those of B0013-1031HPA, whose ethanol productivity was 2.85 g/(l·h) and sugar consumption rate was 5.81 g/(l·h) (Fig. 3b, Table 2).
Fig. 3
Fig. 3

Ethanol fermentation of E. coli B0013-2021HPA from corncob hydrolysate in a 7-l bioreactor. Pre-cultured cells of B0013-2021HPA (a) were inoculated into 3 l of modified M9 medium supplemented with 300 ml of corncob hydrolysate. Using a “two-phase-two-temperature” strategy as mentioned in “Methods”, cell growth phase was controlled at 34 °C under aerobic conditions and ethanol fermentation was conducted at 42 °C under oxygen-limited conditions. As for B0013-1031HPA (b), temperature was set at 37 °C, its optimal temperature, for the two phases. Solid circle: glucose; solid triangle: galactose; solid diamond: arabinose; solid square: xylose; triangle: ethanol; circle: cell mass; dotted arrow: temperature switching point (from 34 to 42 °C), 45 min ahead of transition to oxygen-limited condition; arrow: time point of addition of 300 ml of the corncob hydrolysate

Table 2

Consumption rates of sugars and ethanol productivity by B0013-2021HPA and B0013-1031HPA in a 7-l bioreactor

Strains

Consumption rate of sugarsa [g/(l·h)]

Productivity of ethanolb [g/(l·h)]

Whole process

Cell growth

Fermentation

B0013-2021HPA

5.90

3.52

8.28

4.06

B0013-1031HPA

4.74

3.67

5.81

2.85

a Consumption rate of sugars was calculated based on the sugars consumed during aerobic phase or fermentation phase

b Productivity of ethanol was calculated based on the time during fermentation phase

Lignocellulosic hydrolysate, such as corncob hydrolysate, comprises a mixture of sugars, mainly glucose and xylose [29, 30]. In E. coli and many other microorganisms, glucose is preferentially utilized and other sugars would be used only when glucose is nearly depleted due to CCR [8, 15]. To realize simultaneous utilization of pentose and hexose, previous work focused on development of engineered strains, including construction of catabolite repression mutant by mutation of ptsG to achieve simultaneous fermentation of mixed glucose, xylose and arabinose to ethanol with the yield of 0.45 g/g, the productivity of 0.75 g/(l·h) and sugar consumption rate of 1.31 g/(l·h) in 70 h [15]. Also, simultaneous consumption of mixed sugars was achieved by strain adaptation through substrate-selective inoculum preparation or late addition of saccharifying enzyme to delay releasing of glucose, resulting in maximum ethanol productivity of 0.72 g/(l·h) in 40 h and 0.78 g/(l·h) in 48 h, respectively, from corn stover hydrolysate by E. coli FBR5 [31].

Aerobic condition is considered to be more beneficial to utilization of xylose in E. coli [32, 33]. In this work, the metabolic inefficiency for ethanol production from mixed sugars in lignocellulosic hydrolysates was alternatively solved by switching off glucose utilization to allow growth of cells on xylose and other sugars but glucose during the aerobic cell growth phase and by switching on glucose utilization to enable efficient conversion of glucose and other sugars to ethanol.

Notably, sugars consumption patterns of our developed strain were different from other reports [15, 31, 3436]. This may probably due to the differences in genetic background among E. coli strains.

Conclusions

An alternative bioprocess for ethanol production from biomass was successfully developed using a strain genetically engineered to turn on or off glucose utilization in E. coli by a temperature switch, thus relieving the inhibition effect of glucose on utilization of other sugars. The glucose-utilization switched-off cells can preferentially utilize xylose and other sugars present in lignocellulosic hydrolysates for cell growth, while glucose-utilization switched-on cells can efficiently convert glucose and other sugars to ethanol during anaerobic stage for ethanol fermentation. Significantly, utilization efficiency of sugars in lignocellulosic hydrolysates was improved and so was the economic feasibility of ethanol production from biomass.

Declarations

Authors’ contributions

ZW conceived the study. JS, KT and JW conducted the experiments. JS, KT, ZD, XL, KP, SS, BAP and ZW analyzed the data and prepare the manuscript. All authors read and approved the final manuscript.

Acknowledgements

This research was supported financially by The Raising Program of Innovation Team for Tianjin Universities (TD12-5002).

Competing interests

The authors declare that they have no competing interests.

Availability of data and materials

Not applicable.

Consent for publication

Not applicable.

Ethics approval and consent to participate

Not applicable.

Funding

Not applicable.

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Authors’ Affiliations

(1)
Center for Bioresource and Bioenergy, School of Biotechnology, Jiangnan University, 1800 Lihu Avenue, Wuxi, 214122, China
(2)
Department of Biological Chemical Engineering, College of Chemical Engineering and Materials Science, Tianjin University of Science and Technology, TEDA, Tianjin, 300457, China
(3)
School of Life Science and Food Engineering, Huaiyin Institute of Technology, 1st East Meicheng Road, Huaian, 223003, China
(4)
Department of Biotechnology and Food Technology, Durban University of Technology, Durban, 4002, South Africa
(5)
Department of Microbiology, University of Stellenbosch, Matieland, 7602, South Africa

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