Engineering E. colistrain for conversion of short chain fatty acids to bioalcohols
© Mattam and Yazdani; licensee BioMed Central Ltd. 2013
Received: 21 May 2013
Accepted: 4 September 2013
Published: 10 September 2013
Recent progress in production of various biofuel precursors and molecules, such as fatty acids, alcohols and alka(e)nes, is a significant step forward for replacing the fossil fuels with renewable fuels. A two-step process, where fatty acids from sugars are produced in the first step and then converted to corresponding biofuel molecules in the second step, seems more viable and attractive at this stage. We have engineered an Escherichia coli strain to take care of the second step for converting short chain fatty acids into corresponding alcohols by using butyrate kinase (Buk), phosphotransbutyrylase (Ptb) and aldehyde/alcohol dehydrogenase (AdhE2) from Clostridium acetobutylicum.
The engineered E. coli was able to convert butyric acid and other short chain fatty acids of chain length C3 to C7 into corresponding alcohols and the efficiency of conversion varied with different E. coli strain type. Glycerol proved to be a better donor of ATP and electron as compared to glucose for converting butyric acid to butanol. The engineered E. coli was able to tolerate up to 100 mM butyric acid and produced butanol with the conversion rate close to 100% under anaerobic condition. Deletion of native genes, such as fumarate reductase (frdA) and alcohol dehydrogenase (adhE), responsible for side products succinate and ethanol, which act as electron sink and could compete with butyric acid uptake, did not improve the butanol production efficiency. Indigenous acyl-CoA synthetase (fadD) was found to play no role in the conversion of butyric acid to butanol. Engineered E. coli was cultivated in a bioreactor under controlled condition where 60 mM butanol was produced within 24 h of cultivation. A continuous bioreactor with the provision of cell recycling allowed the continuous production of butanol at the average productivity of 7.6 mmol/l/h until 240 h.
E. coli engineered with the pathway from C. acetobutylicum could efficiently convert butyric acid to butanol. Other short chain fatty acids with the chain length of C3 to C7 were also converted to the corresponding alcohols. The ability of engineered strain to convert butyric acid to butanol continuously demonstrates commercial significance of the system.
KeywordsEngineered E. coli Clostridium acetobutylicum Butyric acid Butanol Fermentation
Finding different means for production of biofuel molecules will help in gradual shift from usage of fossil fuels . Ethanol so far has served the purpose of alternative fuel due to its easy and cost effective manufacturing process . Butanol, however, is considered to be closer to the fossil fuel in terms of its energy density and hygroscopicity [3–5].
n-Butanol had traditionally been produced by Clostridium acetobutylicum through ABE fermentation . C. acetobutylicum undergoes acidogenic phase, when it produces majorly acetic acid and butyric acid, followed by solventogenic phase, when it produces acetone, butanol and ethanol (ABE) mix . There are several challenges to the ABE fermentation that prevented this technology from being commercially viable. Some of these challenges include high feedstock cost, low butanol titer, low butanol productivity and strain instability [4, 7]. Therefore, engineering efforts have been made to construct non-native industry-friendly host to produce n-butanol. Here, butanol producing pathway from Clostridium sp. has been engineered in laboratory host for heterologous butanol production [8–11]. Further enhancement in butanol yield was made by replacing the pathway intermediate enzyme from the non-Clostridium host .
Research recently has been focused on separating alcohol or hydrocarbon production into two distinct biological events - fatty acids production in the first biological event and conversion of the fatty acids into various biofuel molecules in the second biological event. E. coli and Clostridium species have been used as the common host to fulfill these two functions. Free fatty acid production in engineered E. coli has been reported up to 0.3-0.4 g/g glucose [13–15], while native Clostridium was shown to produce 0.45-0.54 g short chain fatty acid per gram of sugar [16, 17]. Further, the long chain fatty acids were converted into alcohols and alka(e)nes by the engineered E. coli[18, 19] and short chain fatty acids were converted into alcohols using Clostridium sp. [20–22]. While pathway for independent biological conversion of long chain fatty acids to alcohol or alkane is well characterized and has been successfully used in the heterologous system, the pathway responsible for conversion of short chain fatty acids of C3-C7 length into either alcohol or alkane has been poorly characterized and has not been used in the heterologous system for such purpose. Moreover, native Clostridium host used for converting butyric acid to butanol needs to be constantly activated and regenerated through heat-shock and re-inoculation , thereby demanding development of more robust, industry friendly platform for this purpose.
Here, we report characterization of C. acetobutylicum pathway for conversion of short chain fatty acids into corresponding alcohols and successful engineering of the E. coli strain for performing this function. We further show that the yield of conversion is strain specific and internal E. coli enzymes do not play a significant role in this process. Most importantly, the process has been validated at the bioreactor level under controlled environment and the engineered E. coli cells have been used for continuous production of butanol.
Results and discussion
Construction of E. colistrain for conversion of butyric acid to butanol
Conversion of butyric acid to butanol by the engineered E. coli (pQE-adhE2/ptb/buk) strain was tested with relevant controls. Neither pQE30 nor pQE-ptb/buk bearing cells could utilize butyric acid to produce butanol, suggesting all the three clostridial enzymes were needed to convert butyric acid to butanol (Figure 2C). The E. coli (pQE-adhE2/ptb/buk) strain produced 1.7 mM butanol from 2.3 mM butyric acid after 120 h of incubation under anaerobic condition. Interestingly, we observed that butyrate concentration in the E. coli (pQE – ptb/buk) strain increased when grown for 48 and 120 hours, leading to negative values for butyric acid consumption in Figure 2C. This could be because both Ptb and Buk enzymes were reversible in nature and might be diverting some of the internal butyryl CoA pool of E. coli into butyrate.
Butyric acid tolerance and substrate preference of engineered E. coli
Since glycerol to butyric acid ratio of 1.5:1 worked best for butanol production, we analyzed the effect of increased biocatalyst on butanol production when higher amount of substrates in the same ratio was used. The experiments were performed using biomass with optical density at 600 nm of 10. With this cell density, we first tested impact of growing cells under aerobic vs anaerobic condition before resuspending the culture at OD600 of 10 and shifting to anaerobic condition for conversion of butyric acid to butanol. Aerobic cultivation will help achieving the higher cell density faster and therefore will save significant time. However, the results indicated that butanol production was three fold lower when cells were grown under aerobic condition as compared to those grown under anaerobic condition (Figure 4C). We further tested higher concentration of butyric acid, ranging from 50 mM to 110 mM, in the culture media by growing cells under anaerobic condition. Maximum butanol concentration of ~60 mM was obtained when butyric acid concentration in the medium was 90 mM (Figure 4C).
Conversion of other short chain fatty acids to alcohols
Strain specificity for production of butanol
E. coli MG1655 strain transformed with butyric acid to butanol pathway produced three products besides butanol, i.e., succinic acid, acetic acid and ethanol, when glycerol and butyric acid were used as substrate. Among these, succinic acid and ethanol were sink for NADH since production of each of these molecules from glycolytic intermediates would need 2 molecules of NADH (Additional file 1: Figure S1). Thus, these two molecules were the major competing products for butanol in terms of NADH requirement. We therefore tested deletion mutants for internal alcohol dehydrogenase (adhE) and fumarate reductase (frdA) in order to prevent formation of ethanol and succinate, respectively. However, these deletions did not lead to enhancement of butanol production (data not shown).
Role of internal acyl-CoA synthetase in the conversion of butyric acid to butanol
E. coli has an internal enzyme, acyl coenzyme A synthetase, encoded by fadD gene that facilitates long chain fatty acids uptake and esterification into CoA thioesters prior to its degradation via β-oxidation or incorporation into phospholipids. This enzyme converts free fatty acids into corresponding acyl-CoA with concomitant hydrolysis of ATP into AMP. We wanted to investigate whether FadD had any role to play in the uptake and conversion of butyric acid to butyryl-CoA. When E. coli MG1655 was transformed with only alcohol dehydrogenase (AdhE2) from C. acetobutylicum, negligible amount of butyric acid was consumed and no butanol was detected in the medium (Figure 6B), suggesting no indigenous enzyme was helping uptake of butyric acid and its assimilation into butyryl-CoA that could be further channeled through AdhE2 to butanol. Moreover, transformation of pQE-adhE2/ptb/buk plasmid, which contained pathway for conversion of butyric acid to butanol from C. acetobutylicum, into fadD deleted strain resulted in similar butyric acid uptake and butanol production as that of wild type strain, indicating that FadD had no role to play in converting butyric acid to butanol.
Butanol production by the engineered E. coliin the bioreactor
We further tested continuous production of butanol by cell recycling through hollow-fiber cassette. The feed containing butyric acid and glycerol was started continuously at the rate of 15 mmol/l/h and 22.5 mmol/l/h, respectively, with the dilution rate of 0.2 h-1 after 24 hr of fermentation with OD600 of 10. The butanol concentration was observed in the permeate intermittently until 240 hrs. An average butanol titer of 37 mM and productivity of 7.6 mmol/l/h was observed in the permeate during the continuous cultivation (Figure 7C). There was a corresponding consumption of butyric acid at the similar rate. Though the butanol production rate was considerably lower than what is expected at the commercial scale, further process development is likely to help in improving the production rate.
We have shown the efficiency of clostridial pathway in E. coli for conversion of short chain fatty acids of chain length C3 – C7 to their corresponding alcohols. We also demonstrated that indigenous enzymes of E. coli did not play any significant role in this process. The observation that the conversion could be done in continuous mode using engineered cells as the biocatalysts justifies this process to be further optimized and assessed for commercial application.
Bacterial strains, plasmids and culture conditions
Strains, plasmids and primers used in this study
Reference or source
E. coli MG1655
F- LAM- rph-1
E. coli B
E. coli DH5α
F- Φ80lacZΔM15 Δ(lacZYA-argF) U169 recA1 endA1 hsdR17 (rK–, mK+) phoA supE44 λ– thi-1 gyrA96 relA1
E. coli M15
F- thi lac mtl, pREP4 plasmid
E. coli BW25113
rrnB DElacZ4787 HsdR514 DE(araBAD)567 DE(rhaBAD)568 rph-1
E. coli ΔfadD
BW25113, ΔfadD :: FRT-kan-FRT
E. coli ΔadhE
BW25113, Δadhe ::FRT-kan-FRT
E. coli ΔfrdA
BW25113, ΔfrdA :: FRT-kan-FRT
bla, cloning vector
pQE30 with adhe2 gene from C. acetobutylicum cloned between BamHI and SalI sites
pQE30 with ptb-buk operon from C. acetobutylicum cloned between SalI and PstI sites
pQE-adhE2 with ptb-buk operon from C. acetobutylicum cloned between SalI and PstI sites
Transformed E. coli strains were streaked on LB agar plates containing 100 μg/ml ampicillin and/or 30 μg/ml kanamycin and grown overnight at 37°C. Isolated colonies were used to prepare primary inoculum by inoculating in 5 ml LB medium containing antibiotics and growing overnight aerobically. The overnight culture was used to prepare secondary inoculum by inoculating in 20 ml TB medium containing 50 mM glucose or glycerol and incubating overnight at 37°C under anaerobic conditions. The grown secondary inoculum was harvested, resuspended in 20 ml of TB medium to achieve an OD600 of 1.0 and transferred in a 100 ml rubber stoppered anaerobic bottle purged with argon gas. The TB medium also contained butyric acid and 0.1 mM IPTG in addition to the appropriate carbon source. The bottle was purged with argon and the culture was grown at 37°C in an orbital shaker. Samples were withdrawn from the bottles at appropriate time points for cell density and metabolite analysis.
The strains were also grown under controlled conditions in a bioreactor. A primary culture was prepared by inoculating an isolated colony in LB and growing the cells overnight at 37°C. The grown culture was used to inoculate 350 ml TB medium in 1 L conical flask containing either glucose or glycerol and incubated for 24 hours in an anaerobic chamber maintained at 37°C. An appropriate volume of this culture was harvested and inoculated in the bioreactor vessel (Multi-vessel BioStat Q Plus fermentor, Sartorius) containing 350 ml of TB medium along with glycerol and butyric acid so as to achieve an initial OD600 of 1 or 10. IPTG was not added in the bioreactor as it was shown at the small scale that addition of IPTG had no impact on conversion of butyric acid into butanol (data not shown), perhaps due to sufficient basal level expression of the pathway enzymes. The bioreactor was maintained at 37°C with a stirrer speed of 300 rpm, pH of 7 and purging of highly pure grade argon at a rate of 0.01 L/min to maintain the anaerobic environment.
Continuous production of butanol was achieved by cell recycling using a Hollow Fiber Cartridge (surface area 420 cm2, 500,000 NMWC) from GE Healthcare. The cultivation was carried out in a bioreactor with 350 ml working volume under the operating conditions mentioned above with an initial cell density at OD600 of 10. Solution containing 50 mM butyric acid, 75 mM glycerol, 72 mM K2HPO4 and 17 mM KH2PO4 were added to the fermentor vessel through the peristaltic pump at the dilution rate of 0.2 h-1 to achieve feeding of 15 mmol/l/h of butyric acid and 22.5 mmol/l/h of glycerol. Medium along with cells was pumped through the hollow fiber cassette. The cells were recycled back to the bioreactor while permeate from hollow fiber cassette containing butanol was recovered and used for analysis of butanol formation.
Cloning of C. acetobutylicum genes in E. coli
Total genomic DNA was isolated from C. acetobutylicum ATCC 824 as per standard procedure . The adhE2 gene of C. acetobutylicum was PCR amplified using P1 and P2 primers, digested with BamHI and SalI restriction enzymes and ligated to the corresponding restriction sites of pQE30 plasmid to obtain pQE-adhE2. The P2 primer also contained codons for 6-histidine tag to monitor the expression at the protein level. The ptb – buk operon of C. acetobutylicum ATCC 824 encoding phosphotransbutyrylase and butyric acid kinase genes was amplified from the genomic DNA using the P3 and P4 primers. The PCR product was digested with SalI and PstI restriction enzymes and ligated to the corresponding restriction sites of pQE30 plasmid to obtain pQE-ptb/buk. P3 primer contained ribosomal biding site for translation initiation and P4 primer contained codons for 6-histidine tag to monitor the expression of operon at the protein level. The adhE2 gene was further cloned at the BamHI and SalI restriction sites of pQE-ptb/buk plasmid to obtain the final construct pQE-adhE2/ptb/buk.
The expression of the cloned genes was confirmed by SDS – PAGE and Western Blotting. Briefly, the cultures were induced and the crude cell lysates obtained were separated on a 12% polyacrylamide gel. The proteins were transferred to a nitrocellulose membrane (0.2 um, BioTraceNT, Pall Corporation), probed with anti – penta-his antibody (H1029, Sigma) followed by HRP-conjugated anti-mouse IgG antibody (A4416, Sigma). Color development of the blot was performed using DAB (diaminobenzidine) and hydrogen peroxide.
For extracellular metabolite analysis, cells were centrifuged at 13000 rpm for 10 min and the supernatant was filtered through 0.22 μm membrane. The extracellular metabolites were analyzed on a 1260 Infinity Series HPLC system (Agilent) equipped with an Aminex HPX-87H anion exchange column (Bio-Rad). Filtered and degassed 4 mM H2SO4 was used as the mobile phase at a flow rate 0.3 ml/min. The column was maintained at a temperature of 40°C in a thermostat chamber. Butanol was analyzed on a 7890A gas chromatography system (Agilent) with a flame ionization detector equipped with a 7694E headspace analyzer using a HP-5 column (30 m length, 0.32 mm id, 0.25 um film thickness). The oven program was set as follows (40°C for 4 minutes, 80°C for 4 minutes at 10°C/min, 120°C for 2 min at 20°C/min, 200°C for 2 min at 20°C/min). The inlet and detector were maintained at 150°C and 280°C, respectively. Metabolite concentrations were calculated from the area of the curve obtained for 1 g/l of the standards (Absolute Standard). All results were presented as average and standard deviation of the data from two independent experiments.
Phosphotransbutyrylase (Ptb) activity was measured by estimating the liberation of coenzyme A on the addition of butyryl CoA to the reaction mixture. The free coenzyme A formed was then allowed to form a coloured complex with 5,5′ – dithio-(2-nitrobenzoic acid) (DTNB) which could then be estimated by measuring the absorbance at 412 nm . The reaction mixture contained 100 mM potassium phosphate buffer (pH 7.4), 0.02 mM butyryl CoA, 0.08 mM DTNB and crude cell extract. The extinction coefficient of the DTNB – CoA – SH complex was taken as 13.6 mM-1 cm-1. Aldehyde/alcohol dehydrogenase (AdhE2) activity was measured in the reverse direction by estimating the amount of free NADH liberated during the reaction . Briefly the reaction mixture contained 19 mM sodium pyrophosphate buffer (pH 8.8), 2.37% v/v ethanol or butanol, 5 mM β – NAD and crude cell extract in a total volume of 2 ml. The absorbance at 340 nm was monitored to estimate the amount of free NADH produced. The extinction coefficient of NADH at 340 nm was taken as 6.22 mM-1 cm-1. The activity of butyrate kinase (Buk) was estimated by monitoring the formation of the coloured ferric hydroxamate complex with butyryl phosphate in the presence of excess of hydroxylamine . The reaction mixture contained 770 mM potassium butyrate (pH 7.5), 48 mM Tris – Cl, 10 mM MgSO4, 700 mM KOH, 10 mM ATP and crude cell extract. The reaction was initiated by the addition of ATP and the mixture was incubated at 37°C for 5 minutes. 1 ml of 10% trichloroacetic acid was used to stop the reaction and the end product was estimated by the addition of 4 ml of FeCl3 (1.25% in 1 N HCl). The extinction coefficient of the hydroxamate complex at 540 nm was taken as 0.691 mM-1 cm-1. The enzyme units were represented as nmol/min/mg.
We thank Dr Alok Kumar Malaviya for the help in setting-up the hollow fiber based cell recycling system. We acknowledge financial support from Department of Biotechnology (DBT), Govt of India. AJM was supported by a fellowship from Council of Scientific and Industrial Research.
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