The dependence on finite petroleum and natural gas resources as well as their potential environmental impact has generated interest in exploring renewable sources for replacements. This has more notably been applied to the areas of transportation fuels. However, less attention has been paid to the chemical feedstock industry. Currently, 99% of chemicals and their derivatives come from petroleum and natural gas [1]. In 2004, the petrochemical industry consumed 4 quadrillion BTUs (British thermal units) of petroleum and natural gas for feedstock use to produce thousands of chemicals [1]. These chemicals are essential to the synthesis of plastics, rubbers, and pharmaceutical compounds that play a major role in our standard of living.

Synthetic biology has made large progress constructing pathways for the production of various biofuels [25]. Recently, these efforts have expanded to address the need for replacement of our current petrochemical feedstocks with renewable sources [613]. Much like in the production of advanced biofuels, synthetic biology offers a potential platform for the production of non-natural chemical feedstocks from simple sugars. This work aims to demonstrate the feasibility of producing chemical feedstocks from microorganisms by engineering Escherichia coli to produce isobutyraldehyde.

Isobutyraldehyde is used as both a fragrance and flavor additive. It is also used to produce plasticizers, isobutyric acid, and isobutanol, which is a precursor to the rubber polyisobutylene. Isobutyraldehyde is currently synthesized from petroleum derived propylene, carbon monoxide, and hydrogen [14]. In terms of microbial production and purification, its high volatility (172 mm Hg at 25°C) may enable less costly purification and facilitate in situ product removal for long-term fermentation.

Atsumi et al. have previously shown that 2-ketoisovalerate generated from L-valine biosynthesis can serve as precursors for the Ehrlich degradation pathway [15] to isobutanol (Figure 1) [5]. In this pathway, 2-ketoisovalerate is converted to isobutyraldehyde using a keto acid decarboxylase (KDC) and then reduced to isobutanol with an isobutyraldehyde reductase (IBR). In 2010, Atsumi et al. evaluated the native aldehyde reductase YqhD for its ability to convert isobutyraldehyde to isobutanol in E. coli[16]. It was discovered that a strain lacking overexpression of IBR was still able to produce the same amount of isobutanol as a strain overexpressing ADH2 (Saccharomyces cerevisiae). It was determined that YqhD in E. coli was responsible for most of IBR activity in isobutanol production. However, even with deletion of yqhD on the E. coli chromosome, the engineered strain was still able to produce isobutanol. It indicates that E. coli has one or several additional IBRs. Thus, here, we systematically removed possible IBR s from the E. coli chromosome to increase isobutyraldehyde production and reduce isobutanol formation.

Figure 1
figure 1

Schematic representation of Isobutyraldehyde production in E. coli . After glycolysis, two molecules of pyruvate are condensed into 2-acetolactate by acetolactate synthase (AlsS; B. subtilis), which is then converted into 2-ketoisovalerate (KIV) by acetohydroxy acid isomeroreductase and dihydroxy acid dehydratase (IlvC and ilvD; E. coli). Then, KIV is decarboxylated to form isobutyraldehyde by keto acid decarboxylase (Kivd; L. lactis). The target product, isobutyraldehyde, can be converted to the side product isobutanol by various aldehyde reductases (ALR) in E. coli.

Results and discussion

As a starting point, E. coli strain JCL260 was used to assess initial isobutyraldehyde production. This strain was previously optimized for isobutanol production [5, 17], by deleting adhE, ldhA, fnr, frdAB, pta, and pflB. The isobutyraldehyde pathway was constructed by using the previously described genes alsS, ilvC, ilvD, and kivd[5, 18].

To assess the initial production, pGR03 (alsS ilvC, and ilvD) and pSA129 (kivd) were introduced into JCL260. This strain produced only 0.14 g/L/OD600 isobutyraldehyde, and as high as 1.45 g/L/OD600 isobutanol after 24 hours. This roughly 1:10 ratio is likely the result of one or several IBR s including yqhD on the E. coli genome [16]. As a result, we first deleted yqhD. This strain produced ~0.7 g/L/OD600 of isobutyraldehyde and ~0.4 g/L/OD600 isobutanol in our condition. This result indicates one or more additional IBR s exist on the E. coli genome.

IBR activity can be catalyzed by the alcohol dehydrogenase (ADH)/aldehyde reductase class of enzyme. Thus, in order to decrease isobutanol production, we searched the E. coli genome sequence using the EcoCyc comprehensive database [19] for other ADH-like enzymes. We identified seven candidate IBR s (adhP, eutG, yiaY, yjgB, betA, fucO, and eutE). Due to either the characterized ADH functions or the conserved ADH-like domain sequences of the above-mentioned genes, we hypothesized that these had the highest probability of having IBR activity. Additionally, no other ADH type enzymes were found. AdhP is a well-characterized NADH-dependent ethanol dehydrogenase [20]. EutG is an NADH-dependent alcohol dehydrogenase involved in ethanolamine utilization, and is suspected to be an ethanol dehydrogenase [2123]. The enzymes EutG, YiaY, BetA, and EutE were previously utilized or removed to produce C4-C10 alcohols [24]. FucO has also been well characterized as a L-lactaldehyde and 1,2-propanediol oxidoreductase [25]. YjgB is a putative Zn-dependent aldehyde reductase [26]. With seven candidate genes identified, we set out to efficiently identify which (if any) of these enzymes were active toward isobutyraldehyde in order to improve isobutyraldehyde production and reduce isobutanol formation.

Single gene deletions to improve isobutyraldehyde production

As a first step, each candidate IBR gene was individually deleted on the ΔyqhD strain (SA542 (Table 1)). Then, we measured production by introducing pGR03 (alsS, ilvC, and ilvD) and pSA129 (kivd) into each strain (Figure 2A). Production was carried out in sealed screw-cap culture tubes to prevent evaporation of isobutyraldehyde. None of the individual genes stood out as largely responsible for the observed isobutanol production (Figure 2A). However, two strains (ΔyiaY and ΔyjgB) showed slight improvements in isobutyraldehyde (up to 1 g/L/OD600) over the ΔyqhD strain (0.7 g/L/OD600), while two (ΔbetA and ΔeutE) showed decreases to below 0.4 g/L/OD600. We considered that multiple enzymes could be involved in IBR activity, resulting in minor or no observable changes in production. In order to test this hypothesis, we set out to combine the deletions and assess production with each additional deletion. If several enzymes were responsible, then total elimination of these genes would result in higher isobutyraldehyde production, and little or no isobutanol formation.

Table 1 Strain and plasmids used in this work
Figure 2
figure 2

Effects of individual and combined deletions of aldehyde reductases. Cells were grown at 37°C for 24 h. ”Δ” indicates gene deletion. All strains contained pGR03 (alsS, ilvC, and ilvD) and pSA129 (kivd). Titers represented as concentration per OD600 to adjust for variations in growth. Error bars represent the standard deviation of triplicate experiments.

Combining gene deletions to improve isobutyraldehyde production

Next we sequentially combined all candidate IBR deletions. With each additional deletion we measured production of isobutyraldehyde and isobutanol (Figure 2B). The isobutyraldehyde production from the strain including ΔadhP ΔeutG and ΔyiaY was similar with that from the parent strain (ΔyqhD). However, with ΔyjgB added to the strain including ΔyqhD ΔadhP ΔeutG and ΔyiaY we observe a significant drop in isobutanol production to 0.19 g/L/OD600 and a significant increase in isobutyraldehyde production of 1.35 g/L/OD600. Subsequent deletions of ΔbetA, ΔfucO, and ΔeutE on the strain including ΔyqhD ΔadhP ΔeutG ΔyiaY and ΔyjgB showed no additional reduction in isobutanol formation. Most strains showed similar growth after 24 hours to OD600 ~3, except for the last two deletions (ΔfucO and ΔeutE) which showed a marked decrease in 24 hour growth (OD600 ~ 1.7-2) (Figure 2B). The marked change in aldehyde ratio from 1:10 (JCL260) to as much as 7:1 (AL329(ΔyqhD ΔadhP ΔeutG ΔyiaY ΔyjgB)) represents a roughly ~10 fold increase in isobutyraldehyde production and ~7.5 fold decrease in isobutanol production (Figure 2B).

These results indicate that the remaining isobutanol production after deletion of yqhD was the result of multiple enzymes that have IBR activity. Additionally, despite deleting our entire list of IBR candidates in E. coli, there remains a small amount of isobutanol production. This suggests yet other enzymes are present that have IBR activity. Since no additional gene candidates were obvious in the E. coli genome and additional deletions became more difficult due to too many FLP recognition target sites [29], we did not search for further IBR candidates.

Overexpression of candidate IBR s to confirm IBR activities

In order to determine conclusively which of the candidate IBRs were active toward isobutyraldehyde, we took the low isobutanol producing strain AL626 (ΔyqhD ΔadhP ΔeutG ΔyiaY ΔyjgB ΔbetA ΔfucO) and overexpressed each candidate IBR in addition to the isobutyraldehyde pathway. In this way, if the candidate IBRs are active, overexpression of these would reverse the ratio of isobutyraldehyde to isobutanol to levels similar to that of the parent strain (JCL260). The candidate IBR s were individually cloned onto pSA138, downstream of kivd, by replacing yqhD using SLIC (see Methods). The new plasmids along with pGR03 were then introduced into AL626. Production from the strains overexpressing adhP eutG yjgB, or fucO led to a reversal of production, while the other enzymes did not, indicating that these have IBR activity (Figure 3a). To verify proper expression of each enzyme from plasmid, cell extracts were ran on SDS-PAGE. All protein expressions were confirmed. The strain overexpressing adhP or eutG produced ~3 g/L/OD600, more than the strain overexpressing yqhD (1.7 g/L/OD600). This is likely because AdhP and EutG are NADH dependent [20, 21, 23], whereas YqhD is NADPH dependent [30]. The strain overexpressing fucO also produced slightly more than the strain overexpressing yqhD (2 g/L/OD600 vs 1.7 g/L/OD600), and is also NADH-dependent [25]. Since glycolysis produces two NADHs per one glucose, availability of NADH is generally higher in E. coli than NADPH. The strain overexpressing yjgB produced similar amounts of isobutanol as the strain overexpressing yqhD, verifying its putative annotation of aldehyde reductase/alcohol dehydrogenase [26] to be correct. The reason that deletion of yqhD has a greater affect than the other genes is likely due to higher expression levels from the genome. A comparison of mRNA levels from a transcriptome study show that mRNA levels of yqhD are between 2 and 10 fold higher than the other candidate genes, except for betA[31]. It is also known that the expression of yqhD is upregulated in the presence of aldehyde [32].

Figure 3
figure 3

Overexpression of each candidate IBR in AL626. (A) Each candidate gene was cloned onto individual plasmids downstream of kivd (pAL213-pAL223) and introduced into AL626 (JCL260ΔyqhD ΔadhP ΔeutG ΔyiaY ΔyjgB ΔbetA ΔfucO) along with pGR03 (alsS, ilvC, and ilvD). Cells were grown at 37°C for 24 h. Titers represented as concentration per OD600 to adjust for variations in growth. (B) Each gene was cloned onto individual plasmids and introduced into AL626. Cell extracts were assayed with acetaldehyde and isobutyraldehyde as substrates as well as with both cofactors (NADH & NADPH). Enzyme activity is defined as μmol NAD(P)H consumed per minute per mg of protein. NAD(P)H consumption measured at 340 nm. Error values represent the standard deviation of triplicate experiments. NA: not assayed. ND: not detectable.

To further explore the activity of each IBR, enzyme assays were performed with each IBR candidate. We took the low isobutanol producing strain AL626 (ΔyqhD ΔadhP ΔeutG ΔyiaY ΔyjgB ΔbetA ΔfucO) and overexpressed each candidate IBR. The candidate IBR s were individually cloned onto pZE12-luc, by replacing luc using SLIC (see Methods). The new plasmids and pZE12-luc (negative control) were then introduced into AL626. We assessed the activity of each enzyme with acetaldehyde (AA) and isobutyraldehyde (IBA) as substrates as well as with both cofactors, NADH and NADPH (Figure 3b). We confirmed aldehyde reductase activity of AdhP, EutG, YjgB, and FucO with both AA and IBA as substrates. The active enzymes showed similar preference for AA and IBA when assayed with their preferred cofactor. AdhP was able to utilize both NADH and NADPH, but IBR activity was 2-fold higher with NADH. FucO showed about 50% the activity of AdhP, consistent with production levels from Figure 3a. FucO showed clear preference for NADH, having ~6-fold higher activity with NADH than with NADPH for both aldehydes. The activity of EutG which is a Fe-containing ADH, as its sequence suggests [23], was not as high as compared to AdhP with AA (0.56 μmol NADH min-1 mg-1) and IBA (0.44 μmol NADH min-1 mg-1), but these activities were still 6 to 10-fold greater compared to the negative control. YjgB preferred NADPH and showed the highest activity of all the enzymes with both AA (7.07 μmol NADPH min-1 mg-1) and IBA (6.47 μmol NADPH min-1 mg-1). YiaY, BetA, and EutE showed very weak or no aldehyde reductase activity with both AA and IBA. The absence of activity from YiaY and BetA with AA and IBA is notable since they were previously used to produce > C5 alcohols [24].

Long-term production with in situ product removal

With a couple of high isobutyraldehyde producing strains, we explored the feasibility of long-term production of isobutyraldehyde. From toxicity experiments (Figure 4), we observe no growth at 10 g/L and significant growth inhibition with 1 g/L. Thus, we expect that toxicity of isobutyraldehyde accumulation could significantly hinder long-term production. In order to prevent inhibitory levels of aldehyde from accumulating, we applied a gas-stripping system to remove product in situ (Figure 5) [33]. Removal of product from a culture solution may also create a driving force for further product formation [34]. Furthermore, the redox balance of this pathway also necessitates sufficient supply of oxygen to the culture. Elimination of isobutanol formation negatively impacts the redox balance of the pathway under anaerobic conditions. Isobutanol formation results in a balanced redox state (Figure 1). As a result, isobutanol can be produced under anaerobic conditions. The isobutyraldehyde pathway, however, yields an excess of 1 NADH per glucose. This excess necessitates aerobic conditions in order to recycle the NAD+ pool through oxidative phosphorylation. Thus, using a gas-stripping system provides the cells with ample oxygen while simultaneously removing isobutyraldehyde from the culture.

Figure 4
figure 4

Comparison of growth with isobutyraldehyde stress. Time courses for the growth of E. coli strain AL626 (JCL260 ΔyqhD ΔadhP ΔeutG ΔyiaY ΔyjgB ΔbetA ΔfucO) in the presence of 0 (black), 0.1 (orange), 1 (blue), and 10 g/L (red) isobutyraldehyde in 15 ml screw-cap tubes. Optical density (OD) measurements taken every hour for 4 hours at 600 nm. Error bars represent the standard deviation of triplicate experiments.

Figure 5
figure 5

Schematic of gas stripping system. Sterile air is pumped (3 cc/min) into a flask containing 100 mL sterile water to saturate the air and thereby prevent evaporation of water in the culture flask. Vaporized product (isobutyraldehyde) is then carried into a series of traps and condensers held at 1 -4 °C where it is captured for quantification. Removal of product during production greatly reduces accumulation which is often toxic to the cells.

In this set up, air flows through the culture flask, where vaporized isobutyraldehyde is captured in a series of cold (~4°C) condensers and ‘trap’ bottles. The high volatility of isobutyraldehyde (172 mmHg at 25°C) facilitates this process [14]. Since isobutyraldehyde is known to catalytically react with oxygen in the air between 30–50°C and convert to isobutyric acid [35], we conducted production at 30°C to minimize this. Furthermore, production of isobutanol at 30°C has been performed with greater success than at 37°C [34].

Based on the results from Figure 3, we used AL626 for long-term production experiments (Figure 6). Production was carried out in a 250 mL baffled shake-flask under constant stirring. Cultures were initially grown at 37°C for faster growth and induced at OD600 ~0.4. Upon induction, the temperature of the culture bath was quickly brought down to 30°C. We optimized the airflow rate (3 cc/min) of the system such that the majority of isobutyraldehyde was collected in the first trap bottle and with minimal amounts remaining in the culture flask. Every 24 hours, 10% of the culture was removed for growth, pH, and product analysis and replaced with fresh media containing ~370 g/L glucose. Trap bottles were also analyzed and replaced every 24 hours with new trap bottles.

Figure 6
figure 6

Long-term production of isobutyraldehyde with a gas stripping system. (A) Total accumulated production of isobutyraldehyde (green) and isobutanol (blue). (B) Daily productivity of isobutyraldehyde (green) and isobutanol (blue). (C) Time profiles of cell growth. (D) Concentrations of isobutyraldehyde (green) and isobutanol (blue) in the production culture to determine effectiveness of product removal by the system. (E) Daily glucose consumption of the culture. (F) Time profile of pH of the production culture. pGR03 (alsS, ilvC, and ilvD) and pSA129 (kivd) were introduced to AL626. Cells were inoculated 1% (vol/vol) from the overnight culture and grown in 100 mL production media (M9 media containing 5 g/L yeast extract and 50 g/L glucose). Every 24 hours, 10% of culture was removed for analysis, and replaced with production media containing 370 g/L glucose (dilutes to 37 g/L/d). Error bars represent the standard deviation of triplicate experiments.

In the first 24 and 48 hours of production, the strain averaged 8 g/L/day of isobutyraldehyde (Figure 6B) with low isobutanol formation (0.7-1.3 g/L/day). As production continued from 72 to 120 hours, we observed a consistent decline of isobutyraldehyde productivity from 8 g/L/day to an eventual 5 g/L/day. This notably corresponded with a similar decline in glucose consumption from ~37 g/L/day at 48 hours, down to 32 g/L/day at 120 hours (Figure 6F). Surprisingly, we observed a marked increase in daily isobutanol formation beginning at 72 hours. After 120 hours, production of isobutanol began to overtake that of isobutyraldehyde in some trials, suggesting an up regulation of one or more unknown IBRs. For this reason, we stopped production after 120 hours. The culture grew to OD600 6.2 after the first day and increased slowly thereafter up to OD600 9 after 120 hours (Figure 6C). This suggests the culture received sufficient oxygen to achieve redox balance throughout the production. The pH of the culture (Figure 6F) remained fairly stable throughout production, decreasing only by 1 unit to a pH of about 6 after 120 hours. In the future, maintaining pH at 7 by addition of base or by using a buffer may improve yield and culture stability with this system.

Overall, isobutyraldehyde levels in the culture flask remained low, typically between 0.5 g/L and 1.5 g/L (Figure 6D). The stable growth and relatively low product accumulation (Figure 6D), indicates the gas-stripping system was successful in reducing the potential toxicity of isobutyraldehyde. Development of an isobutyraldehyde tolerant strain may improve cell growth and culture stability during production, possibly circumventing the need for gas-stripping. Strains tolerant of isobutanol have previously been developed for similar reasons [36]. However, an increase in isobutanol tolerance did not correlate with improved production [34]. Our strain’s productivity of 8 g/L/day is roughly 8-fold greater than toxic levels of isobutyraldehyde (~1 g/L). Achieving a strain that can tolerate these titers may be difficult to develop. Additionally, utilizing gas-stripping has the added advantage of purifying isobutyraldehyde during production, which may be a cost saving method under industrial scale production.

Isobutyraldehyde production from this strain totaled 35 g/L after 120 hours (Figure 6A). Including formation of isobutanol (~10 g/L), total production reached ~45 g/L. The theoretical molar yield of isobutyraldehyde from glucose is 1:1. This results in a gram per gram yield of 0.40 g isobutyraldehyde/g glucose. In the first 48 hours of production, we achieved a yield of 47% of the theoretical maximum. The yield remained relatively constant throughout the experiment with a final yield of 45% of the theoretical maximum after 120 hours.

The reason for the large increase in isobutanol formation is not entirely obvious. Growth, pH, and overall yield remained stable throughout the experiment, but glucose consumption and isobutyraldehyde production slowly decreased. Despite the discovery and removal of five IBR s from the genome, still further significant IBR activity exists in our E. coli strain. One possibility is that expression of the unknown enzyme(s) is low early on in production and later upregulated. Cells that are able to increase expression of such enzyme(s) will likely experience lower toxicity and may begin to outgrow other cells within the culture. Thus, further exploration and elimination of this IBR activity will be needed to achieve more stable isobutyraldehyde production after 72 hours.


In this work, we demonstrated the renewable production of isobutyraldehyde, an important chemical feedstock, from E. coli. We identified AdhP, EutG, YjgB, and FucO as isobutyraldehyde reductases, while YiaY, BetA, and EutE were not active toward isobutyraldehyde. With in situ product removal, we achieved a total isobutyraldehyde production of 35 g/L after 5 days. This industrially relevant titer represents a yield of 45% of the theoretical maximum. However, after the second day, isobutanol formation began to increase markedly, suggesting upregulation of yet additional IBR(s) in E. coli.

The lingering presence of isobutanol indicates that additional IBRs still exist in E. coli which we have yet to identify. In this work, we evaluated genes more specifically annotated or characterized as alcohol dehydrogenases. It is possible that other non-specific oxidoreductases are contributing to IBR activity in the cell. E. coli contains more than a dozen other putative, less specifically annotated, NAD(P)H dependent oxidoreductases. Going forward, applying transcriptome analysis, bioinformatics, and other methods may uncover the remaining IBR(s). Further exploration and elimination of these reductases will be required to improve the long-term production stability of this strain.



Rapid Ligation Kit was purchased from Roche. All other enzymes were purchased from New England Biolabs (Ipswich, MA). All synthetic oligonucleotides were ordered from Integrated DNA Technologies (Coralville, IA). DNA sequencing services were done by Davis Sequencing (Davis, CA). Zymo DNA Clean and Concentrator kit and Gel Recovery kit (Zymo Research, Irvine, CA) were used to purify all PCR products. Isobutanol and Isobutyraldehyde were purchased from Sigma Aldrich (St. Louis, MO). 1-pentanol was purchased from Acros Organics (Belgium).


Overnight cultures were grown in 5 mL Luria Broth (LB) containing appropriate antibiotics. Antibiotic concentrations were as follows: Kanamycin (50 μg/mL), Chloramphenicol (40 μg/mL), Ampicillin 100 (μg/mL), Tetracycline (20 μg/mL). Production was carried out with M9 medium containing 5 g/L yeast extract, ~50 g/L glucose, and 1000-fold dilution of A5 trace metal mix (2.86 g H3BO3, 1.81 g MnCl2⋅4H2O, 0.222 g ZnSO4 ⋅7H2O, 0.39 g Na2MoO4⋅2H2O, 0.079 g CuSO4⋅5H2O, 49.4 mg Co(NO3)2⋅6H2O per liter water).

Gene deletions

All gene deletions were carried out by P1 transduction [37] with the aid of strains from the Keio collection [29], except for eutE. To delete eutE, the method developed by Datsenko and Wanner [27] was used due to its proximity to eutG. The deleted fragments were verified by PCR and sequencing. All strains used in this study are listed in Table 1.

Plasmid construction, cloning, and transformations

To construct pGR03, first pSA69 [5] was digested with AatII and SacI, and treated with Antarctic phosphatase. Then the chloramphenicol resistance gene was taken from pZA31-luc [28] by digestion with AatII and SacI. The two fragments were gel purified, ligated, and introduced into E. coli XL-1 blue strain.

All other plasmids (pAL156-158, pAL162, pAL213-215, pAL217-223) were constructed using sequence and ligation-independent cloning (SLIC) [38]. In general, primers for inserts (GR147-154, GR188-193, GR219-GR232) were designed with ~25 bp priming to the target gene and a 20–25 bp ‘linker’ to target vector. All candidate IBR s were amplified by PCR from E. coli JCL16 genome DNA. Plasmids were verified by colony PCR, by digestion with restriction enzymes, and by sequencing. All plasmids and oligonucleotides are listed in Table 1 and Table 2, respectively.

Table 2 Primer sequences

Vector was amplified from pSA138 with GR180 and GR181, and digested with DpnI to reduce background associated from plasmid template. Primers (GR219 and GR221 for adhP, GR221 and GR222 for eutG, GR223 and GR224 for yiaY, GR225 and GR226 for yjgB, GR227 and GR228 for betA, GR229 and GR230 for fucO, and GR231 and GR232 for eutE) were used to amplify each gene from E. coli JCL16 genome DNA and cloned with SLIC onto the pSA138 vector fragment.

Vector was amplified from pZE12-luc with GR145 and GR146, and digested with DpnI to reduce background associated from plasmid template. Primers (GR147 and GR148 for adhP, GR149 and GR150 for eutG, GR151 and GR152 for yiaY, GR153 and GR154 for yjgB, GR188 and GR189 for betA, GR190 and GR191 for fucO, and GR192 and GR193 for eutE) were used to amplify each gene from E. coli JCL16 genome DNA and cloned with SLIC onto the pZE12-luc vector fragment.

Screw-cap tube production

For isobutyraldehyde production test, 1% (vol/vol) of the overnight culture was inoculated in 5 mL production media in 15 mL screw-cap culture tubes and grown at 37°C in a rotary shaker (250 RPM) until OD600 ~0.4, then induced with 1 mM isopropyl-β-D-thio-galactoside (IPTG) and allowed to produce for 24 hours after induction. Screw-cap tubes were tightly sealed to prevent evaporation of isobutyraldehyde.

Aldehyde reductase activity assay

The plasmids pZE12-luc, pAL162, pAL156-158, and pAL213-214 were introduced into AL626. The strains were grown to OD600 value of ~0.4 in 5 mL LB medium at 37°C, followed by adding 1 mM IPTG. Protein overexpression was performed at 37°C for 4 h. Then 1.8 mL of cells were centrifuged at 13,000 RPM for 10 minutes, resuspended in 300 μL BugBuster Protein Extraction Reagent (Novagen, San Diego, CA, USA), and incubated at room temperature for 20 min for cell lysis. The samples were centrifuged for 20 min, 16,000 g, at 4°C. Supernatants were taken for enzyme assays. ADH activities were measured by following the reduction of acetaldehyde or isobutyraldehyde with NADH or NADPH at 340 nm at 37°C using a Synergy H1 Hybrid Plate Reader from BioTek Instruments, Inc. (Winooski, VT). The assay mixture contained 25 mM acetaldehyde or isobutyraldehyde, 50 mM 3-(N-morpholino)propanesulfonic acid (MOPS) buffer (pH 7.0), 0.2 mM Tris-Cl (pH 7.00), 0.2 mM NAD(P)H, and 12.5 mM potassium phosphate buffer (pH 7.5). One unit of activity is defined as the oxidation of 1 μmol of NAD(P)H per minute per mg protein. Protein concentrations were measured using 5x Advanced Protein Assay Reagent (Cytoskeleton Inc., Denver, CO) by diluting 5μL of cell extract in 1 mL of 1x Advanced Protein Assay Reagent and measuring the OD590 of the mixture. Bovine Serum Albumin (BSA) from NEB was used to prepare a standard curve.

Gas stripping apparatus

Rubber stoppers were used to cap the culture flask and water flask. Two holes were made in each rubber stopper where small, customized, metal pipes were inserted. All flasks, traps, and condensers were connected with clear, flexible, chemical resistant, plastic tubing (Tygon tubing). Air flow rate was set to 3 cc/min with a flow regulator. Trap bottles were filled with 600 mL of water. Culture volume and water flask volume were both 100 mL. Culture was initially grown at 37°C until OD600 ~0.4, then 1 mM IPTG was added and the temperature was quickly brought down to 30°C for the remainder of the experiment. When trap bottles were collected for samples, 200 mL water was washed down each condenser to rinse any product into the trap bottles. Final trap volume was determined with a 1000 mL graduated cylinder.

GC analysis

Concentrations of all products, except glucose, were analyzed by Gas Chromatography equipped with a flame ionization detector (FID). The GC system is a Shimadzu GC-2010 with an AOC-20 S auto sampler and AOC-20i Auto Injector. The column used was a DB-Wax capillary column (30 m length, 0.32-mm diameter, 0.50-μm film thickness) from Agilent Technologies. GC oven temperature was initially held at 40°C for 3 minutes, then increased at a rate of 45°C min-1 until 235°C and held for 3 min. Injector temperature was held at 225°C and FID detector was held at 330°C. Injection volume was 0.5 μL, injected at a 15:1 split ratio. Helium was used as the carrier gas. 1-pentanol was used as internal standard.

Glucose quantification and growth measurements

Glucose was measured using a Sucrose, Fructose, and Glucose kit from Megazyme International Unlimited. Glucose assays and Optical densities (OD) were measured at 340 nm and 600 nm, respectively, with a Genesis 10 S UV–vis Spectrophotometer (Thermo Scientific).