<i>Escherichia coli </i>transformant for producing itaconate and uses thereof

Abstract

The present disclosure provides an Escherichia coli transformant and a method for producing itaconate using the Escherichia coli transformant.

Claims

1. An Escherichia coli transformant, comprising at least one plasmid, wherein the at least one plasmid includes a D-xylose dehydrogenase (XDH) gene, a D-xylonolactonase (XL) gene, a 2-keto-3-deoxy-D-xylonate dehydratase (KdxD) gene, and a 2-ketoglutarate semialdehyde dehydrogenase (KGSADH) gene; wherein an isocitrate dehydrogenase (icd) gene of the Escherichia coli transformant is deleted; wherein the at least one plasmid further includes a D-xylonate dehydratase (XD) gene; wherein the XDH gene, the XL gene, the KdxD gene, the KGSADH gene, and the XD gene are obtained from Burkholderia xenovorans strains; wherein the XDH gene, the XL gene, the XD gene, the KdxD gene, and the KGSADH gene are sequentially constructed from their 5 ends to 3 ends in the at least one plasmid; wherein the Escherichia coli transformant is a transformant of Escherichia coli BW25113; wherein the Escherichia coli transformant converts xylose into -ketoglutaric acid through a nonphosphorylative metabolic pathway; wherein a xylose isomerase gene (xylA), a 2-dehydro-3-deoxy-D-pentonate aldolase gene (yjhH), and a 2-keto-3-deoxygluconate aldolase gene (yagE) of the Escherichia coli transformant are deleted; wherein the Escherichia coli transformant produces itaconate without adding a yeast extract or glutamate; and wherein the at least one plasmid is pKL7 and pKL8.

2. The Escherichia coli transformant according to claim 1, further comprising a citrate synthase (gltA), an aconitase B (acn B), and a pyruvate carboxylase (pyc).

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) The following drawings form part of the present specification and are included here to further demonstrate some aspects of the present invention, which can be better understood by reference to one or more of these drawings, in combination with the detailed description of the embodiments presented herein.

(2) FIG. 1 is a schematic diagram showing the pathway to decouple IA production from endogenous -ketoglutaric acid biosynthesis in the Escherichia coli transformant of the present invention, in which -KG represents -ketoglutaric acid; OAA represents oxaloacetate; MAL represents malate; SUC represents succinate; acnB represents aconitase B; cad represents cis-aconitate decarboxylase; pyc represents pyruvate carboxylase; gltA represents citrate synthase; icd represents gene encoding isocitrate dehydrogenase; xylA represents gene encoding xylose isomerase; yjhH represents gene encoding 2-dehydro-3-deoxy-D-pentonate aldolase; yagE represents gene encoding 2-keto-3-deoxygluconate aldolase; XDH represents gene encoding D-xylose dehydrogenase; XL represents gene encoding D-xylonolactonase; XD represents gene encoding D-xylonate dehydratase; KdxD represents gene encoding 2-keto-3-deoxy-D-xylonate dehydratase; KGSADH represents gene encoding 2-ketoglutarate semialdehyde dehydrogenase.

(3) FIG. 2 is a schematic diagram showing the gene combination for constructing a nonphosphorylative pathway using the Escherichia coli transformant of the present invention, in which KGSADH represents gene encoding 2-ketoglutarate semialdehyde dehydrogenase (KGSADH); KdxD represents gene encoding 2-keto-3-deoxy-D-xylonate dehydratase (KdxD); XD represents gene encoding D-xylonate dehydratase; XL represents gene encoding D-xylonolactonase (XL); XDH represents gene encoding D-xylose dehydrogenase (XDH); Cad represents gene encoding cis-aconitate decarboxylase; pyc represents gene encoding pyruvate carboxylase; gltA represents gene encoding citrate synthase.

(4) FIG. 3 is a diagram showing growth curves of different operon structures of the Escherichia coli transformant of the present invention, in which BW5113 icd+pKL5+pKL6 indicates the phenotype of transforming pKL5 and pKL6 plasmids into the Escherichia coli strain; BW25113 icd+pKL7+pKL8 indicates the phenotype of transforming pKL7 and pKL8 plasmids into the Escherichia coli strain.

(5) FIG. 4A is a data diagram showing the effect of IA production in the environment fed with ammonium salts ((NH.sub.4).sub.2SO.sub.4) by the Escherichia coli transformant BW25113 icd xylA yjhH yagE of the present invention, in which C represents only fed with 5 g/L glycerol and xylose; C-2 g/L N represents fed with 5 g/L glycerol, xylose and 2 g/L (NH.sub.4).sub.2SO.sub.4; C-8 g/L N represents fed with 5 g/L glycerol, xylose and 8 g/L (NH.sub.4).sub.2SO.sub.4.

(6) FIG. 4B is a data diagram showing the cell density of the Escherichia coli transformant BW25113 icd xylA yjhH yagE of the present invention in the environment fed with ammonium salts ((NH.sub.4).sub.2SO.sub.4), in which C represents only fed with 5 g/L glycerol and xylose; C-2 g/L N represents fed with 5 g/L glycerol, xylose and 2 g/L (NH.sub.4).sub.2SO.sub.4; C-8 g/L N represents fed with 5 g/L glycerol, xylose and 8 g/L (NH.sub.4).sub.2SO.sub.4.

(7) FIG. 4C is a data diagram showing the xylose consumption of the Escherichia coli transformant BW25113 icd xylA yjhH yagE of the present invention in the environment fed with ammonium salts ((NH.sub.4).sub.2SO.sub.4), in which C represents only fed with 5 g/L glycerol and xylose; C-2 g/L N represents fed with 5 g/L glycerol, xylose and 2 g/L (NH.sub.4).sub.2SO.sub.4; C-8 g/L N represents fed with 5 g/L glycerol, xylose and 8 g/L (NH.sub.4).sub.2SO.sub.4.

(8) FIG. 4D is a data diagram showing the glycerol consumption of the Escherichia coli transformant BW25113 icd xylA yjhH yagE of the present invention in the environment fed with ammonium salts ((NH.sub.4).sub.2SO.sub.4), in which C represents only fed with 5 g/L glycerol and xylose; C-2 g/L N represents fed with 5 g/L glycerol, xylose and 2 g/L (NH.sub.4).sub.2SO.sub.4; C-8 g/L N represents fed with 5 g/L glycerol, xylose and 8 g/L (NH.sub.4).sub.2SO.sub.4.

(9) FIG. 5A is a data diagram of glycerol and xylose consumption under two stages fermentation.

(10) FIG. 5B is a data diagram of glycerol and xylose consumption under one stage fermentation.

(11) FIG. 6A is a data diagram of IA production titer and acetate titer under two stages fermentation.

(12) FIG. 6B is a data diagram of IA production titer and acetate titer under one stage fermentation.

(13) FIG. 7 is a data diagram of IA production titer and acetate titer at 30 C. and 30% dissolved oxygen.

(14) FIG. 8 is a schematic diagram showing gluconeogenesis from malate to pyruvate catalyzed by malate dehydrogenase (maeA and maeB both encode for malate dehydrogenase).

(15) FIG. 9 is a data diagram showing the effect of different initial xylose concentrations on IA production.

(16) FIG. 10 is a data diagram showing the effect of the Escherichia coli transformant of the present invention on IA production scale up in the bioreactor.

(17) FIG. 11 is a data diagram showing the effect of the maeA maeB double knockout strain of the present invention on affecting IA production and acetate accumulation, in which BW25113 icd xylA yjhH yagE+pKL5+pKL6 indicates the Escherichia coli strain in which maeA and maeB genes are not deleted; BW25113 icd xylA yjhH yagE maeA maeB+pKL5+pKL6 indicates the Escherichia coli strain in which maeA and maeB genes are deleted.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT

(18) In the following detailed description of the embodiments of the present invention, reference is made to the accompanying drawings, which are shown to illustrate the specific embodiments in which the present disclosure may be practiced. These embodiments are provided to enable those skilled in the art to practice the present disclosure. It is understood that other embodiments may be used and that changes can be made to the embodiments without departing from the scope of the present invention. The following description is therefore not to be considered as limiting the scope of the present invention.

Definition

(19) As used herein, the data provided represent experimental values that can vary within a range of 20%, preferably within 10%, and most preferably within 5%.

(20) As used herein, the terms expression plasmid and expression vector can be used interchangeably, and refer to any recombinant expression system that can constitutively or inducibly express a selected nucleic acid sequence in any competent host cell in vitro or in vivo. The expression plasmid can be a linear or circular expression system and encompasses an expression system that maintains the episomal form or is integrated into the genome of the host cell. The recombinant expression system may or may not have the ability to self-replicate, and it may only drive the transient expression of the host cell.

(21) According to the present invention, -ketoglutaric acid is the end product of nonphosphorylative pathways, and is essential for E. coli to grow. Inactivation of icd turns E. coli into both -ketoglutarate and glutamate auxotroph. Rescuing -ketoglutarate auxotroph via nonphosphorylative pathways serves as a selection force to discover new functional gene clusters.

Example 1

(22) Pathway to Decouple Itaconate Production from Endogenous -Ketoglutaric Acid Biosynthesis in Escherichia coli Transformant of Present Invention

(23) In this example and the following examples, all chemicals and reagents were purchased from Sigma-Aldrich (Saint Louis, Mo.) unless otherwise specified. KOD DNA polymerase and KOD Xtreme DNA polymerase were purchased from EMD Chemicals (San Diego, Calif.). All oligonucleotides were synthesized from IDT (Singapore).

(24) All strains, plasmids and their genotypes are shown in Table 1 and Table 2. All gene fragments were amplified by corresponding primers listed in Table 3. The reference of the D-xylose dehydrogenase (XDH) gene, the D-xylonolactonase (XL) gene, the 2-keto-3-deoxy-D-xylonate dehydratase (KdxD) gene, and the 2-ketoglutarate semialdehyde dehydrogenase (KGSADH) gene from Escherichia coli is Tai, Y. et al., Engineering Nonphosphorylative Metabolism to Generate Lignocellulose-derived Products. Nature, 2016. The reference of the isocitrate dehydrogenase (icd) gene from Escherichia coli is Chang, P., et al., Engineering efficient production of itaconic acid from diverse substrates in Escherichia coli. J Biotechnol, 2017. All plasmids were constructed by Gibson DNA assembly with purified fragments (see Gibson, D. G, et al., Enzymatic assembly of DNA molecules up to several hundred kilobases. Nat Methods, 2009. 6(5): p. 343-5). All plasmids were then propagated in XL-1 Blue (Stratagene). Host gene deletion of icd, xylA, yagE, yjhH, maeA and maeB was achieved by P1 transduction using the Keio collection strains as the donor (see Baba, T., et al., Construction of Escherichia coli K-12 in-frame, single-gene knockout mutants: the Keio collection. Mol Syst Biol, 2006. 2: p. 2006 0008). The kan.sup.R insertion into the target gene region was further removed as described in Datsenko, K. A. and B. L. Wanner, One-step inactivation of chromosomal genes in Escherichia coli K-12 using PCR products. Proc Natl Acad Sci USA, 2000. 97(12): p. 6640-5.

(25) TABLE-US-00001 TABLE 1 Strain Genotype Reference E. coli strain rrnB.sub.T14 lacZ.sub.WJ16hsdR514 Datsenko, K. A. and BW25113 araBAD.sub.AH33 rhaBAD.sub.LD78 B. L. Wanner, One- step inactivation of chromosomal genes in Escherichia coli K-12 using PCR products. Proc. Natl. Acad. Sci. U.S.A., 2000. 97(12): p. 6640-5 E. coli strain recA1 endA1 gyrA96 Stratagene XL-1 Blue thi-1 hsdR17 supE44 relA1 lac [F proAB lacI.sup.qZM15 Tn10 (Tet.sup.R)] E. coli strain BW25113 icd Chang, P., et al., BW25113 Engineering icd efficient production of itaconic acid from diverse substrates in Escherichia coli. J Biotechnol, 2017. 249: p. 73-81 E. coli strain BW25113 Present invention BW25113 xylAyjhHyagEicd xylAyjhHyagEicd E. coli strain BW25113 Present invention BW25113 xylAyjhHyagEicdmaeA xylAyjhHyagEicd maeB maeAmaeB

(26) TABLE-US-00002 TABLE 2 Plasmid Genotype Reference PGC07 P15A origin, SpecR, PLlacO1: Chang, P, et al., gltA(EC)pyc(CG) Engineering efficient production of itaconic acid from diverse substrates in Escherichia coli. J Biotechnol, 2017. 249: p. 73-81 pPC150 ColE1 origin, KanR, PLlacO1: Chang, P, et al., cad(AT) Engineering efficient production of itaconic acid from diverse substrates in Escherichia coli. J Biotechnol, 2017. 249: p. 73-81 pPC168 ColE1 origin, KanR, PLlacO1: Chang, P, et al., cad(AT)acnB(EC) Engineering efficient production of itaconic acid from diverse substrates in Escherichia coli. J Biotechnol, 2017. 249: p. 73-81 pKL01 P15A origin, SpecR, PLlacO1: Present invention gltA(CG)pyc(CG) pKL02 ColE1 origin, KanR, PLlacO1: Present invention cad(AT)acnA(EC) pKL03 ColE1 origin, KanR, PLlacO1: Present invention cad(AT)gltA(EC) pKL04 ColE1 origin, KanR, PLlacO1: Present invention cad(AT)gltA(EC) pyc(CG) pKL05 ColE1 origin, AmpR, PLlacO1: Present invention KGSADH pKL06 P15A origin, SpecR, PLlacO1: Present invention XDH-XL-XD-KdxD pKL07 ColE1 origin, KanR, PLlacO1: Present invention cad- KGSADH-XDH pKL08 P15A origin, SpecR, PLlacO1: Present invention gltA(EC)pyc(CG)-XL-XD-KdxD

(27) TABLE-US-00003 TABLE 3 SEQ Primers ID No. Purpose IA28 1 Forward primer of gltA(CG) in pKL01 cloning IA29 2 Reverse primer of gltA(CG) in pKL01 cloning IA30 3 Forward primer of pyc(CG) in pKL01 cloning IA31 4 Reverse primer of pyc(CG) in pKL01/8 cloning IA03 5 Forward primer of cad(AT) in pKL02 cloning IA24 6 Reverse primer of cad(AT) in pKL02 cloning IA26 7 Forward primer of acnA(EC) in pKL02 cloning IA27 8 Reverse primer of acnA(EC) in pKL02 cloning IA05 9 Forward primer of gltA(EC) in pKL03 cloning IA35 10 Reverse primer of gltA(EC) in pKL03 cloning IA04 11 Reverse primer of cad(AT) in pKL03 cloning cad-pLac f 12 Forward primer of cad(AT) in pKL03 cloning IA03 13 Forward primer in pKL04 cloning IA06 14 Reverse primer in pKL04 cloning IAX3 15 Forward primer in pKL05 cloning IAX4 16 Reverse primer in pKL05 cloning IAX8 17 Forward primer of XDH-XL cloning IAX9 18 Reverse primer of XDH-XL cloning IAX10 19 Forward primer of XD cloning IAX11 20 Reverse primer of XD cloning IAX12 21 Forward primer of KdxD cloning IAX13 22 Reverse primer of KdxD cloning IA53 23 Forward primer of pKL07 cloning IA54 24 Reverse primer of pKL07 cloning IA55 25 Forward primer of pKL07 cloning IA56 26 Reverse primer of pKL07 cloning IA49 27 Forward primer of pKL08 cloning IA51 28 Forward primer of pKL08 cloning IA50 29 Reverse primer of pKL08 cloning IAX02 30 Reverse primer of pKL08 cloning

(28) For the itaconate (IA) production under the expression of nonphosphorylative pathway, single colonies were chosen from LB plates and inoculated into 2 mL of LB media contained in test tubes with the appropriate antibiotics (kanamycin 50 g/mL and spectinomycin 50 g/mL). The overnight culture grown in LB at 37 C. in a rotary shaker (250 rpm) was then inoculated (1%, v/v) into 20 mL of M9 medium (12.8 g Na.sub.2HPO.sub.4.7H.sub.2O, 3 g KH.sub.2PO.sub.4, 0.5 g NaCl, 1 g NH.sub.4Cl, 1 mmol MgSO.sub.4, 1 mg vitamin B1 and 0.1 mmol CaCl.sub.2 per liter of water), 1000 trace metal mix A5 (2.86 g H.sub.3BO.sub.3, 1.81 g MnCl.sub.2.4H.sub.2O, 0.222 g ZnSO.sub.4.7H.sub.2O, 0.39 g Na.sub.2MoO.sub.4.2H.sub.2O, 0.079 g CuSO.sub.4.5H.sub.2O, 0.049 g Co(NO.sub.3).sub.2.6H.sub.2O per liter water), 10 g/L glycerol with xylose (2, 5, 10, 20 g/L being test separately) and appropriate antibiotics in 250 mL baffled flask with screwed cap. The cultures were grown at 37 C. in a rotary shaker (250 rpm) to an OD.sub.600 of 0.3-0.4, then induced with 0.1 mM IPTG The induced cultures were grown at 30 C. in a rotary shaker (250 rpm). Samples were taken throughout the production period, centrifuged for HPLC analysis.

(29) Product samples were applied (0.02 mL) to an Agilent Technologies 1260 infinity HPLC equipped with an auto-sampler (Agilent Technologies) and an Agilent Hi-Plex H column (5 mM H.sub.2SO.sub.4, 0.6 mL/min, column temperature at 50 C.). Organic acids were detected using a photodiode array detector at 210 nm or 254 nm. Xylose and glycerol were detected using refractive index (RI Detector). Concentrations were determined by extrapolation from standard curves.

(30) For the itaconate production experiment for optimizing the IA production pathway genes, 5 g/L yeast extract and 20 g/L glucose were added. For the ammonium salts experiment, medium was adjusted pH every 12 hours and fed with 5 g/L xylose and 5 g/L glycerol with different amount of ammonium salts. For the growth curve experiment, using the same culture medium (i.e., M9 medium) and carbon source as itaconate production under the expression of nonphosphorylative pathway experiment. Culture temperature was kept at 37 C.

(31) In this example, to achieve efficient IA production, icd inactivation (or knockout) is a necessary strategy. However, it accompanies with additional supply of nutrients such as yeast extract and glutamate to resolve glutamate auxotrophy. The extra production cost may hinder IA production commercialization. In order to decouple IA production and alpha-ketoglutarate (-KG) biosynthesis in icd inactivated E. coli, the nonphosphorylative pathway was recruited to convert xylose into -KG so as to resolve the concern of glutamate auxotrophy. For IA production, genes such as cis-aconitate decarboxylase (CAD) from Aspergillus terreus, citrate synthase (gltA) from E. coli and pyruvate carboxylase (pyc) from Corynebacterium glutamicum (CG) were selectively overexpressed, and isocitrate dehydrogenase (icd) gene was completely blocked via gene deletion for efficient IA production.

(32) For the nonphosphorylative pathway, gene cluster from Burkholderia xenovorans, which was demonstrated to functionally convert xylose into -KG was included. Xylose isomerase (XylA) gene, 2-keto-3-deoxygluconate aldolase (yagE) gene and 2-dehydro-3-deoxy-D-pentonate aldolase (yjhH) gene were further inactivated to reduce the competition between the endogenous metabolic pathway of E. coli and the target metabolic pathway for intermediate metabolites. Glycerol derived from biodiesel production industry is an abundant byproduct and thus is an attractive candidate for bioconversion carbon source. Moreover, glycerol assimilation pathway will generate more energy (as the form of adenosine triphosphate, ATP) compared to utilization of glucose and xylose. Xylose ranks as the major sugars in lignocellulosic hydrolysate. The schematic diagram showing the pathway to decouple IA production from endogenous -ketoglutaric acid biosynthesis in the Escherichia coli transformant of the present invention is shown in FIG. 1.

(33) FIG. 1 is a schematic diagram showing the pathway to decouple IA production from endogenous -ketoglutaric acid biosynthesis in the Escherichia coli transformant of the present invention. As shown in FIG. 1, the E. coli transformant of the present invention (icd gene is inactivated) converts xylose into -KG through the nonphosphorylative metabolic pathway (expressing the XDH gene, the XL gene, the XD gene, the KdxD gene, and the KGSADH gene), which is different from the traditional pathway of endogenous -KG biosynthesis, so that IA can be produced without adding additional protein nutrients, such as yeast extract or glutamate.

Example 2

(34) Constructing Nonphosphorylative Pathway Using Escherichia coli Transformant of Present Invention

(35) Icd knockout makes the cell lose the ability to convert isocitrate into -KG and the cell needs extra supply of -KG FIG. 2 is a schematic diagram showing the gene combination for constructing a nonphosphorylative pathway using the Escherichia coli transformant of the present invention. As shown in FIG. 2, the gene cluster of Burkholderia xenovorans is recruited and the operon structure is further optimized for improving cell growth. In particular, the expression of the XDH gene is expressed by a high-expression plasmid to enhance gene expression in the strain.

(36) FIG. 3 is a diagram showing growth curves of different operon structures of the Escherichia coli transformant of the present invention. The results of this example show that using the E. coli transformant of the present invention to construct a nonphosphorylative pathway can enhance cell growth to OD.sub.600 of up to 1.6 in 36 hours without exogenous supply of -KG.

Example 3

(37) Determination of IA Production Cultivation Condition Under Expression of IA Pathway and Nonphosphorylative Pathway of Present Invention

(38) To improve the metabolic pathway efficiency, it is common to block competing pathways. Therefore, the native xylose isomerase (xylA), 2-dehydro-3-deoxy-D-pentonate aldolase (yjhH) and 2-keto-3-deoxygluconate aldolase (yagE) in E. coli are blocked (the deletion of competitive pathways for non-phosphorylation is shown in FIG. 1), so that the E. coli transformant (BW25113 icd xylA yjhH yagE) is constructed for following experiments.

(39) Researchers have suggested that the supply of ammonium salts as nitrogen source which can accumulate more cell mass (see Harder, B. J., K. Bettenbrock, and S Klamt, Temperature-dependent dynamic control of the TCA cycle increases volumetric productivity of itaconic acid production by Escherichia coli. Biotechnol Bioeng, 2018. 115(1): p. 156-164). Therefore, the effect of supply of ammonium salts on IA production is investigated in the present invention. Cell mass is positively correlated with IA production (g/L), and can accumulate more activated transformants, thereby increasing IA production. The results are shown in FIGS. 4A-4D.

(40) FIG. 4A is a data diagram showing the effect of IA production in the environment fed with ammonium salts ((NH.sub.4).sub.2SO.sub.4) by the Escherichia coli transformant BW25113 icd xylA yjhH yagE of the present invention. FIG. 4B is a data diagram showing the cell density of the Escherichia coli transformant BW25113 icd xylA yjhH yagE of the present invention in the environment fed with ammonium salts ((NH.sub.4).sub.2SO.sub.4). FIG. 4C is a data diagram showing the xylose consumption of the Escherichia coli transformant BW25113 icd xylA yjhH yagE of the present invention in the environment fed with ammonium salts ((NH.sub.4).sub.2SO.sub.4). FIG. 4D is a data diagram showing the glycerol consumption of the Escherichia coli transformant BW25113 icd xylA yjhH yagE of the present invention in the environment fed with ammonium salts ((NH.sub.4).sub.2SO.sub.4). As shown in FIGS. 4A and 4B, there is a significant difference between feeding with or without ammonium salt (the C group in FIGS. 4A and 4B indicates no supply of ammonium salt, and other groups indicate supply of ammonium salt). Higher cell mass and IA production was achieved by extra supply of ammonium salts. Supplying ammonium salts prolonged IA production as well. However, whether it is 2 g/L (NH.sub.4).sub.2SO.sub.4 or 8 g/L (NH.sub.4).sub.2SO.sub.4, the feeding amount of nitrogen salts shows no big difference. In addition, the group fed only with glycerol and xylose as carbon source ended up with lower glycerol consumption but almost the same amount of xylose consumption as the group fed with ammonium salts (see FIGS. 4C and 4D), which may cause by the accumulation of -KG result from limited amount of nitrogen resource. The nitrogen source is a cofactor in the metabolic pathway for converting -KG into glutamate, so if there is no supply of nitrogen source, it may lead to a decrease in the conversion efficiency of the metabolic pathway, and accumulate -KG. Hence, glycerol derived carbon flux from central metabolism cannot enter the TCA cycle which result in lower glycerol consumption.

Example 4

(41) Effect Evaluation of IA Production Scaled Up in Bioreactor by Escherichia coli Transformant of Present Invention

(42) Combined previous examples on designing synergistic operons of IA and nonphosphorylative pathway, optimized IA production via substrate coutilization and extra supply of ammonium salts, the process was attempted to scale up by 1 L bioreactor which can consistently control pH, temperature and dissolved oxygen (DO). Cad protein prefer folding and function under lower temperature in E. coli of the present invention. Hence, two different culture temperatures and DO 20% were first tested. First condition, starting temperature was 37 C. and changed to 30 C. when OD.sub.600 reaches about 0.6 which was called two-stage fermentation. Second condition kept at 30 C. throughout the whole production process which was called one-stage fermentation. The results are shown in FIG. 5A, FIG. 5B, FIG. 6A and FIG. 6B. FIG. 5A is a data diagram of glycerol and xylose consumption under two stages fermentation. FIG. 5B is a data diagram of glycerol and xylose consumption under one stage fermentation. FIG. 6A is a data diagram of IA production titer and acetate titer under two stages fermentation. FIG. 6B is a data diagram of IA production titer and acetate titer under one stage fermentation. As shown in FIG. 5A and FIG. 5B, two-stages process exhibited slightly faster growth in the first 16 hours which probably due to higher cultivation temperature. One-stage fermentation consumed approximately 4-fold glycerol compared to two-stages process which may result from the correct folding of Cad under lower temperature (see FIG. 5A, FIG. 5B, FIG. 6A and FIG. 6B). Glycerol consumption reflected on the IA titer as well. Unexpectedly, lots of xylose were consumed compared to glycerol. Though the significant consumption difference was not shown in the flask experiment, carbon source of the strain of the present invention prefers sugar such as xylose rather than glycerol.

(43) Owing to the high oxygen requirement for efficient IA production, the dissolved oxygen level was thus increased to 30%. The result is shown in FIG. 7. FIG. 7 is a data diagram of IA production titer and acetate titer at 30 C. and 30% dissolved oxygen. As shown in FIG. 7, IA titer was successfully reached to 12.49 g/L in 100 hours via the increase of DO level. However, significant amount of acetate was detected to be 14 g/L in 100 hours as well. A great amount of acetate will induce pH and osmotic pressure to E. coli. For further optimizations of IA production, acetate formation is the major hurdle of the current fermentation process.

Example 5

(44) Strategies for Directing Carbon Flux into IA Production

(45) Observing from previous results, xylose was largely consumed rather than glycerol which implying the conversion of xylose into acetate. Xylose is assimilated to form -KG -KG then can take part in the subsequent reaction in the TCA cycle. When -KG is converted into malate or oxaloacetate, there are several enzymes that can catalyze gluconeogenesis reaction to transform TCA cycle intermediates into central metabolites such as pyruvate and phosphoenolpyruvate. Hence, these xylose derived central metabolites can be further directed into acetate biosynthesis. Under the assumption of xylose overflow to form acetate via gluconeogenesis pathways, by blocking these pathways, the carbon flux from xylose can be suppressed so as to reduce acetate production. Researchers have reported the endogenous protein expression difference after icd was deleted in E. coli. Malate dehydrogenase (mae) was upregulated approximately 21-folds, which can prove the assumption of xylose overflow through the gluconeogenesis pathway. FIG. 8 is a schematic diagram showing gluconeogenesis from malate to pyruvate catalyzed by malate dehydrogenase (maeA and maeB both encode for malate dehydrogenase). As shown in FIG. 8, there are two malate dehydrogenases maeA and maeB in E. coli.

(46) In avoidance of TCA cycle intermediates accumulation, the nonphosphorylative pathway efficiency needs to be adjusted. Rather than placing adjustment on the aspect of gene modification, by lowering the initial xylose concentration in the culture medium, so that the pathway efficiency is adjusted to some extent. The result is shown in FIG. 9. FIG. 9 is a data diagram showing the effect of different initial xylose concentrations on IA production. As shown in FIG. 9, 2 g/L initial xylose concentration significantly enhances IA production compared with that of other initial xylose concentrations.

Example 6

(47) Escherichia coli Transformant of Present Invention can Produce a Large Amount of IA in 1 L Bioreactor

(48) In this example, IA production was performed in the stirred-tank 1 L bioreactor (Major science). Single colonies were chosen from LB plates and inoculated into 2 mL of LB media contained in test tubes with the appropriate antibiotics (kanamycin 50 g/mL and spectinomycin 50 g/mL). The overnight culture grown in LB at 37 C. in a rotary shaker (250 rpm) was then inoculated (1%, v/v) into 25 mL LB at 37 C. for 24 hours. Centrifuging to separate LB and the cells, resuspended using filtered water to the same volume. 10% of the flask culture was then inoculated (10%, v/v) into 0.7 L bioreactor with M9 medium (12.8 g Na.sub.2HPO.sub.4.7H.sub.2O, 3 g KH.sub.2PO.sub.4, 0.5 g NaCl, 1 g NH.sub.4Cl, 1 mmol MgSO.sub.4, 1 mg vitamin B1 and 0.1 mmol CaCl.sub.2 per liter of water), 1000 trace metal mix A5 (2.86 g H.sub.3BO.sub.3, 1.81 g MnCl.sub.2.4H.sub.2O, 0.222 g ZnSO.sub.4.7H.sub.2O, 0.39 g Na.sub.2MoO.sub.4.2H.sub.2O, 0.079 g CuSO.sub.4.5H.sub.2O, 0.049 g Co(NO.sub.3).sub.2.6H.sub.2O per liter water), 20 g/L glycerol with 5 g/L xylose, 0.1 mM IPTG and appropriate antibiotics. Dissolved oxygen (DO) was maintained at 20% or 30% with respect to air saturation by raising the stirrer speed (from 550 to 700 rpm). The aeration was set to 1 vvm (volume of gas per volume of liquid per minute). The pH was maintained at 7 by the automatic addition of 5 N NaOH. Xylose stock for feeding purpose is 300 g/L; glycerol is 600 g/L with 40 g/L ammonium sulfate.

(49) Combining all the optimization process together, includes: one stage fermentation (keep at 30 C.) for better protein folding of Cad, control culture environment at high oxygen level (DO 30%), feed ammonium salts to prolong IA production and lower the initial xylose concentration. The result of this example is shown in FIG. 10. FIG. 10 is a data diagram showing the effect of the Escherichia coli transformant of the present invention (BW25113 icd xylA yjhH yagE+pKL7+pKL8) on IA production scale up in the bioreactor. As shown in FIG. 10, integrating all this optimization condition, the Escherichia coli transformant of the present invention successfully produces 20.01 g/L IA in 90 hours with yield 0.62 (g IA/g glycerol) and productivity 0.24 g/L/hr. Most importantly, high yield (86% of theoretical yield) of IA production with little amount of acetate as byproduct (3.7 g/L).

Comparative Example

(50) Effect of maeA maeB Double Knockout Strain on IA Production and Acetate Accumulation

(51) The maeA and maeB double knockout strain (BW25113 icd xylA yjhH yagE maeA maeB) was then constructed for IA production test. The result is shown in FIG. 11.

(52) FIG. 11 is a data diagram showing the effect of the maeA maeB double knockout strain of the present invention on affecting IA production and acetate accumulation. As shown in FIG. 11, inactivation of these two genes resulted in acetate increase and IA titer reduction. The result may attribute to the accumulation of TCA cycle intermediates thus hinder the entering carbon flux from central metabolites such as acetyl-CoA which can be easily directed into acetate.

(53) In summary, the Escherichia coli transformant of the present invention certainly has the effect of: by constructing a heterologous metabolic pathway, the nonphosphorylative pathway of Burkholderia xenovorans in Escherichia coli, enables the strain to self-convert to synthesize -ketoglutaric acid and further synthesize glutamate by metabolizing xylose. Furthermore, in the medium without additional protein nutrient source, the growth of the Escherichia coli transformant of the present invention is optimized that the original cell concentration of OD.sub.600 is 0.296 (36 hours)(before optimization of gene combination), and the optimized cell concentration of OD.sub.600 is 1.62 (36 hours)(after optimization of gene combination) through the optimization of gene combination. Using glycerol and xylose can increase IA production and optimize cell growth, and the yield of IA can reach 1.2 g/L (24 hours) by eliminating the competitive pathways of the nonphosphorylative metabolic pathway. The experimental results of the present invention confirm that reducing the initial concentration of xylose in the medium can increase the yield of IA by 2.2 g/L (24 hours), and in combination with the above optimized conditions, the process is amplified in a 1 liter fermentation tank (i.e., a bioreactor), the yield of IA can achieve 20.01 g/L (90 hours), 0.62 (g IA/g glycerol), and 0.24 g/L/hour productivity in minimal medium. The IA titer can reach 1.4 g/L in 24 hours (cultured in the flask in minimal medium without additional protein nutrient source).

(54) Although the present invention has been described with reference to the preferred embodiments, it will be apparent to those skilled in the art that a variety of modifications and changes in form and detail may be made without departing from the scope of the present invention defined by the appended claims.