PROCESS FOR THE PRODUCTION OF ORTHO-AMINOBENZOIC ACID AND/OR ANILINE BY USING RECOMBINANT YEAST

Abstract

The present invention relates to the production of o-aminobenzoic acid from fermentable substrates using yeast cells.

Claims

1.-15. (canceled)

16. A method for producing o-aminobenzoic acid comprising the steps of a) fermenting at least one fermentable substrate in a fermentation vessel using a yeast cell capable of converting the at least one fermentable substrate into o-aminobenzoic acid; and b) separating the produced o-aminobenzoic acid from the fermentation broth.

17. The method according to claim 16, wherein the separation of o-aminobenzoic acid in method step b) is performed after lowering the pH of the fermentation broth.

18. The method according to claim 16, wherein the separation of the produced solid o-aminobenzoic acid in method step b) is performed by adjusting the rotation speed of a stirrer in the fermentation vessel.

19. The method according to claim 16, wherein the separation of the produced solid o-aminobenzoic acid in method step b) is performed by filtration, settling, hydrocyclons and centrifugation

20. The method according to claim 16, wherein the separation of the produced o-aminobenzoic acid in method step b) is performed by extraction with a suitable solvent

21. The method of claim 20, wherein the o-aminobenzoic acid is extracted from fermentation broth which has been removed from the fermentation vessel.

22. The method of claim 20, wherein the solvent is added to the fermentation broth in the fermentation vessel.

23. The method according to claim 16, wherein the fermentation in method step a) is performed under anoxic conditions.

24. The method according to claim 16, wherein the fermentation in method step a) is performed at a pH of less than 7.0.

25. The method according to claim 16, wherein a part of the o-aminobenzoic acid is produced during the stationary growth phase of the yeast cells.

26. A method for producing aniline comprising the method steps defined in claim 16 and an additional method step c) of converting the separated o-aminobenzoic acid to aniline.

27. The method according to claim 26, wherein the o-aminobenzoic acid is converted to aniline by thermal decarboxylation in the presence or absence of a catalyst.

28. A recombinant yeast cell comprising a modification of anthranilate phosphoribosyltransferase activity which decreases the activity of said enzyme.

29. A method comprising utilizing the recombinant yeast of claim 28 for producing o-aminobenzoic acid from at least one fermentable substrate.

30. The method of claim 29, wherein the production of o-aminobenzoic acid from at least one fermentable substrate is performed according to the method of claim 16.

Description

BRIEF DESCRIPTION OF THE FIGURES

[0094] FIG. 1: Results of an aerobic fed batch fermentation with yeast as described in example 1.

[0095] FIG. 2: Results of an anaerobic batch fermentation with yeast as described in example 1.

[0096] FIG. 3: Schematic depiction of the separation of solid oAB in the fermenting vessel. A: sterilization; B: fermentation; C: air compression; D: biomass separation; E1 and E2: adsorption and desorption; F: filtration; G: decarboxylation; H: distillation; I: filtration; J: crystallization. [0097] 1: carbon source (e.g. sugar); 2: nitrogen sources (e.g. NH.sub.3); 3: buffer solution (e.g. NaOH); 4: air; 5A and 5B: feeding points for HCl, may be used alternatively or combined; 6: exhaust air; 7: biomass suspension; 8: oAB crystals suspension; 9: eluent, e.g., dilute NaOH; 10: HCl; 11: waste water; 12: waste water; 13: CO.sub.2; 14: residue; 15: residue; 16: aniline product; 17: biomass

[0098] FIG. 4: Schematic depiction of the separation of solid oAB from the fermentation broth outside of the fermentation vessel. A: sterilization; B: fermentation; C: air compression; D: solid/solid/liquid separation; E1 and E2: adsorption and desorption; F: filtration; G: decarboxylation; H: distillation; I: filtration; J: crystallization. [0099] 1: carbon source (e.g. sugar); 2: nitrogen sources (e.g. NH.sub.3); 3: buffer solution (e.g. NaOH); 4: air; 5A and 5B and 5C: feeding points for HCl, may be used alternatively or combined; 6: exhaust air; 7: fermentation broth (biomass, water, oAB); 8: oAB crystals suspension; 9: eluent, e.g., dilute NaOH; 10: HCl; 11: waste water; 12: waste water; 13: CO.sub.2; 14: residue; 15: residue; 16: aniline product; 17: biomass

[0100] FIG. 5: Schematic depiction of the liquid extraction of oAB performed inside the fermentation vessel. A: sterilization; B: fermentation; C: air compression; D: biomass separation; E1 and E2: adsorption and desorption; G: decarboxylation; H: distillation; I: filtration; J: crystallization. [0101] 1: carbon source (e.g. sugar); 2: nitrogen sources (e.g. NH.sub.3); 3: buffer solution (e.g. NaOH); 4: air; 5A and 5B: feeding points for HCl, may be used alternatively or combined 6: exhaust air; 7: biomass suspension; 9: eluent, e.g., dilute NaOH; 10: HCl; 11: waste water; 12: waste water; 13: CO.sub.2; 16: aniline product; 17: biomass; 18: solvent; 19: oAB solution in solvent to feed to reaction; 20: solvent purge; 21: solvent makeup.

[0102] FIG. 6: Schematic depiction of the liquid extraction of oAB performed outside of the fermentation vessel. A: sterilization; B: fermentation; C: air compression; D: biomass separation; E1 and E2: adsorption and desorption; G: decarboxylation; H: distillation; I: filtration; J: crystallization; L: liquid extraction. [0103] 1: carbon source (e.g. sugar); 2: nitrogen sources (e.g. NH.sub.3); 3: buffer solution (e.g. NaOH); 4: air; 5A and 5B and 5C and 5D and 5E: feeding points for HCl, may be used alternatively or combined 6: exhaust air; 7: fermentation broth (biomass, water, oAB); 9: eluent, e.g., dilute NaOH; 10: HCl; 11: waste water; 12: waste water; 13: CO.sub.2; 16: aniline product; 17: biomass; 18: solvent feed to extractor; 19: oAB solution in solvent to feed to reaction; 20: solvent purge; 21: solvent makeup

[0104] FIG. 7: Diagram showing the solubility of oAB in water depending on the pH. It can be seen that solubility reaches its minimum between pH 3 and pH 4.

[0105] The following examples are only intended to illustrate the invention. They shall not limit the scope of the claims in any way.

EXAMPLES

Example 1 (Inventive): Production of o-Aminobenzoic Acid with Yeast

Strains, Media and Growth Conditions.

[0106] The Saccharomyces cerevisiae TRP4 knock out strain was purchased from GE Healthcare Dharmacon Inc. If not denoted differently all chemicals were acquired from Sigma-Aldrich (Sternheim). Saccharomyces cerevisiae was grown under sterile conditions at 30? C. in YPD broth (bacteriological peptone, 20 g/L, yeast extract, 10 g/L, glucose, 20 g/L) supplemented with G418 (200 ?g/mL) or defined Yeast Nitrogen Base (YNB) without Amino Acids Mineral Medium (ammonium sulfate, 5.0 g/L, biotin, 2.0 ?g/L, calcium pantothenate, 400 ?g/L, folic acid, 2.0 ?g/L, inositol, 2.0 mg/L, nicotinic acid, 400 ?g/L, p-aminobenzoic acid, 200 ?g/L, pyridoxine HCl, 400 ?g/L, riboflavin, 200 ?g/L, thiamine HCL, 400 ?g/L, citric acid, 0.1 g/L, boric acid, 500 ?g/L, copper sulfate, 40 ?g/L, potassium iodide, 100 ?g/L, ferric chloride, 200 ?g/L, magnesium sulfate, 400 ?g/L, sodium molybdate, 200 ?g/L, zinc sulfate, 400 ?g/L, potassium phosphate monobasic, 1.0 g/L, magnesium sulfate, 0.5 g/L, sodium chloride, 0.1 g/L, calcium chloride, 0.1 g/L) supplemented with Yeast Synthetic Drop-out Medium Supplements without Tryptophan (adenine, 18 mg/L, myo-inositol, 76 mg/L, p-aminobenzoic acid, 8 mg/L, uracil, 76 mg/L, L-leucine, 380 mg/L, L-alanine, L-arginine, L-asparagine, L-cysteine, L-histidine, L-isoleucine, L-lysine, L-methionine, L-phenylalanine, L-proline, L-serine, L-threonine, L-tyrosine, Lvaline, 76 mg/L, each), G418 (200 ?g/mL), ?-D-glucose (20 g/L), and limiting amounts of L-tryptophan (5 mg/L for aerobic and 1.5 mg/L for anaerobic conditions, respectively). The strain was characterized in (fed)-batch fermenters (OmniFerm, HiTec Zang, Herzogenrath, Germany) with a cultivation volume of 1 L. Pre-cultures were inoculated from a glycerol stock [15% (v/v) glycerol] stored at ?80? C. Seed train comprises a 3 ml YPD culture in a test tube at constant shaking at 200 rpm for 12 h (pre-culture I), a 50 ml YPD culture in a 1000 ml Erlenmeyer flask on a rotary shaker at constant shaking at 200 rpm for 8 h (pre-culture II) and a 50 ml YNB culture in a 1000 ml Erlenmeyer flasks on a rotary shaker at constant shaking at 200 rpm for 12 h (pre-culture III). Pre-culture II was inoculated by transferring 1 ml from pre-culture I into fresh sterile YPD medium of pre-culture II. Pre-culture III was inoculated to an optical density at 600 nm (OD.sub.600) of 1 by transferring an appropriate amount of cells into a sterile conical centrifuge tube. After centrifugation (1,500?g, 5 min, RT) cells were suspended in sterile 1 ml saline (9 g/L sodium chloride) and transferred to the sterile YNB medium of pre-culture III. Procedure for inoculation of the fermenter to an OD.sub.600 of 1 from pre-culture III was the same as described for inoculation of pre-culture III. For yeast cultivation under aerobic conditions initial stirring speed was set to 500 rpm and air was supplied at 0.2 L/min. For anaerobic conditions a constant stirring speed of 300 rpm was used and N.sub.2 was supplied at 0.2 L/min. Oxygen and carbon dioxide levels in the exhaust gas of the fermenters were continuously monitored online using an off-gas analyzer (HiSense, HiTec Zang, Herzogenrath, Germany). For aerobic conditions dissolved oxygen was maintained at >30% air saturation by automatic adjustment of the stirring speed. For each condition pH was measured (Easyferm Plus VP 225, Hamilton H?chst, Germany) and maintained at 4.0 by automatic addition of 1.0 M (NH.sub.4)OH and 1 M HCl. For each condition the temperature was kept at 30? C. During the fermentation 1.5 ml samples were taken. An Eppendorf BioPhotometer (Eppendorf, Hamburg) was used for optical density measurements. An 1 mL aliquot of each sample was centrifuged for 5 min at 16,000?g (5415R; Eppendorf, Hamburg). Concentration of glucose, o-aminobenzoate and ethanol in the supernatant was determined with a CuBiAn XC (Optocell technology) biochemistry analyzer, HPLC-DAD (1100; Agilent Technologies, Santa Clara, USA), and GC-FID (7890A Agilent Technologies, Santa Clara, USA), respectively.

High Performance Liquid Chromatography

[0107] An Agilent 1100 series HPLC-DAD system [with diode array detector; Agilent Technologies, Santa Clara (USA)] was used to quantify the o-aminobenzoate concentration in culture supernatants. As stationary phase a C18 column Luna HPLC-column (4.6?250 mm; 3 pm; Phenomenex) was used at 20? C. with a binary solvent system consisting of methanol (solvent B) and water containing 0.1% (v/v) formic acid (solvent A). 10 ?L of diluted culture supernatant was applied. Separation was achieved by the following gradient at a flow rate of 0.5 mL/min: 0-1 min, 2% B; 1-2 min, 2-10% B; 2-12 min, 10-70% B; 12-23 min, 70-90% B; 23-25 min, 90-98% B, 25-27 min, 98% B; 27-27.5 min, 98%-2% B; 27.5-30 min, 2% B. The o-aminobenzoate concentration was determined by peak integration at 254 nm (retention time: 18.9 min) and comparing to an external calibration curve.

Gas Chromatography

[0108] An Agilent 7890A GC-system [Agilent Technologies, Santa Clara (USA)] was used to quantify the ethanol concentration in culture supernatants. A Stabiwax-DB column (30 m?0.32 mm, ID 1 ?m, Restek) was used. Separation was achieved by the following oven program: 0-3 min, 30? C.; 3-6 min, 40-150? C.; 6-8.4 min, 150-220? C. 1 ?L of diluted culture supernatant was applied. Injector was set to 250? C. with a total flow of 787.43 mL/min and a split ratio of 100:1, resulting in a flow of 7.7666 ml/min. Signals were detected via FID set to 300? C.

Results and Discussion

[0109] The yeast knock-out strain Saccharomyces cerevisiae TRP4 produced 320 mg/L o-aminobenzoic acid under aerobic conditions after 75 h of cultivation as determined by HPLC-DAD (254 nm). Under anaerobic conditions it produced 92 mg/L o-aminobenzoic acid after 73 h of cultivation. Production seems not to be coupled to growth since a constant accumulation of o-amonibenzoate during growth as well as in the stationary phase was observed. Assuming an OD.sub.600 of 1 is correlated to a dry weight of 0.45 g/L, specific productivity of o-aminobenzoic acid in the stationary phase was about 1.0 and 1.3 mg gDW.sup.?1 h.sup.?1, under aerobic and anaerobic conditions, respectively. As expected, under anaerobic conditions a significant amount of ethanol was produced as determined by GC-FID.