WO2012170059A1 - Procédés de production d'hexanediol (hdo) et d'hexaméthylènediamine (hmd) à partir de bouillons de fermentation contenant de l'acide adipique - Google Patents

Procédés de production d'hexanediol (hdo) et d'hexaméthylènediamine (hmd) à partir de bouillons de fermentation contenant de l'acide adipique Download PDF

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Publication number
WO2012170059A1
WO2012170059A1 PCT/US2011/050993 US2011050993W WO2012170059A1 WO 2012170059 A1 WO2012170059 A1 WO 2012170059A1 US 2011050993 W US2011050993 W US 2011050993W WO 2012170059 A1 WO2012170059 A1 WO 2012170059A1
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Prior art keywords
hmd
broth
solid portion
ammonia
water
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PCT/US2011/050993
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English (en)
Inventor
Olan S. Fruchey
Leo E. Manzer
Dilum Dunuwila
Brian T. Keen
Brooke A. Albin
Nye A. Clinton
Bernard D. Dombek
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Bioamber S.A.S.
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Priority claimed from PCT/US2011/039903 external-priority patent/WO2011159557A1/fr
Application filed by Bioamber S.A.S. filed Critical Bioamber S.A.S.
Publication of WO2012170059A1 publication Critical patent/WO2012170059A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
    • C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
    • C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
    • C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
    • C07C209/04—Preparation of compounds containing amino groups bound to a carbon skeleton by substitution of functional groups by amino groups
    • C07C209/14—Preparation of compounds containing amino groups bound to a carbon skeleton by substitution of functional groups by amino groups by substitution of hydroxy groups or of etherified or esterified hydroxy groups
    • C07C209/16—Preparation of compounds containing amino groups bound to a carbon skeleton by substitution of functional groups by amino groups by substitution of hydroxy groups or of etherified or esterified hydroxy groups with formation of amino groups bound to acyclic carbon atoms or to carbon atoms of rings other than six-membered aromatic rings
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives
    • C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives
    • C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
    • C07C51/44—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation

Definitions

  • This disclosure relates to processes for producing hexamethylenediamine (HMD), 5 adiponitrile (ADN), adipamide (ADM) and derivatives thereof from adipic acid (AA) obtained from fermentation broths containing diammonium adipate (DAA) or monoamrnonium adipate (MAA).
  • HMD hexamethylenediamine
  • ADN 5 adiponitrile
  • ADM adipamide
  • AA adipic acid obtained from fermentation broths containing diammonium adipate (DAA) or monoamrnonium adipate (MAA).
  • Certain carbonaceous products of sugar fermentation are seen as replacements for0 petroleum-derived materials for use as feedstocks for the manufacture of carbon-containing chemicals.
  • One such product is AA.
  • FIG. 1 is a block diagram of a process for making AA from a DAA containing broth.
  • Fig. 2 is a graph showing the solubility of AA in water as a function of temperature.
  • Fig 3. is a flow diagram showing the selected production of HDO, HMD, ADN, ADM and derivatives thereof.
  • Fig. 4 is a flow diagram showing the selected production of HMD, ADN, ADM and derivatives thereof from MAA.
  • Fig. 5 is a flow diagram showing the selected production of HMD, ADN, ADM and derivatives thereof from DAA.
  • FIG. 1 shows in block diagram form one representative example of a bioprocessing system 10.
  • a growth vessel 12 typically an in-place steam sterilizable fermentor, may be used to grow a microbial culture (not shown) that is subsequently utilized for producing the DAA, MAA and/or AA-containing fermentation broth.
  • Such growth vessels are known in the art and are not further discussed.
  • the microbial culture may comprise microorganisms capable of producing adipic acid from fermentable carbon sources such as carbohydrate sugars.
  • microorganisms include Escherichia coli (E. coli), Aspergillus niger, Corynebacterium glutamicum (also called Brevibacteriumflavum), Enterococcus faecalis, Veillonella parvula, Actinobacillus succinogenes. Paecilomyces varioti, Saccharomyces cerevisiae, Candida tropicalis, Bacteroides fragilis, Bacteroides ruminicola, Bacteroides amylophilus, Lebsiella pneumonae mixtures thereof and the like.
  • Preferred microorganisms include the Candida tropicalis (Castellani) Berkhout, anamorph strain OH23 having ATCC accession number 24887, E. coli strain AB2834/p D136/pKD8.243A/pKD8.292 having ATCC accession number 69875, the E. coli cosmid clones designated 5B 12, 5F5, 8F6 and 14D7 comprising a vector expressing the cyclohexanone monoxygenase having the amino acid sequence shown in SEQ ID NO: 2 and encoded by SEQ ID NO: 1 from Acinetobacter strain SE19, and the yeast strain available from Verdezyne, Inc. (Carslbad, CA, USA; hereinafter "Verdezyne Yeast") which produces AA from alkanes and other carbon sources.
  • Verdezyne Yeast the yeast strain available from Verdezyne, Inc.
  • Fermentation broths containing AA can be produced from the Candida tropicalis (Castellani) Berkhout, anamorph strain OH23 having ATCC accession number 24887 by culture at 32°C in a liquid medium containing 300 mg of NH 4 H 2 P0 4 , 200 mg of KH 2 P0 4 , 100 mg of K 2 HP0 4 , 50 mg of MgS0 4 *7H 2 0, 1 ⁇ g of biotin, 0.1 % (w/v) yeast extract and about 1 % (v/v) n-hexadecane in 100 ml of distilled water.
  • Other culture media such as YM broth containing «-hexadecane may also be used.
  • Fermentation broths containing AA can also be produced from E. coli strain AB2834/pKD136/pKD8.243A/pRD8.292 having ATCC accession number 69875. This can be done as follows.
  • One liter of LB medium (in 4 L Erlenmeyer shake flask) containing IPTG (0.2 ⁇ ⁇ ⁇ ), ampicillin (0.05 g), chloramphenicol (0.02 g) and spectinomycin (0.05 g) can be inoculated with 10 ' mL of an overnight culture of E. coli strain AB2834/pKD136/pKD8.243A/pKD8.292 cells grown at 250 rpm for 10 h at 37°C.
  • the cells can be harvested, resuspended in 1 L of M9 minimal medium containing 56 mM D-glucose, shikimic acid (0.04 g), IPTG (0.2 mM), ampicillin (0.05 g), chloramphenicol (0.02 g) and spectinomycin (0.05 g).
  • the cultures can then be returned to 37°C incubation.
  • the pH of the culture can be closely monitored, particularly over the initial 12 h. When the culture reaches a pH of 6.5, 5N NaOH or an appropriate amount of another base such as ammonium hydroxide can be added to adjust the pH back to approximately 6.8. Over the 48 h accumulation period, the culture should not allowed to fall below pH 6.3.
  • E. coli strain AB2834/p D136/pKD8.243A/pKD8.292 cells can essentially replace the 56 mM D-glucose in the medium with 17 mM cis, ct ' s-muconate.
  • the reduction of microbially synthesized cis, m-muconate AA to produce a fermentation broth containing AA can then proceed as follows. Fifty milligrams of platinum on carbon (10%) can be added to 6 mL of a cell-free culture supernatant from the fermentation containing about 17.2 mM cis, cw-muconate. This sample can then be hydrogenated at 50 psi hydrogen pressure for 3 h at room temperature to produce a fermentation broth containing AA. The fermentation broth produced in this fashion may contain, for example, about 15.1 mM AA. The procedure for producing fermentation broths containing AA by culturing E.
  • Fermentation broths containing AA can also be produced from the E. coli cosmid clones designated 5B 12, 5F5, 8F6 and 14D7 comprising a vector expressing the cyclohexanone monoxygenase SEQ ID NO: 2 encoded by SEQ ID NO: 1 from Acinetobacter strain SE19 by culturing these clones in M9 minimal medium supplemented with 0.4% glucose as the carbon source.
  • Cells can be grown at 30°C with shaking for 2 h and the addition of 330 ppm of cyclohexanol to the medium. This can be followed by further incubation at 30°C for an additional period of time such as, for example, 2 h, 4 h or 20 h or other time intervals.
  • Fermentation broths containing AA can also be produced with the Verdezyne Yeast strain available from Verdezyne, Inc. (Carslbad, CA, USA) which was reported on February 8, 2010 to produce AA when cultured in a medium (e.g., SD medium) comprising alkanes or other carbon sources such as sugars and plant-based oils.
  • a medium e.g., SD medium
  • alkanes or other carbon sources such as sugars and plant-based oils.
  • Fermentation broths containing AA can also be produced from E. coli or other microorganisms transformed with nucleic acids encoding succinyl-CoA:acetyl-CoA acyl transferase; 3-hydroxyacyl-CoA dehydrogenase; 3-hydroxyadipyl-CoA dehydratase; 5- carboxy-2-pentenoyl-CoA reductase; adipyl-CoA synthetase, phosphotransadipylase/adipate kinase, adipyl-CoA transferase or adipyl-CoA hydrolase. Fermentation broths containing AA can also be produced from E.
  • Fermentation broths containing AA can also be produced from E. coli or other microorganisms transformed with nucleic acids .
  • alpha-ketoadipyl-CoA synthetase phosphotransketoadipylase/alpha-ketoadipate kinase or alpha-ketoadipyl-CoA:acetl-CoA tranferase; 2-hydroxyadipyl-CoA dehydrogenase; 2-hydroxyadipyl-CoA dehydratase; 5- carboxy-2-penteoyl-CoA reductase; and adipyl-CoA synthetase, phosphotransadipylase/adipate kinase, adipyl-CoA:acetyl-CoA transferase or adipyl-CoA hydrolase.
  • Fermentation broths containing AA can also be produced from E. coli or other microorganisms transformed with nucleic acids encoding 2-hydroxyadipate dehydrogenase; 2-hydroxyadipyl-CoA synthetase, phosphotranshydroxyadipylase/2-hydroxy-adipate kinase or 2-hydroxyadipy!-CoA:acetyl-CoA transferase; 2-hydroxyadipyl-CoA dehydratase; 5- carboxy-2-pentenoyl-CoA reductase; and adipyl-CoA synthetase, phosphotransadipylase/adipate kinase, adipyl-CoA:acetyl-CoA transferase or adipyl-CoA hydrolase.
  • Fermentations with E. coli or other microorganisms transformed with nucleic acids encoding these enzymes may be performed using a variety of different carbon sources under standard conditions in standard culture mediums (e.g., M9 minimal medium) and appropriate antibiotic or nutritional supplements necessary to maintain the transformed phenotype.
  • standard culture mediums e.g., M9 minimal medium
  • appropriate antibiotic or nutritional supplements necessary to maintain the transformed phenotype.
  • the procedure for producing fermentation broths containing AA by culturing E. coli or other microorganisms transformed with nucleic acids encoding these enzymes, appropriate growth mediums and carbon sources are also described in US 2009/0305364, the subject matter of which is incorporated herein by reference.
  • a fermentable carbon source e.g., carbohydrates and sugars
  • a source of nitrogen and complex nutrients e.g., corn steep liquor
  • additional media components such as vitamins, salts and other materials that can improve cellular growth and/or product formation
  • water may be fed to the growth vessel 12 for growth and sustenance of the microbial culture.
  • the microbial culture is grown under aerobic conditions provided by sparging an oxygen-rich gas (e.g., air or the like).
  • an acid e.g., sulphuric acid or the like
  • ammonium hydroxide are provided for pH control during the growth of the microbial culture.
  • the aerobic conditions in growth vessel 12 are switched to anaerobic conditions by changing the oxygen-rich gas to an oxygen-deficient gas (e.g., C0 2 or the like).
  • the anaerobic environment may trigger bioconversion of the fermentable carbon source to AA in situ in growth vessel 12.
  • Ammonium hydroxide is provided for pH control during bioconversion of the fermentable carbon source ⁇ AA.
  • the AA that is produced is at least partially if not totally neutralized to DAA due to the presence of the ammonium hydroxide, leading to the production of a broth comprising DAA.
  • C0 2 may be an additional source of carbon for the produc tion of AA.
  • the contents of growth vessel 12 may be transferred via stream 14 to a separate bioconversion vessel 16 for bioconversion of a carbohydrate source to AA.
  • An oxygen-deficient gas e.g., C0 2 or the like
  • Ammonium hydroxide is provided for pH control during bioconversion of the carbohydrate source to AA. Due to the presence' of the ammonium hydroxide, the AA produced is at least partially neutralized to DAA, leading to production of a broth that comprises DAA.
  • CO2 may be an additional source of carbon for production of AA.
  • the bioconversion may be conducted at relatively low pH (e.g., about 3 to about 6).
  • a base (ammonium hydroxide or ammonia) may be provided for pH control during bioconversion of the carbohydrate source to AA.
  • ammonium hydroxide or ammonia
  • the AA produced is at least partially neutralized to MAA, DAA or a mixture comprising AA, MAA and/or DAA.
  • the AA produced- during bioconversion can be subsequently neutralized, optionally in an additional step, by providing either ammonia or ammonium hydroxide leading to a broth comprising DAA.
  • a "DAA-containing fermentation broth” generally means that the fermentation broth comprises DAA and possibly any number of other components such as MAA and/or AA, whether added and/or produced by bioconversion or otherwise.
  • a "MAA-containing fermentation broth” generally means that the fermentation broth comprises MAA and possibly any number of other components such as DAA and/or ' AA, whether added and/or produced by bioconversion or otherwise.
  • the broth resulting from the bioconversion of the fermentable carbon source typically contains insoluble solids such as cellular biomass and other suspended material, which are transferred via stream 18 to clarification apparatus 20 before distillation. Removal of insoluble solids clarifies the broth. This reduces or prevents fouling of subsequent distillation equipment.
  • the insoluble solids can be removed by any one of several solid-liquid separation techniques, alone or in combination, including but not limited to, centrifugation and filtration (including, but not limited to ultra-filtration, micro-filtration or depth filtration). The choice of filtration can be made using techniques known in the art. Soluble inorganic compounds can be removed by any number of known methods such as, but not limited to. ion-exchange, physical adsorption and the like.
  • centrifugation is a continuous disc stack centrifuge. It may be useful to add a polishing filtration step following centrifugation such as dead-end or cross- flow filtration, which may include the use of a filter aide such as diatomaceous earth or the like, or more preferably ultra-filtration or micro-filtration.
  • the ultra-filtration or micro- filtration membrane can be ceramic or polymeric, for example.
  • a polymeric membrane is SelRO MPS-U20P (pH stable ultra-filtration membrane) manufactured by Koch Membrane Systems (850 Main Street, Wilmington, MA, USA).
  • a filtration step may be employed alone using ultra-filtration or micro-filtration.
  • the clarified distillation broth should contain DAA in an amount that is at least a majority of, preferably at least about 70 wt%, more preferably about 80 wt% and most preferably at least about 90 wt% of all the diammonium dicarboxylate salts in the broth.
  • concentration of DAA and/or MAA as a weight percent (wt%) of the total dicarboxylic acid salts in the fermentation broth can be determined by high pressure liquid chromatography (HPLC) or other known means.
  • Water and ammonia are removed from distillation apparatus 24 as an overhead, and at least a portion may optionally be recycled via stream 26 to bioconversion vessel 16 (or growth vessel 12 operated in the anaerobic mode).
  • the specific distillation temperature and pressure are not critical as long as the distillation is carried out in a way that ensures that the distillation overhead contains water and ammonia, and the distillation' bottoms comprises at least some AA and at least about 20 wt% water.
  • a more preferred amount of water is at least about 30 wt% and an even more preferred amount is at least about 40 wt%.
  • the rate of ammonia removal from the distillation step increases with increasing temperature and also can be increased by injecting steam (not shown) during distillation.
  • the rate of ammonia removal during distillation may also be increased by conducting distillation under a vacuum or by sparging the distillation apparatus with a non-reactive gas such as air, nitrogen or the like.
  • Removal of water during the distillation step can be enhanced by the use of an organic azeotroping agent such as toluene, xylene, methylcyclohexane, methyl isobutyl ketone, cyclohexane, heptane or the like, provided that the bottoms contains at least about 20 wt% water.
  • an organic azeotroping agent such as toluene, xylene, methylcyclohexane, methyl isobutyl ketone, cyclohexane, heptane or the like
  • the bottoms contains at least about 20 wt% water.
  • an organic agent capable of forming an azeotrope consisting of the water and the agent distillation produces a biphasic bottoms that comprises an aqueous phase and an organic phase, in which case the aqueous phase can be separated from the organic phase, and the aqueous phase used as the distillation bottoms.
  • By-products such as adip
  • a preferred temperature for the distillation step is in the range of about 50°C to about 300°C, depending on the pressure. A more preferred temperature range is about 150°C to about 240°C, depending on the pressure. A distillation temperature of about 170°C to about 230°C is preferred. "Distillation temperature” refers to the temperature of the bottoms (for batch distillations this may be the temperature at the time when the last desired amount of overhead is taken).
  • Adding a water miscible organic solvent or an ammonia separating solvent may facilitate deammoniation over a variety of distillation temperatures and pressures as discussed above.
  • solvents include aprotic, bipolar, oxygen-containing solvents that may be able to form passive hydrogen bonds.
  • Examples include, but are not limited to, diglyme, triglyme, tetraglyme, sulfoxides such as dimethylsulfoxide (DMSO), amides such as dimethylformamide (DMF) and dimethylacetamide, sulfones such as dimethylsulfone, gamma-butyrolactone (GBL), sulfolane, polyethyleneglycol (PEG), butoxytriglycol, N- methy!pyrolidone (NMP), ethers such as dioxane, methyl ethyl ketone (MEK) and the like.
  • DMSO dimethylsulfoxide
  • amides such as dimethylformamide (DMF) and dimethylacetamide
  • sulfones such as dimethylsulfone, gamma-butyrolactone (GBL), sulfolane, polyethyleneglycol (PEG), butoxytriglycol, N- methy!pyrolidone
  • distillation it is important that the distillation be carried out in a way that ensures that at least some MAA and at least about 20 wt% water remain in the bottoms and even more advantageously at least about 30 wt%.
  • the distillation can be performed at atmospheric, sub-atmospheric or super-atmospheric pressures.
  • the distillation is conducted at super atmospheric pressure at a temperature of greater than 100°C to about 300°C to form an overhead that comprises water and ammonia and a liquid bottoms that comprises AA and at least about 20 wt% water.
  • Super atmospheric pressure typically falls within a range of greater than ambient atmosphere up to and including about 25 atmospheres.
  • the amount of water is at least about 30 wt%.
  • the distillation can be a one-stage flash, a multistage distillation (i.e., a multistage column distillation) or the like.
  • the one-stage flash can be conducted in any type of flasher (e.g., a wiped film evaporator, thin film evaporator, thermosiphon flasher, forced circulation flasher and the like).
  • the multistages of the distillation column can be achieved by using trays, packing or the like.
  • the packing can be random packing (e.g., Raschig rings, Pall rings, Berl saddles and the like) or structured packing (e.g., och-Sulzer packing, Intalox packing, Mellapak and the like), the trays can be of any design (e.g., sieve trays, valve trays, bubble-cap trays and the like).
  • the distillation can be performed with any number of theoretical stages.
  • the distillation apparatus is a column
  • the configuration is not particularly critical, and the column can be designed using well known criteria.
  • the column can be operated in either stripping mode,' rectifying mode or fractionation mode.
  • Distillation can be conducted in either batch, semi-continuous or continuous mode. In the continuous mode, the broth is fed continuously into the distillation apparatus, and the overhead and bottoms are continuously removed from the apparatus as they are formed.
  • the distillate from distillation is an ammonia water solution, and the distillation bottoms is a liquid, aqueous solution of MAA and AA, which may also contain other fermentation by-product salts (i.e., ammonium acetate, ammonium formate, ammonium lactate and the like) and color bodies.
  • the distillation bottoms can be transferred via stream 28 to cooling apparatus 30 and cooled by conventional techniques. Cooling technique is not critical. A heat exchanger (preferably with heat recovery) can be used. A flash vaporization cooler can be used to cool the bottoms to about 15°C. Cooling to 15°C typically employs a refrigerated coolant such as, for example, glycol solution or, less preferably, brine. A concentration step can be included prior to cooling to help increase product yield. Further, both concentration and cooling can be combined using known methods such as vacuum evaporation and heat removal using integrated cooling jackets and/or external heat exchangers.
  • a heat exchanger preferably with heat recovery
  • a flash vaporization cooler can be used to cool the bottoms to about 15°C. Cooling to 15°C typically employs a refrigerated coolant such as, for example, glycol solution or, less preferably, brine.
  • a concentration step can be included prior to cooling to help increase product yield. Further, both concentration and cooling can be combined using known methods such as vacuum evaporation and
  • the distillation bottoms is fed via stream 32 to separator 34 for separation of the solid portion from the liquid portion. Separation can be accomplished via pressure filtration (e.g., using Nutsche or Rosenmond type pressure filters), centrifugation and the like.
  • the resulting solid product can be recovered as product 36 and dried, if desired, by standard methods.
  • the liquid portion of the distillation bottoms 34 may contain remaining dissolved AA, any unconverted MAA, any fermentation by-products such as ammonium acetate, lactate, or formate, and other minor impurities.
  • This liquid portion can be fed via stream 38 to a downstream apparatus 40.
  • apparatus 40 may be a means for making a de-icer by treating in the mixture with an appropriate amount of potassium hydroxide, for example, to convert the ammonium salts to potassium salts. Ammonia generated in this reaction can be recovered for reuse in the bioconversion vessel 16 (or growth vessel 12 operating in the anaerobic mode). The resulting mixture of potassium salts is valuable as a de-icer and anti-icer.
  • the mother liquor from the solids separation step 34 can be recycled (or partially recycled) to distillation apparatus 24 via stream 42 to further enhance recovery of AA, as well as further convert MAA to AA.
  • the solid portion of the cooling-induced crystallization is substantially pure AA and is, therefore, useful for the known utilities of AA.
  • One such use is for the production of HMD, ADN, ADM and derivatives thereof.
  • HPLC can be used to detect the presence of nitrogen-containing impurities such as adipamide and adipimide.
  • the purity of AA can be determined by elemental carbon and nitrogen analysis.
  • An ammonia electrode can be used to determine a crude approximation of AA purity.
  • the fermentation broth may be a clarified MAA-containing fermentation broth or a clarified AA-containing fermentation broth.
  • the operating pH of the fermentation broth may be oriented such that the broth is a MAA- containing broth or a AA-containing broth.
  • MAA, DAA,- AA, ammonia and/or ammonium hydroxide may be added to those broths to attain a broth pH preferably less than 6 to facilitate production of the above-mentioned substantially pure AA.
  • such broth generally means that the fermentation broth comprises MAA and possibly any number of other components such as DAA and/or AA, whether added and/or produced by bioconversion or otherwise.
  • Streams comprising AA, MAA and/or DAA as described above may be converted to selected downstream products such as HMD, ADN, 6-aminocapronitrile (ACN), ADM and the like as described below.
  • the AA, MAA and/or DAA may be dissolved in water to form an aqueous solution thereof which can be directly fed to the downstream reactor.
  • the AA, MAA or DAA may be converted to ADN, either directly or indirectly through the intermediate ADM by dehydration. Such dehydrations may be achieved thermally, enzymatically or in the presence of catalysts. Thus, appropriate temperatures, pressures and catalysts are selected to achieve the appropriate level of dehydration, depending on whether the conversion to ADN occurs directly or indirectly.
  • the conversion may employ an appropriate dehydrating catalyst such as acidic or basic catalysts, including phosphates as disclosed in US 4,237,067 and supported catalysts utilizing Ti, V, Hf or Zr on clays or alumina as disclosed in US 5,587,498.
  • an appropriate dehydrating catalyst such as acidic or basic catalysts, including phosphates as disclosed in US 4,237,067 and supported catalysts utilizing Ti, V, Hf or Zr on clays or alumina as disclosed in US 5,587,498.
  • Such catalysts are typically employed at temperatures of about 220°C to about 350°C at pressures of about 1.172 to 4.37 MPa, for example.
  • dehydration can be achieved thermally as disclosed in US 3,296,303, wherein acids plus an ammonia source are thermally dehydrated in the presence of glycol solvents at temperatures of about 100°C to 130°C at pressures of about 1.03 to about 1.38 MPa.
  • AA, MAA or DAA may be dehydrated directly to ADN or indirectly to ADN by the intermediate ADM. Then, once ADN is produced, it is possible to convert ADN directly to an amine such as HMD or to indirectly convert ADN to HMD through the intermediate ACN.
  • direct conversion from ADN to HMD can be achieved in any number of ways such as disclosed in US 6,376,714 wherein dinitriles in the presence of hydrogen and an ammonia source are converted utilizing catalysts such as Fe, Co, Ni, Rh or Pd promoted with Ru, Cr or W at temperatures of about 50°C to about 150°C at about 2.01 to about 10.34 MPa.
  • catalysts such as Fe, Co, Ni, Rh or Pd promoted with Ru, Cr or W at temperatures of about 50°C to about 150°C at about 2.01 to about 10.34 MPa.
  • US 4,003,933 converts nitriles to amines with hydrogen over a Co/Zr02 catalyst at about 120°C to about 130°C and at about 10.34 MPa.
  • Other catalysts may include Fe, Rh, lr and Pt on Ti0 2 or Zr0 2 .
  • ADN to ACN can be achieved by selecting appropriate hydrogenation conditions such as those disclosed in US 5,151 ,543 wherein nitriles are converted to amino nitriles, in this case ADN to ACN, utilizing Raney catalysts such as Co or Ni promoted with Fe, Cr or Mo with hydrogen and an ammonia source at about 50°C to about 80"C at pressures of 1.72 - 6.89 MPa.
  • Raney catalysts such as Co or Ni promoted with Fe, Cr or Mo
  • an ammonia source at about 50°C to about 80"C at pressures of 1.72 - 6.89 MPa.
  • the amino nitrile or diamino compounds can be co-produced from the dinitriles such as those disclosed in US 7,132,562.
  • US '562 utilizes Fe, Co, Ru, Ni catalysts modified with Cr, V, Ti or Mn at temperatures of about 50°C to about 250°C and 20.68 to 34.47 MPa to achieve high yields and selectivity to the diamine or amino nitrile.
  • the catalysts may also be modified with ordinary P or N with HCN, or CO and hydrogen and an ammonia source.
  • US 3,579,583 discloses the conversion of dicarboxylic acids to amines, particularly alkyl amines, utilizing hydrogen and an ammonia source at temperatures of 200°C to 300°C at pressures of 10.1 to 30.4 MPa in the presence of a Zn-Al 2 0 3 or Zn-Cr catalyst.
  • US 4,935,546 discloses the conversion of acids to amines with hydrogen and an ammonia source in the presence of a Co, Cu or Cr catalyst on a Ti0 2 or AI2O3 support at temperatures of 250°C to 350°C and at pressures of 2 to 15 MPa.
  • Indirect conversion of A A to HMD may also be achieved by hydrogenation of AA to HDO, as shown in Fig. 3.
  • Amination of HDO to HMD can be conducted by the use of a suitable catalyst and an ammonia source.
  • suitable catalysts and reaction conditions for amination of HDO include zirconium, copper and nickel catalysts disclosed in US 6,057,442 and suitable conditions include 80 to 300°C and pressure of 0.1 to 40 MPa.
  • Suitable catalysts and reaction conditions for this pathway are also disclosed in W097/35834 and include contacting HDO and ammonia in the presence of a catalyst, that may include platinum, rhenium, cobalt, molybdenum, nickel, tungsten or palladium.
  • polyamides may be produced from amino nitriles such as ACN.
  • ACN amino nitriles
  • One example of conversions of this type may be found in US 5,109,104 which converts an omega amino nitrile in the presence of an oxygenated phosphorus catalyst with water. This is generally achieved in a several-step conversion at temperatures of 200°C to 330°C and at pressures ranging from 1 .72 to 2.41 MPa.
  • Polyamides may also be formed from the diamines such as HMD wherein the HMD is polymerized with a dicarboxylic acid or ester to form the polyamide.
  • the preferred dicarboxylic acids have a chain length of C4 to C
  • the dicarboxylic acid or ester may be an aromatic dicarboxylic acid or ester or it may be an alkyl dicarboxylic acid.
  • a 1 -L round bottom flask was charged with 800g of a synthetic 4.5% DAA solution.
  • the flask was fitted with a five tray Oldershaw section which was capped with a distillation head.
  • the distillate was collected in an ice cooled receiver.
  • the contents of the flask were heated with a heating mantel and stirred with a magnetic stirrer. Distillation was started and 719.7g of distillate collected. Titration of the distillate revealed it was a 0.29% ammonia solution (i.e. an about 61% conversion of DAA to MAA).
  • the hot residue (76g) was discharged from the flask and placed in an Erlenmeyer flask and slowly cooled to room temperature while stirring over a weekend.
  • This example shows the conversion of MAA to AA.
  • a 300 mL Parr autoclave was charged with 80g of synthetic MAA and 124g of water.
  • the autoclave was sealed and the contents stirred and heated to about 200°C (autogenic pressure was about 203 psig).
  • water was then fed to the autoclave at a rate of about 2 g/min and vapor was removed from the autoclave at a rate of about 2g/min by means of a back pressure regulator.
  • the vapor exiting the autoclave was condensed and collected in a receiver.
  • the autoclave was run under these conditions until a total of 121 Og of water had been fed and a total of 1 185g of distillate collected.
  • the contents of the autoclave (209g) were partially cooled and discharged from the reactor.
  • the slurry was allowed to stand stirring at room temperature over night in an Erlenmeyer flask.
  • the slurry was then filtered and the solids rinsed with 25g of water.
  • the moist soljds were dried in a vacuum oven at 75°C for 1 hr yielding 59g of AA product.
  • Analysis via an ammonium ion electrode revealed 0.015 mmole ammonium ion/g of solid.
  • the melting point of the recovered solid was 151 to 154 U C.
  • This example shows the conversion of DAA to MAA in the presence of a solvent.
  • a beaker was charged with 36.8g of distilled water and 19.7g of concentrated ammonium hydroxide. Then 23.5g of adipic acid was slowly added. The mixture was stirred forming a clear solution which was then placed in a 500 mL round bottom flask which contained a stir bar. Triglyme (8pg) was then added to the flask. The flask was then fitted with a 5 tray 1 " Oldershaw column section which was topped with a distillation head. The distillation head was fitted with an ice bath cooled receiver. The distillation flask was also fitted with an addition funnel which contained 150g of distilled water. The contents were then stirred and heated with a heating mantel.
  • Example 4 shows the conversion of MAA to AA in the presence of a solvent.
  • a beaker was charged with 46.7g of distilled water and 9.9g of concentrated ammonium hydroxide. Then 23.5g of adipic acid was slowly added. The mixture was stirred forming a clear solution which was then placed in a 500 mL round bottom flask which contained a stir bar. Triglyme (80g) was then added to the flask. The flask was then fitted with a 5 tray 1" Oldershaw column section which was topped with a distillation head. The distillation head was fitted with an ice bath cooled receiver. The distillation flask was also fitted with an addition funnel which contained 1800g of distilled water. The contents were then stirred and heated with a heating mantel.
  • the solids were then dried under vacuum at 80°C for 2 hrs yielding 13.5g of solids.
  • the solids were then dissolved in 1 14g of hot water and then cooled to 5°C and held stirring for 45 minutes.
  • the slurry was filtered yielding 13.5g of wet solids and 109.2g of mother liquor.
  • the solids were dried under vacuum at 80°C for 2 hrs yielding 1 1.7g of dried solids.
  • Analysis of the solids revealed an ammonium ion content of 0.01 17 mmol/g (i.e. essentially pure adipic acid).

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Abstract

La présente invention concerne des procédés de production de composés contenant de l'azote, parmi lesquels l'hexanediol (HDO), l'hexaméthylènediamine (HMD), l'adiponitrile (ADN) et l'adipamide (ADM), ainsi que de dérivés de ceux-ci, à partir d'acide adipique (AA) issu de bouillons de fermentation contenant de l'adipate de diammonium (ADA) ou de l'adipate de monoammonium (AMA).
PCT/US2011/050993 2011-06-10 2011-09-09 Procédés de production d'hexanediol (hdo) et d'hexaméthylènediamine (hmd) à partir de bouillons de fermentation contenant de l'acide adipique WO2012170059A1 (fr)

Applications Claiming Priority (2)

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PCT/US2011/039903 WO2011159557A1 (fr) 2010-06-16 2011-06-10 Procédés pour produire de l'hexaméthylènediamine (hmd), de l'adiponitrile (adn), de l'adipamide (adm) et des dérivés de ceux-ci
USPCT/US2011/039903 2011-06-10

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9458480B2 (en) 2009-05-07 2016-10-04 Genomatica, Inc. Microorganisms and methods for the biosynthesis of adipate, hexamethylenediamine and 6-aminocaproic acid

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2223303A (en) * 1939-04-12 1940-11-26 Du Pont Process for the catalytic hydrogenation of carboxylic acid substances to amines
DE2718363A1 (de) * 1977-04-25 1978-10-26 Roehm Gmbh Verfahren zur herstellung von carbonsaeuren aus ihren ammoniumsalzen
US6057442A (en) * 1997-09-29 2000-05-02 Basf Aktiengesellschaft Preparation of amines

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2223303A (en) * 1939-04-12 1940-11-26 Du Pont Process for the catalytic hydrogenation of carboxylic acid substances to amines
DE2718363A1 (de) * 1977-04-25 1978-10-26 Roehm Gmbh Verfahren zur herstellung von carbonsaeuren aus ihren ammoniumsalzen
US6057442A (en) * 1997-09-29 2000-05-02 Basf Aktiengesellschaft Preparation of amines

Non-Patent Citations (1)

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Title
CARNAHAN J E ET AL: "Ruthenium-catalysed hydrogenation of acids to alcohols", JOURNAL OF THE AMERICAN CHEMICAL SOCIETY, AMERICAN CHEMICAL SOCIETY, WASHINGTON, DC; US, vol. 77, no. 14, 1 July 1955 (1955-07-01), pages 3766 - 3768, XP002155956, ISSN: 0002-7863, DOI: 10.1021/JA01619A025 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9458480B2 (en) 2009-05-07 2016-10-04 Genomatica, Inc. Microorganisms and methods for the biosynthesis of adipate, hexamethylenediamine and 6-aminocaproic acid

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