WO2012158182A1 - Procédés pour produire du butanediole et du diaminobutane a partir de bouillons de fermentation contenant du succinate d'ammonium - Google Patents

Procédés pour produire du butanediole et du diaminobutane a partir de bouillons de fermentation contenant du succinate d'ammonium Download PDF

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WO2012158182A1
WO2012158182A1 PCT/US2011/051180 US2011051180W WO2012158182A1 WO 2012158182 A1 WO2012158182 A1 WO 2012158182A1 US 2011051180 W US2011051180 W US 2011051180W WO 2012158182 A1 WO2012158182 A1 WO 2012158182A1
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bottoms
broth
water
dab
solid portion
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PCT/US2011/051180
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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/US2011/036755 external-priority patent/WO2011146440A1/fr
Application filed by Bioamber S.A.S. filed Critical Bioamber S.A.S.
Publication of WO2012158182A1 publication Critical patent/WO2012158182A1/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
    • C07C51/02—Preparation of carboxylic acids or their salts, halides or anhydrides from salts of carboxylic acids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/41—Preparation of salts of carboxylic acids
    • 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
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G69/00—Macromolecular compounds obtained by reactions forming a carboxylic amide link in the main chain of the macromolecule
    • C08G69/02—Polyamides derived from amino-carboxylic acids or from polyamines and polycarboxylic acids
    • C08G69/26—Polyamides derived from amino-carboxylic acids or from polyamines and polycarboxylic acids derived from polyamines and polycarboxylic acids

Definitions

  • This disclosure relates to processes for producing DAB, SDN and DAM from succinic acid (SA) produced by fermentation as well as downstream products.
  • SA succinic acid
  • a material related to MAS can be produced by microorganisms using fermentable carbon sources such as sugars as starting materials.
  • succinate producing microorganisms described in the literature neutralize the fermentation broth to maintain an appropriate pH for maximum, growth, conversion and productivity.
  • the pH of the fermentation broth is maintained at or near a pH of 7 by introduction of ammonium hydroxide imo the broth, thereby converting the SA to dianimonlum succinate- (DAS).
  • DAS dianimonlum succinate-
  • the DAS must be converted to.
  • MAS to derive MAS from the fermentation broth.
  • Kushiki Japanese Patent Application, Publication No.. 2005-139156 discloses -a method of -obtaining MAS from an aqueous solution of DAS that could be obtained from a fermentation broth to which an ammonium salt is -added as a counter ion. Specifically., MAS is crystallized from an aqueous solution of DAS by adding acetic acid to the solution to adjust the pH of the solution to a value between 4.6 and 6.3, causing impure MAS to crystallize from the ' solution,
  • Masuda Japanese Unexamined Application Publication P2007-254354, Oct. 4, 200
  • "ammonium succinate” is diammonium succinate.
  • Masuda removes water and ammonia by heating solutions of the ammonium succinate to yield a solid SA-based composition containing, in addition to .ammonium succinate, at least one of monoarnmomum succinate, succinic acid, monoamide succinate., succinimide, suecinamide or ester succinate.
  • Masuda discloses a process that results in production of impure MAS.
  • the processes of both Kushiki and Masuda lead to materials that need to be subjected to various purification regimes to produce high purity MAS.
  • Bio-derived SA such as that derived from MAS and/or DAS is a platform molecule for synthesis of a number of commercially important chemicals and polymers. Therefore, it is highly desirable to provide a technology that offers flexibility to integrate clear, commercially viable paths from SA to derivatives such as DAB, SDN and DAM and further downstream products.
  • DAB deoxyribonucleic acid
  • SDN succinic amino nitrile
  • DAM succinic amino nitrile
  • We also provide a process for making nitrogen containing compounds including providing a clarified DAS-containing fermentation broth; adding an ammonia separating solvent to the broth; distilling the broth at a temperature and pressure sufficient to form an overhead that includes water and ammonia, and a liquid bottoms that includes SA, and at least about 20 wt% water; cooling the bottoms to a temperature sufficient to cause the bottoms to separate into a liquid portion in contact with a solid portion that is substantially pure SA; separating at least part of the solid portion from the liquid portion; (1) contacting the solid portion with hydrogen and ammonia in the presence of at least one hydrogenation catalyst to produce DAB; or (2) dehydrating at least part of the solid portion to produce SDN; or (3) dehydrating at least part of the solid portion to produce DAM; and recovering the DAB, SDN or DAM.
  • Fig. 1 schematically illustrates a fully integrated process for producing fermentation-derived SA and subsequently converting SA to DAB, SDN and DAM.
  • Fig. 2 schematically illustrates a portion of Fig. 1, shown in greater detail, that provides selected reaction pathways from SA to BDO, DAB, SDN and DAM and other selected downstream products.
  • Fig. 3 is a graph showing the solubility of S A as a function of temperature in both water and a 20 wt% aqueous MAS solution.
  • Fig. 4 schematically illustrates selected reaction pathways from MAS to DAB, SDN and DAM and other selected downstream products.
  • Fig. 5 schematically illustrates selected reaction pathways from DAS to DAB, SDN and DAM and other selected downstream products.
  • FIG. 1 shows in flow diagram form one representative example of a bioprocessing system/process.
  • a growth vessel typically an in-place steam sterilizable fermentor, may be used to grow a microbial culture that is subsequently utilized for the production of the DAS - 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 succinic acids from fermentable carbon sources such as carbohydrate sugars.
  • microorganisms include Escherichia coli (E. coli), Aspergillus niger, Corynebacterium glutamicum (also called Brevibacterium flavum), Enterococcus faecalis, Veillonella parvula, Actinobacillus succinogenes, Mannheimia succiniciproducens, Anaerobiospirillum succiniciproducens, Paecilomyces Varioti, Saccharomyces cerevisiae, Bacteroides fragilis, Bacteroides ruminicola, Bacteroides amylophilus, Alcaligenes eutrophus, Brevibacterium ammoniagenes, Brevibacterium lactofermentum, Candida brumptii, Candida catenulate, Candida mycoderma, Candida zeylanoides, Candida paludigen
  • a preferred microorganism is an E. coli strain deposited at the ATCC under accession number PTA-5132. More preferred is this strain with its three antibiotic resistance genes ⁇ cat, amphl, tetA) removed. Removal of the antibiotic resistance genes cat (coding for the resistance to chloramphenicol), and amphl (coding for the resistance to kanamycin) can be performed by the so-called “Lambda-red ( ⁇ -red)" procedure as described in Datsenko KA and Wanner BL., Proc. Natl. Acad. Sci. U S A 2000 Jun 6; 97(12) 6640-5, the subject matter of which is incorporated herein by reference.
  • tetracycline resistant gene tetA can be removed using the procedure originally described by Bochner et al., J Bacterid. 1980 August; 143(2): 926-933, the subject matter of which is incorporated herein by reference.
  • Glucose is a preferred fermentable carbon source for this microorganism.
  • 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 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 the growth vessel are switched to anaerobic conditions by changing the oxygen-rich gas to an oxygen-deficient gas (e.g., C(1 ⁇ 2 or the like).
  • an oxygen-deficient gas e.g., C(1 ⁇ 2 or the like.
  • the anaerobic environment triggers bioconversion of the fermentable carbon source to succinic acid in situ in the growth vessel.
  • Ammonium hydroxide is provided for pH control during bioconversion of the fermentable carbon source to SA.
  • the SA that is produced is at least partially if not totally neutralized to DAS due to the presence of the ammonium hydroxide, leading to the production of a broth comprising DAS.
  • the C(1 ⁇ 4 provides an additional source of carbon for the production of SA.
  • the contents of the growth vessel may be transferred via a stream to a separate bioconversion vessel for bioconversion of a carbohydrate source to SA.
  • An oxygen-deficient gas e.g., CO 2 or the like
  • Ammonium hydroxide is provided for pH control during bioconversion of the carbohydrate source to SA. Due to the presence of the ammonium hydroxide, the SA produced is at least partially neutralized to DAS, leading to production of a broth that comprises DAS.
  • the C ⁇ 3 ⁇ 4 provides an additional source of carbon for production of SA.
  • the bioconversion may be conducted at relatively low pH (e.g., 3 - 6).
  • a base (ammonium hydroxide or ammonia) may be provided for pH control during bioconversion of the carbohydrate source to SA.
  • SA ammonium hydroxide
  • either SA is produced or the SA produced is at least partially neutralized to MAS, DAS, or a mixture comprising SA, MAS and/or DAS.
  • the SA produced during bioconversion can be subsequently neutralized, optionally in an additional step, by providing either ammonia or ammonium hydroxide leading to a broth comprising DAS.
  • a "DAS-containing fermentation broth” generally means that the fermentation broth comprises DAS and possibly any number of other components such as MAS and/or SA, whether added and/or produced by bioconversion or otherwise.
  • a "MAS-containing fermentation broth” generally means that the fermentation broth comprises MAS and possibly any number of other components such as DAS and/or SA, 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 a stream to a clarification apparatus 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 technique 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, such as ultrafiltration or micro-filtration alone.
  • the resulting clarified DAS-containing broth or MAS-containing broth, substantially free of the microbial culture and other solids, is transferred via a stream to a distillation apparatus.
  • the clarified distillation broth should contain DAS and/or MAS in an amount that is at least a majority of, preferably at least about 70 wt%, more preferably 80 wt% and most preferably at least about 90 wt% of all the diammonium dicarboxylate salts in the broth.
  • concentration of DAS and/or MAS as a weight percent (wt%) of the total dicarboxylic acid salts in the fermentation broth can be easily determined by high pressure liquid chromatography (HPLC) or other known means.
  • Water and ammonia are removed from the distillation apparatus as an overhead, and at least a portion is optionally recycled via a stream to the bioconversion vessel (or the growth vessel operated in the anaerobic mode).
  • 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 MAS 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 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, cyclohexane, methyl cyclohexane, methyl isobutyl ketone, heptane or the like, provided that the bottoms contains at least about 20 wt% water.
  • an organic azeotroping agent such as toluene, xylene, cyclohexane, methyl cyclohexane, methyl isobutyl ketone, heptane or the like.
  • 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 facilitates 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- methylpyrolidone (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)
  • GBL gamma-butyrolactone
  • sulfolane polyethyleneglycol
  • PEG polyethylenegly
  • distillation it is important that the distillation be carried out in a way that ensures that at least some MAS 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 SA 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., Koch-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
  • the distillation bottoms is a liquid, aqueous solution of MAS and SA, 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 a stream to a cooling apparatus and cooled by conventional techniques. Cooling technique is not critical. A heat exchanger (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 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 heat
  • Fig. 3 illustrates the reduced solubility of SA in an aqueous 20 wt% MAS solution at various temperatures ranging from 5°C to 45°C.
  • SA can be more completely crystallized out of an aqueous solution if some MAS is also present in that solution.
  • a preferred concentration of MAS in such a solution is about 20 wt% or higher.
  • the distillation bottoms after cooling, is fed via a stream to a separator 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 and dried, if desired, by standard methods.
  • the liquid portion of the distillation bottoms may contain remaining dissolved SA, any unconverted MAS, any fermentation byproducts such as ammonium acetate, lactate, or formate, and other minor impurities.
  • This liquid portion can be fed via a stream to a downstream apparatus.
  • the downstream apparatus 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 (or the growth vessel 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 can be recycled (or partially recycled) to a distillation apparatus via a stream to further enhance recovery of S A, as well as further convert MAS to SA.
  • the solid portion of the cooling-induced crystallization is substantially pure SA and is, therefore, useful for the known utilities of SA.
  • HPLC can be used to detect the presence of nitrogen-containing impurities such as succinamide and succinimide.
  • the purity of SA can be determined by elemental carbon and nitrogen analysis.
  • An ammonia electrode can be used to determine a crude approximation of SA purity.
  • the fermentation broth may be a clarified MAS-containing fermentation broth or a clarified SA-containing fermentation broth.
  • the operating pH of the fermentation broth may be oriented such that the broth is a MAS- containing broth or a SA-containing broth.
  • MAS, DAS, SA, ammonia, and or ammonium hydroxide may be optionally added to those broths to attain a broth pH preferably less than about 6 to facilitate production of the above-mentioned substantially pure SA.
  • such broth generally means that the fermentation broth comprises MAS and possibly any number of other components such as DAS and/or S A, whether added and/or produced by bioconversion or otherwise.
  • Streams comprising SA, MAS and/or DAS as described above may be converted to selected downstream products such as nitrogen containing compounds including but not limited to DAB, SDN, SAN, DAM and the like as described below.
  • the SA, MAS and/or DAS may be dissolved in water to form an aqueous solution thereof which can be directly fed to the downstream reactor.
  • the SA, MAS or DAS may be converted to SDN, either directly or indirectly through the intermediate DAM by dehydration.
  • dehydrations may be achieved thermally, enzymatically or in the presence of catalysts.
  • appropriate temperatures, pressures and catalysts are selected to achieve the appropriate level of dehydration, depending on whether the conversion to SDN occurs directly or indirectly.
  • the conversion should 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 is 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 is US 5,587,498.
  • Such catalysts are typically employed at temperatures of about 220°C to about 350°C at pressures of about 170 to 600 psig, 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 100°C to 130°C at pressures of 150 to 200 psig.
  • SA, MAS or DAS may be dehydrated directly to SDN or indirectly to SDN by the intermediate DAM. Then, once SDN is produced, it is possible to convert SDN directly to an amine such as DAB or to indirectly convert SDN to DAB through the intermediate SAN.
  • direct conversion from SDN to DAB 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 50°C to 150°C at 300 to 1500 psig. The result is high yields of the diamine, in this case DAB.
  • US 4,003,933 converts nitriles to amines with hydrogen over a Co/Zr0 2 catalyst at 120°C to 130°C and at 1500 psig.
  • Other catalysts may include Fe, Rh, Ir and Pt on Ti0 2 or Zr0 2 .
  • SDN to SAN 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 SDN to SAN, utilizing RANEY catalysts such as Co or Ni promoted with Fe, Cr or Mo with hydrogen and an ammonia source at 50°C to 80°C at pressures of 250 to 1000 psig.
  • RANEY catalysts such as Co or Ni promoted with Fe, Cr or Mo with hydrogen and an ammonia source at 50°C to 80°C at pressures of 250 to 1000 psig.
  • the amino nitrile or diamino compounds can be co-produced from 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 50°C to 250°C and 3000 to 5000 psig 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 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 20 to 150 bar.
  • Indirect conversion of SA to DAB may also be achieved by hydrogenation of SA to 1 ,4-butanediol (BDO), as shown in Fig. 2.
  • BDO ,4-butanediol
  • Amination of BDO to DAB can be conducted by the use of a suitable catalyst and an ammonia source.
  • suitable catalysts and reaction conditions for amination of BDO 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 BDO 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 SAN.
  • 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 250 to 350 psig.
  • Polyamides may also be formed from the diamines such as DAB, wherein the DAB is polymerized with a dicarboxylic acid or ester to form the polyamide.
  • the preferred dicarboxylic acids have a chain length of to
  • the dicarboxylic acid or ester may be an aromatic dicarboxylic acid or ester or it may be an alkyl dicarboxylic acid.
  • ammonium acetate, ammonium lactate and ammonium formate are significantly more soluble in water than SA, and each is typically present in the broth at less than 10% of the DAS concentration.
  • acids acetic, formic and lactic acids
  • SA reaches saturation and crystallizes from solution (i.e., forming the solid portion), leaving the acid impurities dissolved in the mother liquor (i.e., the liquid portion).
  • the pot temperature was recorded as the last drop of distillate was collected.
  • the pot contents were allowed to cool to room temperature and the weight of the residue and weight of the distillate were recorded.
  • the ammonia content of the distillate was then determined via titration. The results were recorded in Tables 1 and 2.
  • This example used a DAS-containing, clarified fermentation broth derived from a fermentation broth containing E. coli strain ATCC PTA-5132.
  • the initial fermentation broth was clarified, thereby resulting in a clarified fermentation broth containing about 4.5% DAS. That clarified broth was used to produce crystalline SA as follows.
  • the broth was first concentrated to approximately 9% using an RO membrane and then subjected to distillation at atmospheric pressure to further concentrate the broth to around 40%.
  • the concentrated broth was used as the starting material for conversion of DAS to SA, carried out batchwise in a 300 ml Parr reactor. A 200 g portion of the solution was reacted at 200°C/200 psig for 11 hours. As the reaction proceeded, water vapor and ammonia liberated from the DAS were condensed and collected overhead. Condensate was collected at about 2 g/min, and makeup water was fed back to the system at approximately the same rate.
  • a 500 mL round bottom flask was charged with 80g of an aqueous 36% DAS solution and 80g of triglyme.
  • the flask was fitted with a 5 tray 1" glass Oldershaw column section which was topped with a distillation head.
  • An addition funnel containing 3300g of water was also connected to the flask.
  • the flask was stirred with a magnetic stirrer and heated with a heating mantel.
  • the distillate was collected in an ice cooled receiver. When the distillate started coming over the water in the addition funnel was added to the flask at the same rate as the distillate was being taken. A total of 3313g of distillate was taken.
  • the distillate contained 4.4g of ammonia, as determined by titration.
  • a pressure distillation column was made using an 8 ft long 1.5" 316 SS Schedule 40 pipe packed with 316 SS Propak packing.
  • the base of the column was equipped with an immersion heater to serve as a reboiler. Nitrogen was injected into the reboiler via a needle valve to pressure.
  • the overhead of the column had a total take-off line which went to a 316 SS shell and tube condenser with a receiver.
  • the receiver was equipped with a pressure gauge and a back pressure regulator. Material was removed from the overhead receiver via blowcasing through a needle valve. Preheated feed was injected into the column at the top of the packing via a pump along with a dilute 0.4% sodium hydroxide solution.
  • Preheated water was also injected into the reboiler via a pump.
  • This column was first operated at 50 psig pressure which gave a column temperature of 150° C.
  • the top of the column was fed a 4.7% DAS containing broth at a rate of 8 mL/min along with 0.15 mL/min of 0.4% sodium hydroxide solution.
  • Water was fed to the reboiler at a rate of 4 mL/min.
  • the overhead distillate rate was taken at 8 mL/min and the residue rate was taken at 4 mL/min.
  • a total of 2565g of broth was fed to the column along with 53g of 0.4% sodium hydroxide solution.
  • a total of 2750g of distillate was taken and 1269g of residue taken during the run.

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Abstract

La présente invention concerne des procédés consistant à fournir un succinate de diammonium (DAS), ou un succinate de mono-ammonium (MAS), clarifié contenant un bouillon de fermentation; à distiller le bouillon d'un distillat de tête qui comprend de l'eau et de l'ammoniac, et un fond liquide qui contient SA, et au moins 20 % en poids d'eau; à refroidir le fond à une température suffisante pour provoquer la séparation du fond en une partie liquide en contact avec une partie solide qui est du SA sensiblement pur; à séparer la partie solide de la partie liquide; et à convertir la partie solide pour produire des composés contenant de l'azote tels que du diaminobutane (DAB), du dinitrile succinique (SDN), de l'aminonitrile succinique (SAN) ou du succinamide (DAM) et des produits en aval.
PCT/US2011/051180 2011-05-17 2011-09-12 Procédés pour produire du butanediole et du diaminobutane a partir de bouillons de fermentation contenant du succinate d'ammonium WO2012158182A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
PCT/US2011/036755 WO2011146440A1 (fr) 2010-05-19 2011-05-17 Procédés de production de diaminobutane (dab), de dinitrile succinique (sdn) et de succinamide (dam)
USPCT/US2011/036755 2011-05-17

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102016220662A1 (de) * 2016-10-21 2018-04-26 Thyssenkrupp Ag Verfahren zur Herstellung wenigstens einer hydrierten Verbindung aus einem Carbonsäurederivat

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102016220662A1 (de) * 2016-10-21 2018-04-26 Thyssenkrupp Ag Verfahren zur Herstellung wenigstens einer hydrierten Verbindung aus einem Carbonsäurederivat

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