Patent Application
20170029353
Ordinarily, the production of diacids such as succinic, malic, maleic and fumaric acid by fermentation of sugar by a microorganism involves recovery the diacid from the fermentation broth by formation of the calcium salt of the diacid, which is not soluble in the aqueous broth. In the case of fermentation by fungi such as Rhizopus oryzae or Asperigillus oryzae, which preferentially make fumaric and malic acid, respectively, the calcium is typically introduced into the broth in the form of CaCO3, which forms Ca(HCO3)2 in solution. The bicarbonate is effective to maintain the pH of the broth as the diacid being produced tends to lower the pH. The diacid is recovered as the calcium salt form. The calcium salts of such C4 diacids have a very low solubility in aqueous solutions (typically less than 3 g/liter at room temperature), and are not suitable for many applications for which the free acid is needed, such as chemical conversion to derivative products like butanediol and the like. Therefore, the calcium salt is typically dissolved in sulfuric acid, forming insoluble calcium sulfate, which can readily be separated from the free diacid. Calcium sulfate is a product having few commercial applications, and accordingly is typically discarded as a solid waste in landfills or other solid waste disposal sites.
In an alternative process described for example in WO2010/147920, instead of using calcium carbonate, the pH of the medium for fungi growth was maintained using a magnesium oxygen containing the bicarbonate salt in aqueous solution. The use of magnesium rather than calcium was found to enhance production of the acid by fermentation. The fermentation was conducted at a pH of 5-8 and more preferably 6.0-7.0. The pH was maintained by the addition of the magnesium oxygen compound, and CO2 was introduced into the medium in combination with the magnesium oxygen compound to maintain a molar fraction of bicarbonate (HCO3−) of at least 0.1 and most preferably at least 0.3 based on the total moles of HCO3−, CO3−2, and CO2 in the medium. At the end of the fermentation, the liquid portion of the medium contained a majority of diacid as a soluble magnesium salt, which was separated from a solids portion of the medium containing precipitated salts and other insoluble material. The dissolved acid salt was converted into the free acid form by reducing the pH to below the isoelectric point of the diacid using a mineral acid such as sulfuric acid, and lowering the temperature of the medium to (most preferably) not greater than 5° C., which precipitated the free acid from the solution.
While useful for producing a free acid, the techniques described for using the magnesium salts results are expensive, first because the magnesium oxygen compounds cost considerably more than the analogous calcium compounds and the bulk of the magnesium remains in the fermentation medium in the form of the magnesium salt of the inorganic acid which is not economically useful for further fermentation or other purposes. Second, the need to lower the temperature of the recovered soluble salts to precipitate the free acid adds additional energy costs.
There is a need in the art therefore, to devise other methods for recovery of diacids from a fermentation media that will produce a diacid product suitable for use in subsequent chemical reactions, while also avoiding the production of calcium and/or magnesium waste products that contribute extra cost to the production of the diacids.
The present disclosure provides, in one aspect, methods of recovery of organic diacids from a fermentation process in a commercially useful form while reducing the accumulation of unusable waste products such as calcium sulfate or unusable forms of magnesium. The method of recovery involves formation and separation of carbonate salts of a divalent metal cation such as calcium or magnesium, which are precipitated and filtered from a fermentation broth while simultaneously forming ammonium salts of the diacid which remain soluble. The recovered metal carbonate precipitate can be reused in the fermentation process rather than discarded as unusable waste. The recovered filtrate containing the solubilized ammonium salts of the diacid can be subsequently processed into free diacids or directly used to make derivative products in single pot reactions or single pot reactions with and intervening removal of ammonium.
In another aspect he disclosure provides for integrated, single pot chemical hydrogenation methods for the synthesis of the commercially valuable solvent N-methyl-2-pyrrolidone (NMP) and the reagents gamma-butyrolactone (GBL) and 1,4-butane-diol (BDO) that are based on hydrogenation of the C4 diacids present in a fermentation broth, recovery of soluble ammonium salts thereof, and reduction of the ammonium salts or free diacids obtained therefrom to the desired compounds. The disclosure therefore provides a bio based alternative to NMP, GBL and BDO synthesis from renewable resources that does not rely on reagents produced from petrochemical sources.
Production and Recovery of Ammonium Diacid Salts from Fermentation Media. The present disclosure provides, in aspect, methods of production and recovery of organic diacids made by a fermentation process in the commercially useful form of ammonium salts, while reducing the accumulation of unusable waste products such as calcium sulfate or unusable forms of magnesium. The organic diacids most suitable for use in the methods of the present disclosure are the C4 diacids, succinic, malic, maleic, and fumaric acid. (Because maleic acid is the cis isomer of fumaric acid any statements herein regarding fumaric acid are equally applicable to maleic acid).
A variety of microorganisms can be used to produce diacids by fermentation. For the production of the C4 diacids, various species of the fungi Asperigillus, especially A. flavus, A. oryzae, and A. sojae are known to produce relatively high titers C4 diacids enriched with malic acid. Various species of the fungi Rhizopus, particularly R. oryzae are also known to produce relatively high titers of C4 diacids enriched with fumaric acid. Of these, the methods described herein have been employed for demonstrative, but not limited purposes, with fermentation media prepared from A. oryzae and R. oryzae.
Bacterial species are also known for production of C4 diacids, especially bacteria of various genera given a species designation “succinogenes,” which are so designated because they are known for producing diacids enriched in succinic acid. These include, for example, Wolinella succinogenes, Fibrobacter succinogenes, and Actinobacillus succinogenes. Of these, the methods described herein have been exemplified with Actinobacillus succinogenes fermentation media that produce a mixture of C4 diacids enriched with succinic acid.
Because all fermentation media, whether for fungi or bacterial fermentations contain similar compositions of nutrients in aqueous solution (e.g., a sugar carbon source, trace salts and vitamins along with divalent cations) and produce similar compositions of C4 diacids, the methods provided herein are applicable to any process that produces C4 diacids by fermentation by any microorganism even though the exact mixtures of C4 diacids produced may differ. Some fermentations, for example, fermentations with Rhizopus or Asperigillus produce small amounts of unwanted by-products such as acetic acid, glycerol, glutaric acid, ethanol and citric acid, however, these by product materials do not interfere with the recovery of the ammonium C4 diacid product or with direct use of the whole recovered clarified medium as a feedstock reagent for subsequent reactions.
Advantageously, the techniques described herein can be practiced for recovery of diacids from whole fermentation media, clarified fermentation media, and purified fermentation media. “Whole fermentation media” means the complete fermentation broth inclusive of cell biomass and constituent nutrients, supplements and fermentation by-products. Example 4 shows that such a whole fermentation broth can be processed to convert a mixture of malate, fumarate and succinate salts to a mixture that has converted at least 96% of the malate and fumarate to diammonium succinate in a single pot series of steps. It is preferable to use whole fermentation media for reasons of cost and yield because the precipitated divalent metal carbonate salt is solid material that is difficult to separate from the particulate biomass of the fermentation media. “Clarified fermentation media,” is the liquid fraction of crude fermentation media remaining after cell biomass and other suspended solids have been removed by filtration, centrifugation or other suitable technique. Example 3 shows recovery of ammonium diacids from a clarified fermentation media. “Purified” fermentation media is a clarified fermentation media that has been subject to at least one step to separate an unwanted component containing fraction from a fraction enriched with diacids. Typical techniques that may be used to obtain a purified fermentation media include, for example, distillation, ion exchange chromatography, electrodialysis, electrodeionization and ultrafiltration.
The methods rely in first part on introduction of sufficient carbonate into the fermentation under a first set of conditions of high temperature and pressure to form a partially insoluble carbonate salt of a divalent metal cation freeing the divalent metal from the diacid. In second part the method relies on the simultaneous formation of an ammonium salt of the diacid which is more soluble than the divalent metal salt of the diacid and much more soluble than the divalent metal carbonate salt. The ammonium salt will dissolve precipitated divalent metal salts of the diacids. Temperature and pressure conditions are then lowered to a second condition (typically standard temperature pressure (STP) i.e. 25° C., 14.7 psi, conditions is sufficient) whereby the metal carbonate salt quantitatively precipitates from the media leaving behind a solubilized fraction containing the ammonium salt of the diacid. The solubilized fraction is separated from the precipitated fraction by filtration or other means, and can be used directly as a reagent feedstock to form derivative products of the C4 diacids.
While the methods are most suitable for the C4 diacids, where the soluble salt is an ammonium salt, the methods are also applicable to separation of any organic acid or diacid produced by fermentation using a substitute salt, where a first physical conditions such as temperature and pressure can be applied so that (i) the carbonate salt of the divalent metal ion is less soluble in an aqueous medium than the corresponding diacid salt of the same metal cation; (ii) the substitute salt of the acid or diacid is at least 10 times more soluble than the divalent metal salt of the diacid under the first conditions;
and (iii) the substitute salt of the diacid remains soluble under a second set of conditions where the carbonate salt of the divalent metal cation is insoluble.
Suitable divalent metal cations for the process include any where the carbonate salt thereof has a solubility in water of less than 0.5 g per liter at 25° C. and a pH of 2 to 4. In preferred practices, the most suitable divalent metal cation is either calcium or magnesium whose carbonate salts have a solubility of approximately 0.02 and 0.4 g/l, respectively. Other functional divalent metal cations may include manganese, iron, cobalt, nickel, copper and zinc. Other functional, but less suitable divalent metal cations may include molybdenum, silver and cadmium. Calcium and magnesium are preferred because of their abundance and their particular suitability for use in alkaline forms as pH control supplements in a fermentation media that is used to produce the diacid in the first place. Moreover, carbonate salts of calcium and magnesium are alkaline and/or can readily be converted to other alkaline forms for re-use in pH control of the fermentation.
In typical practices the amount of divalent metal cation recovered from the fermentation medium is at least 90% of the divalent metal cation that otherwise would form a salt of the diacid while the amount of recovered ammonium salt of the diacid is at least 90% of the amount of diacid subsequently be converted into a soluble alkaline compound of the metal that can be recycled for continued use in the diacid production process by introduction into a new fermentation media to counterbalance the lowering of the pH that occurs during the production of the diacid.
In the methods provided herein, separation of diacids from a fermentation medium relies, in part, on the fact that under a first condition where a source of carbonate is infused into an aqueous media at elevated temperature and pressure a divalent metal cation that otherwise would form a partially or completely insoluble salt of the diacid preferentially complexes with the carbonate to form the divalent metal carbonate salt, while the diacid forms a salt of a substitute cation that remains soluble in the aqueous medium under the first condition. This first condition occurs at a temperature of at least 100° C. and a pressure of at least 200 psig. In one exemplary practice the temperature was 120° C. and the pressure was 200-230 psig. Yet higher temperatures improve solubility of substitute salts of the diacid and of CO2 without substantially increasing of the solubility of the divalent metal carbonate that is formed. In certain exemplary practices, a temperature range of 120° C.-230° C. was used and the carbonate was infused by introducing CO2 at a pressure of 200-500 psig.
In one step, carbonate is introduced into a fermentation medium containing the diacid. The most effective way to introduce the carbonate is by infusion with CO2 under pressure of at least 200 psig at a temperature of at least 120° C. Carbonate can also be introduced by using a partially solubilized carbonate slurry suspension that will further dissolve upon dilution into the medium or by use of a solubilized bicarbonate salt at a pH that will form the carbonate. For example, magnesium or calcium bicarbonate solutions or NH4HCO3, Na2CO3, or NaHCO3 with the medium at a pH of greater than 6 may also be used. The amount of carbonate to introduce should at least be one molar equivalent to the amount of divalent metal cation that is present in the media at the time it is desired to recover the diacids produced. More typically, the amount of carbonate should be between one and two molar equivalents of the amount of divalent metal cation.
The amount of divalent metal cation in turn will be predicated on the amount of diacid produced, or expected to be produced, by the fermentation process. Typically, the amount of divalent metal cation should be about one half to two molar equivalents of the amount of diacid produced or expected to be produced. In exemplary practices the amount of divalent metal cation used was 1.2 to 1.6 molar equivalents to the amount of diacid produced. It is preferable to introduce the divalent metal cation as a soluble salt, for example as calcium bicarbonate, or magnesium sulfate. Some divalent metal cation salts of calcium and magnesium, however, such as calcium carbonate, magnesium carbonate, and magnesium hydroxide are only partially soluble at neutral pH. These materials may be introduced into the medium as partly solubilized slurry in water or as a dry material that will dissolve when diluted into the larger volume of the fermentation medium at the appropriate pH.
For example, in one exemplary practice, when Mg(OH)2 was used to control the pH of fermentation to produce succinic acid from Actinobacillus succinogenes, when the fermentation media began to dip below pH 6.9, a slurry of Mg(OH)2 was added to adjust the pH with the total amount of magnesium added by the end of fermentation being about 1.6 molar equivalents of the amount of succinate produced. In other exemplary practices using Rhizopus oryzae to produce primarily fumarate at an optimal pH of about 5.8, or using Asperigillus oryzae to produce primarily malate at an optimal pH of between 6 and 7, a slurry of CaCO3 was added to the fermentation media when the pH began to lower below these optimal ranges, with the total amount of calcium added by the end of fermentation being about 1.2 to 1.3 molar equivalents of the amount of the total diacids produced.
Depending on the tolerance of the diacid producing organism to low pH, the divalent metal cation can be introduced into the medium before, producing organism has high tolerance to low pH so that production of the diacid does not inhibit fermentation by the microorganism, the divalent metal cation can be introduced after the fermentation is complete. In this case the divalent metal cation can be introduced in any suitable salt form or as an oxide. Suitable salt forms include the carbonate, bicarbonate, hydroxide or halide salts of the divalent metal cation. If the diacid producing microorganisms is inhibited in the fermentation process by low pH, then preferably the divalent metal cation is introduced as an alkaline compound such as in the oxide form or as the bicarbonate or carbonate salt continuously or intermittently during the fermentation process to counter the lowering of pH as mentioned above. If pH control is not important to fermentation yield, then the divalent metal cation may be introduced at any time before, during or after the fermentation process and in any salt form or alkaline form.
In addition to infusing carbonate into the medium, ammonium as the substitute cation for formation of the diacid salt is also introduced into the medium and these conditions are maintained for long enough to equilibrate the formation of soluble ammonium salt of the diacid and the divalent salt of the carbonate. As used herein, “ammonium salt of the diacid” or simply “ammonium diacid” means at least one of a mono ammonium salt of the diacid having one free acid group and one ammonium group, or a diammonium salt of both acid groups. It is important to note that the time for equilibration includes time needed to redissolve divalent cation salts of the diacids that have previously formed and begun to precipitate from the media and to substitute the ammonium ion for the diacid which will maintain the solubility thereof. In exemplary practices, the conditions used for formation of divalent metal cation and substitution to make the diammonium salt of the diacid, were a temperature of at least 100° C., a pressure of at least 200 psig, and a pH of 8 to 11. In particular exemplary practices the temperature was 120° C. to 230° C., the pressure was 200 psig to 500 psig, the pH was 8-9, and the time for equilibration
Ammonia, or any ammonium donating salt may be used in the method, including organic or inorganic ammonium salts. For reasons of subsequent possessing and derivatization of the diacid, it is preferred to use an inorganic ammonium salt, such as ammonium hydroxide, ammonium sulfate or an ammonium halide. It is most preferable to use ammonium hydroxide so as not to introduce any other ions other than H+ and −OH, or introduce other chemically reactive functional groups such as sulfate if it is desired to further perform single pot reactions as described herein after. The amount of ammonium salt will depend on the amount of diacid in the recovered media and the type of ammonium salt desired. If the mono ammonium salt is desired, the amount of ammonium should be about one molar equivalent to the amount of diacid. If the diammonium salt is desired, the amount of ammonium should be at least two molar equivalents to the amount of diacid present. In exemplary practices for forming the diammonium salts of the diacids, 3-4 molar equivalents of ammonium hydroxide was used.
After equilibration under the first condition is reached, the pressure is released and the temperature is lowered to ambient temperature providing a second condition whereby the divalent metal carbonate salt will quantitatively precipitate from the fermentation media while the ammonium salt remains solubilized. In the case of calcium or magnesium the second condition can be a temperature at least as high as room temperature (25° C.), however, depending on concentration of the salts; higher temperatures may also work with prolonged incubation. Temperatures lower than room temperature will also work, provided the temperature is not so low as to cause precipitation of ammonium salt of the diacid, and provided there is not such an excess of the divalent metal cation relative to the ammonium that formation of greater than 10% of the metal salt of the diacid also occurs where the temperature is such that the metal salt of the diacid also precipitates, lowering recovery of the diacid in the form of the soluble ammonium salt.
The precipitated divalent metal carbonate salt is separated from the fermentation medium by any suitable means known in the art such as filtration or centrifugation. In certain embodiments of the method, the separated metal carbonate salt is recovered and either reused as is, or converted to another alkaline form for recycled use in the fermentation process. For example, in one alternative, a slurry of the recovered calcium carbonate can be directly added to a new acidic fermentation media in part dissolving into calcium bicarbonate to raise the pH. In another alternative, the recovered calcium carbonate can first be dissolved in a mineral acid forming calcium bicarbonate directly which can also be used to adjust pH in solution form. In yet another practice, the calcium carbonate can be decomposed to the compound calcium oxide by heating at a temperature of 825° C. or higher, which will liberate CO2 that can be recaptured by compression. The analogous reaction also occurs with magnesium carbonate (MgCO3) which decompose to MgO at even lower temperatures in the range of 250° C.-800 C, with the typical temperature for 100% conversion being about 500° C.-662° C. Calcium oxide and magnesium oxide both convert to their respective hydroxide compounds when dissolved in aqueous media, providing an alternative alkaline compound that can be recycled to the fermentation media for pH control. As yet another alternative practice, magnesium carbonate can also be converted to its water soluble bicarbonate Mg(HCO3)2 by treatment with acid, and the alkaline bicarbonate used to adjust the pH of the fermentation medium.
While it is most desirable to recycle the recovered divalent alkaline compound by use in subsequent rounds of fermentation, as another option, the metal carbonate salt or its alkaline derivatives can be sold for use in other processes, such as for making building materials.
The filtrate or supernatant depleted of the metal carbonate and containing the solubilized ammonium salt of the diacid is also recovered. This ammonium diacid containing fraction can be used directly for further hereafter, or the free diacid or ammonium diacid salt can be further purified. For example, the free acid can be generated by acidifying the media to form the free diacid. The free diacid then can readily be separated from the ammonium ion by ion exchange chromatography or other conventional ion removal process such as electro deionization or electrodialysis. In one practice, the recovered filtrate is concentrated by evaporation into a concentrated liquid or solid product that directly used as a reagent feedstock for further processing.
Reference is made to
In the alternative step 30a using temperature of about 300° C. for about 2 hours the cell mass is converted into an insoluble ash and the calcium compound is in the dried calcium carbonate form as solid materials. In the alternative step 30b using a temperature of at least 825° C. for about 1 hour the calcium carbonate is decomposed into dried calcium oxide solid material with the liberation of carbon dioxide. As an option, at step 35 the calcium carbonate or the calcium oxide can be dissolved in a mineral acid such as HCl forming a solution of calcium bicarbonate and insoluble ash, which if desired, can be separated by filtration. At step 45 any of the recovered oxy calcium materials with or without the ash may be recycled to adjust the pH of fermentation at step 10. In an exemplary practice for production of mixed C4 diacids (fumarate, malate, succinate) by fermentation with Rhizopus oryzae, a slurry of calcium carbonate was used as the pH adjusting compound at step 10.
While illustrated with oxy calcium compounds in
Single Pot Reduction of Ammonium Diacids from Fermentation Media. In a further aspect of this disclosure, the recovered ammonium salts of the C4 diacids produced in a fermentation media are used as an alternative source for making the widely used solvent and reagent N-methyl-2-pyrrolidone (NMP).
NMP and its derivatives are used as intermediates for the synthesis of agrochemicals, pharmaceuticals, textile auxiliaries, plasticizers, stabilizers and specialty inks. It is also employed as a nylon precursor. To make NMP from the ammonium diacid is a one two, three or four step process depending on the diacid moiety, all of which can be conducted in a single reaction vessel without intervening purification of intermediates.
In the case of ammonium succinate, NMP is made in a one or two step process, that includes combining the ammonium succinate with a molar excess of methanol and hydrogen to form a reaction mixture and heating the reaction mixture to a temperature of 200° C. to 300° C., most typically about 230° C., in the presence of a first hydrogenation catalyst for time sufficient to initially form the cyclic diamide N methyl succinamide (NMS, aka. 1-methyl-2,5-pyrrolidinedione). With prolonged incubation times, the NMS is further hydrogenated to NMP according to the reaction sequence illustrated in
In the case of ammonium fumarate (or maleate), NMP is made in a two step process that includes a first hydrogenation step with a first hydrogenation catalyst to reduce the double bond of the fumarate prior to introduction of methanol followed by a second hydrogenation step in the presence of a second hydrogenation catalyst and methanol as shown in
In the case of ammonium malate, NMP is made in a three step process that includes a prior dehydration of the hydoxy group of malate by merely heating the ammonium malate in aqueous solution to a temperature of at least 210° C., which can be done in the absence of a hydrogenation catalyst to form ammonium fumarate in a sequence depicted by
Suitable catalysts for the hydrogenation reactions in any of the foregoing steps include, but are not limited to nickel, (e.g, Raney nickel, G-49B available from Sud Chemie (Louisville, Ky.) which is nickel on kiselghur with a zirconium promoter), ruthenium, e.g. Ru/C, which is ruthenium on a carbons substrate), palladium as in for example palladium on carbon (Pd/C), or copper chromite (Ru/C, Pd/C, Pt/C). It is preferred to use a ruthenium and/or rhodium catalyst for single catalyst hydrogenation reactions. When nickel is used in a multi catalyst hydrogenation sequence, the nickel catalyst is preferably used as the first hydrogenations catalyst for the reduction of the C4 acids to succinate, and the ruthenium and/or rhodium is used for subsequent hydrogenations to produce NMP in the presence of methanol. The hydrogenation reactions typically require infusion under a H2 atmosphere at a pressure of at least 100 psig, most typically between 200-500 psig and at temperatures of greater than 100° C., typically between 120-300° C. for a time sufficient to hydrogenate (reduce) the relevant bonds.
In another further embodiment, the ammonium salts of the diacids are used as an alternative source of making the solvent and reagent 1,4 butanediol (BDO).
BDO can be made by alternative routes, depending on the starting C4 diacid.
When the starting material is predominantly ammonium fumarate and/or ammonium maleate, there are two routes to BDO, each of which requires separation of ammonium from the salt. A first route includes the steps of (i) acidifying the reaction mixture to form the free acid and ammonium, (ii), removing the ammonium by ion exchange, electrodialysis, electrodeionization or other suitable ion removal technique; (ii) adding methanol and an acidic or basic catalyst to form the dimethyl fumarcyl ester; and reducing the dimethyl fumarcyl to BDO by hydrogenation in the presence of a suitable hydrogenation catalyst as illustrated in
A second route for BDO synthesis when the starting material is predominantly ammonium fumarate and/or ammonium maleate is to simultaneously conduct the anion exchange separation of the ammonium ion and methyl esterification of fumarate by contacting the ammonium fumarate with an acidic ion exchange resin over a column in the presence of methanol as illustrated in
Of course, BDO can also be synthesized from ammonium malate using the same two routes mentioned above, except that prior to the ammonium separation or contact with methanol, the malate is converted to fumarate by heat catalyzed dehydration as mentioned herein before for the production of NMP.
The third route for synthesis of BDO can be used when the C4 diacid is primarily ammonium succinate. In this case there is no need to esterify the diacid to the dimethyl ester derivative. Instead, a mineral acid is added in sufficient amounts to form free succinic acid and the ammonium is substituted with H+ by ion exchange, electrodialysis, electrodeionization or other suitable ion removal step, and the succinic acid is directly subject to reductive hydrogenation in the presence of hydrogen with a palladium and/or ruthenium catalyst to form BDO as illustrated in
In other embodiments, butyrolactone (GBL) can also be directly produced from the ammonium succinate.
The route for production of GBL is illustrated in
The examples that follow are provided to illustrate various aspects of the invention and are not intended to limit the invention in any way. One of ordinary skill in the art may use these Examples a guide to practice various aspect of invention with different catalyst or conditions without departing the scope of the invention disclosed.
A mixture of 7.01 g (0.04 mol) of calcium malate and 20 mL of NH4OH (28%) in 150 mL of water, was pressurized under 500 psi of CO2 at room temperature. The reaction mixture was stirred for 2 h while incubated at 120° C. After the reaction, the gas was released and the mixture was cooled to room temperature and a white solid precipitate of calcium carbonate (5.64 g) was formed, which was collected by filtration and dried. The flow-through filtrate was evaporated under vacuum to obtain an oily product, which was ammonium malate (6.11 g). The yield of ammonium malate was 93%, based on the calcium malate.
A sample of 20.28 g (0.12 mol) calcium malate was mixed with 30 mL of NH4OH (28%) in 200 mL of water and charged under 60 psi of CO2 at room temperature. The mixture was stirred for 2 h while incubated at 120° C. and reached a pressure at 180 psi. After the reaction, the gas was released and the mixture was cooled to room temperature and the white solid was filtered out. The flow-through filtrate was evaporated under vacuum to obtain an oily product, which was determined to be ammonium malate (21.76 g). The filter cake was calcium carbonate (11.27 g). The yield of ammonium malate was 96%,based on the calcium malate input.
A clarified fermentation broth of 502.82 g obtained by growing a Rhizopus oryzae on glucose to produce a mixture of fumaric, succinic and malic acid was mixed with 35 ml of NH4OH (28%), and pressurized under 500 psi of CO2 at room temperature. The mixture was stirred for 2 h while incubated at 120° C. After the reaction, the gas was released and the mixture cooled to room temperature and the white solid precipitated (44.87 g) that formed was collected by filtration and determined to be primarily CaCO3 and contained 0.5% of free malic acid and 0.8% of free fumaric acid. The flow-through filtrate was evaporated under vacuum to obtain 54.368 of a light brown solid product, which was determined to be a mixture of ammonium salts, including 65.6% ammonium fumarate, 18% ammonium malate and 15.8% diammonium succinate (DAS).
A whole broth from fermentation of glucose to form C4 diacids by Rhizopus according to Example 6 was obtained. The whole broth contained calcium salts of the diacid, unconsumed glucose, cell biomass and fermentation by-products such as glycerol and acetic acid. Based on analytical results, the whole broth contained 46.9 g/kg fumaric acid, 19.2 g/kg malic acid and 3.3 g/kg of succinic acid (calculated as free acids although present in the form of Ca salts in the broth).
The whole broth (393.87 g) was treated by addition of 73 ml of NH4OH (28%) and infusion with CO2 at 200 psi at a temperature of 80° C. for 2 hours. A nickel catalyst in the form of Raney-nickel or a palladium catalyst on carbon (Pd/C) was added to certain samples of the ammonium treated and carbonated broth as indicated by the table below, which were then heated to a temperature of 120° C. at a pressure of 500 psig of H2 and stirred for a period of 1 hour. On sample did not contain any catalyst. Two samples were further heated to a temperature of 230° C. and stirred for another 2 hours. In one of the 230° C. samples 18 ml of methanol was also added to the hydrogenation mixture. Heating the whole broth under these conditions also affected a kill step on the Rhizopus biomass inactivating further biological processes.
The temperature was reduced to room temperature for a period of 2 hours, and the suspended solid material comprised of calcium carbonate salt and cell biomass was collected by filtration, and the filtrate that contained dissolved diammonium salts of the diacids was recovered and analyzed giving the results shown in Table 1 below:
Based on the content of the starting broth, the results indicated that in even in the absence of a catalyst and at the relatively low temperature of 120° C., greater than 98% of the fumarate and at least and at least 60% of the malate in the medium was converted to diammonium succinate. In the presence of either metal catalyst at a temperature of 230° C. at least 95% of the combined fraction of malate and fumarate were converted into diammonium succinate. In the presence of methanol at 230° C. a substantial portion of diacids were further reduced to NMS and NMP as shown in Table 2.
An evaporated broth from an Actinobaccillus succinogenes fermentation to produce C4 diacids that was converted into ammonium diacid salts from calcium salts was obtained. The evaporated broth, which contained 64% ammonium succinate, 25.4% malic acid, and 10.3% glycerol was mixed with 2.32 g of Raney Nickel and 25 ml of methanol in 200 ml water and heated to 280° C. in an autoclave reactor fitted with temperature and pressure controllers. The air was removed by bubbling hydrogen three times through a dip-tube and the hydrogen was charged at 400 psig at room temperature. The mixture was heated to 280° C. for 2 hours, during which time some hydrogen was consumed. The mixture was stirred for another 6 hours at 280° C. with H2 pressure at 1200 psig. Afterwards, the reactor was cooled to room temperature and the residual hydrogen released. The catalyst was filtered out, the recovered filtrate was evaporated under vacuum to obtain a white solid material that was analyzed and shown to contain 10.36 g/kg of NMS, 12.45 g/kg of NMP, and 3.16 g/kg of diammonium succinate.
A. For Actinobacillus succinogenes, the strain was obtained from Michigan Biotechnology Institute (Lansing, Mich.). The media contained in g/l:
Over the course of the fermentation the pH was adjusted with Mg(OH) totaling 87.5 g/l. The fermentation growth parameters were:
The major byproducts of the fermentation were:
The final titer, yield and productivity of C4 diacids was:
B. For Rhizopus oryzae, the strain was obtained from Archer Daniels Midland Company, Decatur Ill. The media contained in g/l:
Composed of:
Over the course of the fermentation the pH was adjusted with a slurry of CaCO3 totaling 90 g/l. The fermentation growth parameters were:
The major byproducts of the fermentation were:
The final titer, yield and productivity of C4 diacids was:
C For Aspergillus oryzae, the strain was obtained from Novozymes (Washington, D.C.). The media contained in g/l:
Over the course of the fermentation the pH was adjusted with CaCO3 totaling 120 g/l. The fermentation growth parameters were:
The major byproducts of the fermentation were:
The final titer, yield and productivity of C4 diacids was:
This application is a continuation of U.S. patent application Ser. No. 14/233,282 filed Jan. 21, 2014 which is a national stage entry of International Patent application PCT/ US12/45933 which claims benefit of priority from U.S. Provisional Application Nos. 61/510,204 and 61/510,209, each filed Jul. 21, 2011, the contents of which are incorporated herein.
| Number | Date | Country | |
|---|---|---|---|
| 61510204 | Jul 2011 | US | |
| 61510209 | Jul 2011 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 14233282 | Jan 2014 | US |
| Child | 15278649 | US |
