WO2004061114A1 - カラム法によるアミノ酸又はその塩の製造方法及びその製造装置 - Google Patents
カラム法によるアミノ酸又はその塩の製造方法及びその製造装置 Download PDFInfo
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- WO2004061114A1 WO2004061114A1 PCT/JP2003/016636 JP0316636W WO2004061114A1 WO 2004061114 A1 WO2004061114 A1 WO 2004061114A1 JP 0316636 W JP0316636 W JP 0316636W WO 2004061114 A1 WO2004061114 A1 WO 2004061114A1
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- Prior art keywords
- amino acid
- carbonate
- aqueous solution
- eluent
- pressure
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- WTWSHHITWMVLBX-DKWTVANSSA-M sodium;(2s)-2-aminobutanedioate;hydron Chemical compound [Na+].[O-]C(=O)[C@@H](N)CC(O)=O WTWSHHITWMVLBX-DKWTVANSSA-M 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 239000013076 target substance Substances 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
- B01D15/26—Selective adsorption, e.g. chromatography characterised by the separation mechanism
- B01D15/36—Selective adsorption, e.g. chromatography characterised by the separation mechanism involving ionic interaction
- B01D15/361—Ion-exchange
- B01D15/363—Anion-exchange
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
- B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
- B01D15/16—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to the conditioning of the fluid carrier
- B01D15/163—Pressure or speed conditioning
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J41/00—Anion exchange; Use of material as anion exchangers; Treatment of material for improving the anion exchange properties
- B01J41/04—Processes using organic exchangers
- B01J41/05—Processes using organic exchangers in the strongly basic form
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C227/00—Preparation of compounds containing amino and carboxyl groups bound to the same carbon skeleton
- C07C227/38—Separation; Purification; Stabilisation; Use of additives
- C07C227/40—Separation; Purification
Definitions
- the present invention relates to a method for producing an amino acid or a salt thereof by a column method and an apparatus for producing the same.
- the present invention provides a method for producing an amino acid or an amino acid salt from an amino acid-containing aqueous solution using a carbonic acid-type anion exchange resin, a reduction in the amount of by-products generated in an adsorption step or an elution step, and a reduction in the amount of a by-product and an eluate. It relates to a system for collecting and reusing eluent. Background art
- a purification method using an ion-exchange resin is one of the most classic and representative unit operation methods. Since amino acid is an amphoteric electrolyte, either cation exchange resin or anion exchange resin can be used for purification. Generally, the most common case is to use a strongly acidic cation exchange resin.In this case, a fermentation solution adjusted to an appropriate hydrogen ion concentration is passed through a resin tower, and the adsorbed amino acids are eluted and recovered with an aqueous ammonia solution. A common practice is to do this. A typical example is the purification of L-lysine, one of feed amino acids, using a cation exchange resin.
- the ion exchange resin method has advantages such as lower energy cost compared to separation methods such as crystallization separation method and electrodialysis method, and lower equipment cost compared to membrane separation method.
- the ion exchange resin method is roughly divided into an adsorption step and an elution step.
- the adsorption step is an adsorption step for adsorbing the amino acid (AA) to the resin (Resin) (hereinafter, formula (1)).
- the elution step is the amino acid adsorbed on the resin using a predetermined eluent liquid (E). This is the step of eluting the following (formula (2)).
- the ions discharged from the adsorption step The liquid containing non-adsorbed substances on the exchange resin is a flow-through liquid, and is eluted from the eluate; the liquid containing amino acid is called an eluent.
- the first problem with the ion-exchange resin treatment method is that the eluent contains not only the target amino acid but also the eluent, which must be separated. Since the ion exchange reaction is an equilibrium reaction, in order to elute the amino acid from the ion exchange resin, an excess eluent is always required in terms of moles relative to the amount of the amino acid. This can be represented by the following equation (3).
- the excess eluent ((n-1) E in the formula (3)) is mixed into the eluent, it is necessary to separate the amino acid from the eluent after the elution step.
- the eluent is a volatile substance such as an ammonium component, it is easy to remove the excess eluent by simply concentrating the eluent, but if it is a non-volatile salt, it is difficult to separate it. As a result, the entire process became complicated and increased manufacturing costs were inevitable.
- the second problem is the separation of the eluent which is also present in the flow-through.
- the eluent elutes from the ion-exchange resin as well as the non-adsorbed substances in the aqueous solution containing the amino acid, as shown in E on the right side of equation (1). Is done.
- This eluent is usually formed as a by-product by forming salts with non-adsorbed substances in the fermentation liquor. For example, when a lysine fermentation solution is purified using an ammonium component as an eluent with a cation exchange resin, sulfate ions in the fermentation solution are combined with the ammonium component of the eluent to produce ammonium sulfate.
- One method of overcoming such disadvantages of the ion exchange resin method is to use an aqueous solution of carbon dioxide obtained by dissolving carbon dioxide gas in water under a predetermined pressure as an eluent, and using anion exchange resin.
- a method of ion-exchanging adsorbed amino acids is known
- This method has three problems. The first is that in the adsorption step of re-adsorbing the amino acid to the carbonated anion exchange resin after eluting the amino acid, the carbon dioxide gas is bubbled as shown in equations (5) and (6). is there.
- Re-adsorb The normal ion exchange reaction proceeds while repeating this microscopically.However, when an aqueous solution of carbon dioxide in which carbon dioxide gas is dissolved in water is used as the eluent, the concentration of carbonate ions in the eluent is low. The carbonate ions required to re-elute the re-adsorbed amino acids are not always sufficient. As a result, sufficient elution cannot be performed with acidic amino acids.
- Japanese Patent Application Laid-Open No. 5-1393815 discloses that after the ammonia component contained in the aqueous solution is fractionated, A method for obtaining carbon dioxide as gaseous carbon dioxide is disclosed. Disclosure of the invention
- the present invention is to produce and purify an amino acid or a salt thereof from an aqueous solution containing various kinds of neutral, acidic or basic amino acids using an anion-exchange resin, to reduce the amount of by-products generated from an adsorption step or an elution step, and to flow once. It is an object of the present invention to construct a system that can collect the eluent from the liquid and the eluent and reuse it.
- a second aspect of the invention is a method for producing an amino acid or a salt thereof according to the first aspect of the invention, wherein the amino acid contained in the amino acid-containing aqueous solution is an acidic amino acid, a neutral amino acid or a basic amino acid.
- the third aspect of the invention is that the neutral amino acids are cystine, phenylalanine, threonine, tyrosine, serine, tryptophan, titrulline, isoleucine, leucine, no, phosphorus, alanine, proline, glutamine, methionine, glycine, and the acidic amino acid is glutamic acid.
- aspartic acid wherein the basic amino acid is lysine, ornithine, arginine or histidine, the method for producing an amino acid or a salt thereof according to the first or second aspect of the invention,
- a fourth aspect of the present invention is the method for producing an amino acid or a salt thereof according to any one of the first to third aspects of the present invention, wherein the pressurized state is at least 0.1MPa.
- the fifth aspect of the invention is that the eluent liquid is an aqueous solution of carbonic acid and hydrogen carbonate, an aqueous solution of ammonium carbonate, an aqueous solution of hydrogen carbonate, an aqueous solution of ammonium carbonate, an aqueous solution of ammonium hydrogen carbonate, and an aqueous solution of basic hydrogen carbonate for acidic amino acids.
- a sixth aspect of the present invention performs an adsorption step of adsorbing the amino acid in the amino acid-containing aqueous solution to the anion exchange resin and an elution step of eluting the adsorbed amino acid from the anion exchange resin.
- the storage tank (B) has a pressurized facility with air and / or inert gas or carbon dioxide gas, and a line with pulp that regulates the supply of amino acid-containing aqueous solution, eluent solution or water and eluent, etc.
- a seventh aspect of the present invention is the apparatus for producing an amino acid or a salt thereof according to the sixth aspect of the present invention, wherein the amino acid contained in the amino acid-containing aqueous solution is an acidic amino acid, a neutral amino acid or a basic amino acid.
- the neutral amino acid is cystine, phenylalanine, threonine, tyrosine, serine, tryptophan, titrulline, isoleucine, leucine, norin, alanine, proline, glutamine, methionine, glycine, and the acidic amino acid is glutamic acid or glutamic acid.
- a ninth aspect of the present invention is that the eluent liquid is an aqueous solution of carbonic acid and hydrogen carbonate, an aqueous solution of ammonium carbonate, and an aqueous solution of ammonium hydrogencarbonate for neutral amino acids.
- the eleventh aspect of the present invention is to heat the eluent containing a basic amino acid according to the first to fifth aspects of the present invention under atmospheric pressure, if necessary, to reduce excess carbon dioxide component and carbon dioxide in the eluate.
- a basic amino acid-containing aqueous solution is characterized by removing the ammonium component, adding hydrochloric acid in an approximately equimolar amount to the basic amino acid to this, and removing the aqueous solvent of the obtained basic amino acid hydrochloride aqueous solution.
- a second method of the present invention is a method for producing a functional amino acid salt, wherein the free amino acid contained in the amino acid-containing aqueous solution while passing through an amino acid-containing aqueous solution passes through a pressurized pressure-resistant ram filled with a carbonate type anion exchange resin.
- FIG. 1 shows an apparatus for producing an amino acid or a salt thereof by the anion exchange resin method of the present invention.
- FIG. 2 shows an apparatus for recovering an eluent component or an ammonia component as a nitrogen source which is present in an eluent or a flow-through liquid of the present invention.
- FIG. 3 is an elution curve of an acidic amino acid from a carbonate type anion exchange resin.
- FIG. 4 is an elution curve of a neutral amino acid from a carbonate type anion exchange resin.
- FIG. 5 is an elution curve of a basic amino acid from a carbonate type anion exchange resin. ⁇ Explanation of reference numerals>
- the present invention includes the step of adsorbing various amino acids to the carbonate-type anion exchange resin and the step of regenerating the adsorbed amino acid to the carbonate type in parallel with the elution step using an eluent solution. Further, the method includes an elution step of obtaining an eluate containing an amino acid and a production step of concentrating and purifying the eluate to obtain an amino acid or an amino acid salt.
- an amino acid-containing aqueous solution whose hydrogen ion concentration is adjusted as necessary is fed to the pressure-resistant ram, and while the aqueous solution passes through the pressure-resistant ram, the free amino acid contained therein is charged into the pressure-resistant ram.
- the adsorption step is performed in a pressure-resistant ram under pressure.
- the pressure-resistant column is equipped with pressurized equipment that can directly pressurize with gas, use a gas that is almost insoluble in water, such as air, helium, nitrogen, or argon. Pressurize the pressure ram with a pressure of at least 0.1 MPa.
- the pressure may be directly increased to 0.1 MPa or more by using the water pressure of the storage tank without using the gas pressurizing equipment.
- the required water pressure can be maintained by placing the storage tank at a high place or pressurizing the storage tank with gas.
- an amino acid-containing aqueous solution is supplied, and the free amino acid is adsorbed on the anion exchange resin.
- the hydrogen ion concentration of the feed solution needs to be set in a region where the ion form of the amino acid becomes an anion. Hydrogen ion used at this time
- the concentration adjusting liquid is prepared by using ammonia which can be easily recovered from the flow-through liquid as described later. The adjustment of the hydrogen ion concentration is different for various acidic, neutral or basic amino acids.
- the acidic amino acid can be adsorbed on the anion exchange resin without adjusting the hydrogen ion concentration even if the aqueous solution is neutral near pH 7, since the acidic amino acid itself is negatively charged. If necessary, further adjustment of the hydrogen ion concentration with the ammonium component is acceptable.
- Neutral amino acids are not negatively charged when the aqueous solution is at pH 7 for neutral amino acids. Therefore, it cannot be adsorbed on the anion exchange resin as it is. Therefore, an alkali is added to make the neutral amino acid negatively charged.
- aqueous solutions such as sodium hydroxide, potassium hydroxide, and aqueous ammonia can be used.
- the purpose of the present invention is to reduce salts, which are by-products in the flow-through liquid, to recover and reuse the eluent.
- the basic amino acid is not negatively charged when the aqueous solution is at pH 7. Therefore, as in the case of neutral amino acids, an additional force is applied to the negatively charged hydrogen ion concentration.
- the alkali it is preferable to use an aqueous ammonia solution or liquid ammonia.
- the amino acid-containing aqueous solution used in the present invention can be treated not only in the case of a previously purified aqueous solution containing no solidifying salt but also in the case of amino acid fermentation in an unpurified amino acid fermentation solution.
- Aerobic fermentation is carried out by a given production bacterium using an aqueous solution that has been subjected to a predetermined pretreatment such as disinfection and decolorization and hydrogen ion concentration adjustment of the fermentation liquor, as well as sugar sources such as molasses and corn starch, nutrients and inorganic substances as fermentation raw materials. It also includes the amino acid fermentation liquor itself obtained.
- the pressure-resistant ram used in the present invention is made of glass or stainless steel and has a pressure resistance of at least 0.1 IMPa.
- an anion exchange equipped with a temperature controller such as a jacket so that the temperature of the process liquid can be controlled.
- the pressure ram may be equipped with a pressurizing device using a gas almost insoluble in water such as air, helium, nitrogen, or argon to maintain the pressurized state.
- neutral amino acids are cystine, phenylalanine, threonine, tyrosine, serine, tryptophan, titrulline, isoleucine, leucine, valine, alanine, proline, glutamine, methionine, or dalysin
- acidic amino acids are glutamic acid.
- aspartic acid and the like, and the basic amino acid is lysine, arginine, orditin or histidine.
- These amino acids may be in L-form, D-form or racemic form.
- an elution step for eluting an amino acid from the amino acid adsorption resin will be described.
- the eluent solution is adjusted by blowing carbon dioxide gas into a water-filled storage tank and applying a predetermined pressure.
- the eluent is an aqueous solution of ammonium carbonate, this is performed by blowing carbon dioxide gas and ammonia gas into a storage tank filled with water and applying a predetermined pressure, or by blowing carbon dioxide gas into the aqueous ammonia solution and applying a predetermined pressure.
- the eluent liquid water or an aqueous ammonia solution is fed into the storage tank, and then carbon dioxide gas is blown into the storage tank to make the eluent liquid steady.
- the pressure in the storage tank in the steady state is obtained so as to be 0.1 MPa or more. It is desirable to equip the storage tank with a stirrer and a self-circulating pump so that the concentration in the storage tank becomes uniform quickly.
- the temperature is preferably low to increase the solubility of carbon dioxide gas, but care must be taken when amino acids have low solubility.
- the chemical reaction at this time is as shown in equations (7) to (10).
- the neutral amino acid may be an aqueous solution of carbonic acid, an aqueous solution of hydrogencarbonate, an aqueous solution of ammonium carbonate, or an aqueous solution of ammonium hydrogencarbonate.
- An aqueous solution of ammonium carbonate and an aqueous solution of hydrogen carbonate are used, and as the basic amino acid, an aqueous solution of ammonium carbonate and an aqueous solution of hydrogen carbonate are used.
- the amino acid adsorbed on the anion-exchange resin is eluted from the anion-exchange resin using the aqueous solution of carbonic acid, the aqueous solution of hydrogen carbonate, the aqueous solution of ammonium carbonate or the aqueous solution of ammonium hydrogen carbonate.
- the pressure of the pressure-resistant ram is set to 0.1 MPa or more using carbon dioxide gas.However, in order to suppress foaming of the carbon dioxide gas in the pressure-resistant ram, it is preferable that the storage tank store the eluent. It is better to be slightly higher than it.
- Ions contributing to ion exchange are Anion of formula (7) to the equation (1 0) carbonate ions generated in the (C0 3 2 I) and bicarbonate ions (HC0 3 _). The ion exchange reaction at this time is described by a chemical formula as follows.
- AAN is a neutral neutral amino acid residues, AAN-H is free form) eluted
- the solution is a carbonated aqueous solution
- AAN is a neutral amino acid residue and AAN-H is a free neutral amino acid.
- the eluent is an aqueous solution of ammonium bicarbonate
- the eluent is an aqueous solution of ammonium carbonate
- Resin-AAN "+ NH 4 + + HCO3— ⁇ Resin-HCO3— + AAN-NBU (15) (However, AAN is a neutral amino acid residue, and AAN-NH4 is a neutral amino acid ammonium salt.)
- the ionic form of the amino acid upon elution is a mixture of soil and +.
- Basic amino acid (monovalent) carbonate is a mixture of AAB-H and AAB-HCOs.
- the carbonate ion or bicarbonate ion contained in the eluent solution replaces the amino acid in the anion exchange resin. Adsorb. Therefore, the regenerated carbonic acid-type anion exchange resin can be reused as it is in the next adsorption step.
- product amino acids are distributed in free form, so it can be said that it is preferable to use an aqueous solution of carbonic acid as the eluent.
- an aqueous solution of ammonium carbonate is used as the eluent, the amount of carbonate ions in the eluent is large. Therefore, elution efficiency is increased.
- an aqueous solution of ammonium carbonate is used as an eluent.
- An aqueous carbonate solution, an aqueous hydrogen carbonate solution, an aqueous ammonium hydrogen carbonate solution, or an aqueous ammonium carbonate solution is used for the purification of neutral amino acids, and an aqueous ammonium carbonate solution or an aqueous ammonium hydrogen carbonate solution is used for the purification of basic amino acids.
- Fig. 3 shows the elution curve of glutamic acid (GH) eluted from the resin
- Fig. 4 shows the elution curve of phenylalanine (Phe)
- Fig. 5 shows the elution curve of lysine (Lys).
- the eluent liquid amount (R V) had a maximum value with respect to the resin amount, and showed a curve with relatively little tailing. From this, the phenomenon that amino acids adsorbed on the resin are not eluted forever while adsorbed on the resin can be avoided, and it can be said that this method is practically sufficiently valuable.
- the eluent obtained in this way contains eluents such as carbonate ion and bicarbonate ammonium ion.
- the eluate is released to normal pressure and heated if necessary. By concentrating, it can be volatilized and removed as shown in formulas (19) to (22). These can be recycled and reused as eluents and raw materials for fermentation.
- these steps are advantageous because the purity of the amino acid or the salt thereof in the eluate is increased.
- amino acid is glutamic acid in particular, ammonium glutamate (GluNH4) is present in the eluent, so if sodium hydroxide is added to the solution from which the excess eluent has been removed, the following reaction takes place and sodium glutamate (GluNa) is obtained.
- GluNH4 ammonium glutamate
- sodium hydroxide is added to the solution from which the excess eluent has been removed, the following reaction takes place and sodium glutamate (GluNa) is obtained.
- the acidic amino acid-containing aqueous solution obtained by removing the fermentation cells from the L-glutamic acid fermentation broth is adjusted to ⁇ near neutrality and stored in storage tank b.
- Compressed air was fed from the air line d, and the internal pressure of the storage tank b was increased to about 0.2 to 1 MPa.
- water having a temperature of 20 is circulated through the cooling water lines 1, m, j, and k to the jacket in the pressure-resistant ram a and the storage tank b to keep the temperature constant.
- the pump g the feeding of the L-glutamic acid fermentation liquor to the pressure-resistant ram is started.
- Bubbles accumulated at the top of the column were sufficiently displaced, and the pressure-resistant ram a was filled with liquid. Since the amino acid was adsorbed on the anion exchange resin, the valve f was opened, the liquid was started to be drawn from the lower part of the column, and the ion exchange reaction was started. At this time, the pump scale and the opening of the pressure-reducing valve were adjusted so that the internal pressure of the pressure-resistant ram was higher than the normal pressure and 0.1 to IMPa, and the flow rate of the liquid became 0.1 to 2 LZhr. The liquid sending time depends on the capacity of the pressure-resistant ram. The acidic amino acid was adsorbed on the carbonate type anion exchange resin. During the adsorption reaction, no bubbling of carbon dioxide gas occurs in the pressure ram.
- ⁇ Elution Step> An aqueous ammonia solution having a pH of 10 to 13 was placed in the storage tank b. Carbon dioxide gas was also blown into this to prepare an aqueous solution of ammonium carbonate. Cold water is circulated through the jacket of the pressure-resistant column a and the storage tank b to keep the temperature constant, and the feed of the aqueous solution of ammonium carbonate is sent to the pressure-resistant ram a. It is preferable that the internal pressure of the pressure-resistant ram a is 0.1 to 2 MPa, and the flow rate of the liquid is 0.1 to 1 L / hr. Thus, acidic amino acids eluted from the anion exchange resin can be obtained.
- the amount of caustic soda Aqueous sodium hydroxide solution is added to make it equimolar with the L-glutamic acid of the above to neutralize. If necessary, it can be concentrated by heating under vacuum to obtain an acidic amino acid salt.
- the production of neutral amino acids and the configuration of the production apparatus can be performed according to the method described in the production method of acidic amino acids. The different points will be described below.
- An aqueous solution containing a neutral amino acid is adjusted to pH 8 to 13, preferably pH 10 to pH 11 so as to be adsorbed on the anion exchange resin, so that ammonium ions coexisting in the fermentation broth are negatively adjusted.
- the neutral amino acid can be easily adsorbed on the anion exchange resin.
- an aqueous solution of a carbonate ion, an aqueous solution of hydrogen carbonate, an aqueous solution of ammonium carbonate, or an aqueous solution of ammonium hydrogen carbonate can be used as the eluent.
- the above-described apparatus shown in FIG. 1 can be used as it is for the purification and production of neutral amino acids. In the case of neutral amino acids, no salts are formed because they are neutral in the eluent.
- the amino acid is lysine
- lysine is ionized (Lys +) in the eluent, and when hydrochloric acid is added to the solution from which the excess eluent has been removed, the following reaction occurs to give lysine hydrochloride (LysHCl).
- the step of recovering the eluent and the active ingredient from the flow-through liquid will be described.
- the flow-through liquid discharged from the adsorption step was used to adjust the hydrogen ion concentration in the carbonate ions released from the anion-exchange resin, the pH of the bicarbonate and pH adjustment, and in the purification before fermentation and treatment with the ion-exchange resin.
- ammonium components are present and are released to normal pressure, the carbonate is gasified and foams, the ammonia components are also evaporated, and these components hardly exist in the flow-through liquid.
- the ammonia gas component can be distilled and separated by the distillation method disclosed in Japanese Patent Publication No. 55-139,815.
- the carbon dioxide gas volatilized is recovered and used as an eluent, and the volatilized ammonia can be recovered and reused in fermentation and purification before ion-exchange resin treatment. Leads to a reduction in
- the step of recovering the eluent from the eluate will be described.
- the eluent solution is an aqueous solution of ammonium carbonate or ammonium bicarbonate for acidic amino acids, or an aqueous solution of carbonic acid, hydrogen carbonate, aqueous ammonium carbonate or ammonium carbonate for neutral amino acids.
- An aqueous solution of ammonium carbonate or an aqueous solution of ammonium carbonate is used for the process.
- Amino acids adsorbed on the anion-exchange resin are desorbed from the anion-exchange resin by the eluent solution, and at the same time, the anion-exchange resin becomes carbonated by adsorbing carbonate ions or bicarbonate ions present in the eluent solution, resulting in carbon dioxide exchange.
- the resin is regenerated.
- Some unexchanged carbonate ions and ammonium are not adsorbed on the anion exchange resin and pass through the anion exchange resin column as they are. Therefore, carbonate ions, hydrogen carbonate ions and ammonium ions are present as eluent components in the eluent, and these can be recovered and reused in the present invention.
- a pressure-resistant ram a filled with an anion-exchange resin for adsorbing amino acids, a storage tank b for supplying an amino acid-containing aqueous solution thereto, and a fermentation solution and an eluate are transported from the storage tank b.
- Pump g is provided and these are connected by pipeline.
- the pressure proof ram a has a drawing line s for drawing out the flow-through liquid, eluent or washing liquid, a valve f for adjusting the pressure near the outlet of the pressure proof ram a on this line, and a gas above the pressure proof ram a. Line for punching q and valve for its adjustment!
- Reservoir b has fermentation fluid, aqueous ammonia or eluent supply feed o, pressurized air line d, eluent supply line i, and valves c, h, n, which control the supply of material from these lines.
- p a valve e at the outlet of the storage tank to control the pressure and discharge in the storage tank, and a cooling water line 1, m.
- the measurement was performed using a polarized Zeeman primitive absorption spectrophotometer Z-8100 manufactured by Hitachi, Ltd.
- WNH4 () CV ⁇ C VNH4-100 / RV / R VNH4 (25) (However, CV: amount of once-through concentrate (LC VNH 4 ; amount of ammonia in once-through concentrate (g / LRV; once-through liquid) Amount (LR VNH4; amount of ammonium ion in the flow-through liquid (gZL))
- W co 3 (%) CV ⁇ CV C03 ⁇ 1 0 0 / RV / RV co 3 (2 7) ( where, CV; flow concentrate volume (LCV C 3;. Carbonate ion content in the flow-through concentrate (g ZL RV; Flow- through liquid volume (LRV C03 ; Carbonate ion amount in the flow-through liquid (g L)) Calculation of the recoverable amount of carbonate ion R C03 () from the flow-through liquid>
- a strong basic anion exchange resin S A-10A manufactured by Mitsubishi Chemical Corporation was used as the anion exchange resin.
- 0.4 L of a 0.75 mol 1 ZL aqueous sodium hydrogen carbonate solution was passed through the chlorine-type anion exchange resin 0.4 at 1 LZ h for 4 hours to convert the ion exchange resin into a carbonate type. This resin was sufficiently washed with pure water.
- fermentation cells were removed from the liquid feed port o using a microfiltration membrane (microfiltration membrane) at pH 7, and the L-glutamic acid content was 122 g L.
- the valve c was opened, compressed air was fed from the air line d, and the internal pressure of the storage tank was increased to 0.4 MPa.
- the cooling water line Water at a temperature of 20 was circulated through the jacket through k, l, and m to keep the temperature constant.
- the valves e and r were opened, and the pump g was operated to start feeding the L-glutamic acid fermentation liquor to the pressure-resistant ram.
- the bubbles remaining at the top of the column are sufficiently purged using the liquid drain line Q from the top of the column via the valve r, and the inside of the pressure proof ram is filled with liquid.
- the valve r is closed and the pressure reducing valve f By opening, the liquid was started to be drawn from the lower part of the column, and the ion exchange reaction was started.
- the pump graduation and the opening of the pressure reducing valve were adjusted so that the internal pressure of the pressure-resistant ram was 0.5 MPa and the flow rate of the liquid was 0.6 LZ hr.
- the solution was sent for 4 hours, and L-glutamic acid was adsorbed on the carbonate type anion exchange resin. During the adsorption reaction, no foaming of carbon dioxide gas occurred in the pressure-resistant ram, and good adsorption was performed. At this time, a flow-through liquid of 2.4 L / hr was obtained. Cleaning process> Next, the pump g was stopped, and the pressure reducing valve f and the valve e were closed.
- the valve e and the pressure reducing valve f were opened, and the pump g was operated to start sending the aqueous solution of ammonium carbonate.
- the pump scale and the opening of the pressure reducing valve were adjusted so that the internal pressure of the pressure-resistant ram was 0.7 MPa and the flow rate of the liquid was 0.7 L / hr.
- the solution was fed for 2 hours, and L-glutamic acid was eluted from the anion exchange resin to obtain 1.4 L of eluent.
- the L-glutamic acid concentration at this time was 15.7 g.
- ⁇ Deaeration step> The eluate was sent to the deaerator da, and concentrated under reduced pressure until 0.62 L to evaporate and separate dissolved carbon dioxide and ammonia.
- the L-glutamic acid concentration of the obtained eluate concentrate was 35.8 gZL, and the ammonia concentration was 1.9 gZL. Residual ammonium is present as a counterion of L-glutamic acid.
- the separated carbon dioxide gas and ammonia were sent to a separation and recovery device sp and collected. Carbon dioxide gas can be recycled as eluent, and ammonia can be recycled as fermentation raw material, pH adjusting solution, and eluent.
- Example 1 a carbonic acid type strongly acidic anion exchange resin S A-10A 0.4 L manufactured by Mitsubishi Chemical Corporation was used as in Example 1.
- an operation of adsorbing L-phenylalanine to an anion-exchange resin was performed according to Example 1.
- the fermented liquid was subjected to a microfiltration membrane (microfiltration membrane) to remove the cells, and the pH was adjusted to 10 using an aqueous ammonia solution to convert the ionic form of L-phenylalanine into anion form.
- the concentration of L-pheniralanine was 29.7 gZL.
- the feed flow rate to the pressure proof ram was 0.6 LZhr, and the liquid sending time was 2.67 hours.
- the pressure in the storage tank was 0.4 MPa, the pressure in the pressure-resistant column was 0.5 MPa, and the temperature was 20. Through the adsorption reaction, no carbon dioxide gas foaming occurred. At this time, a flow-through liquid of 1.6 LZhr was obtained.
- Elution step> Next, elution of L-phenylalanine from the anion exchange resin was performed.
- the operation procedure is the same as that of Example 1, except that carbon dioxide gas is dissolved in pure water instead of aqueous ammonia solution.
- the flow rate was 1.6 LZhr
- the liquid sending time was 2.25 hours
- the storage tank pressure was 0.5 MPa
- the pressure resistance ram pressure was 0.6 MPa
- the temperature was 25.
- L-phenylalanine was eluted from the anion exchange resin to obtain 3.6 L of eluent.
- the L-phenylalanine concentration at this time was 7. O gZL.
- ⁇ Deaeration step> The eluent was sent to the deaerator da, and the pressure was reduced to 1.8 L to separate dissolved carbon dioxide and ammonia as gases.
- the L-phenylalanine concentration of the obtained eluate concentrate was 14. l gZL.
- the separated carbon dioxide gas and ammonia were sent to the separation and recovery device sp and collected. Carbon dioxide can be recycled as an eluent, and ammonia can be recycled as a raw material for fermentation, a pH adjusting solution, and an eluent.
- Example 1 a carbonic acid type strongly acidic anion exchange resin S A-10 A 0.4 L manufactured by Mitsubishi Chemical Corporation was used as in Example 1.
- An operation of adsorbing L-proline to an anion-exchange resin was performed according to Example 1.
- the ionic form of L-proline was adjusted to an anion form by adjusting the pH to 10 using an aqueous ammonia solution.
- the concentration of L-proline was 106 gZL.
- the feed flow rate to the pressure proof ram was 0.6 LZhr, and the liquid sending time was 2.67 hours.
- the pressure of the storage tank was 0.4 MPa, the pressure of the pressure-resistant ram was 0.5 MPa, and the temperature was 20. No carbon dioxide gas foaming occurred during the adsorption reaction. At this time, a flow-through liquid of 1.6 L / hr was obtained.
- L-proline was eluted from the anion exchange resin. operation The procedure was the same as in Example 2, except that carbon dioxide gas was dissolved in pure water. The flow rate was 1.6 LZhr, the liquid sending time was 3.0 hours, the pressure in the storage tank was 0.5 MPa, the pressure in the pressure-resistant ram was 0.6 MPa, and the temperature was 25 ° C. L-proline was dissolved from the anion exchange resin to obtain 4.8 L of eluent. The L-proline concentration at this time was 8. O g / L.
- ⁇ Deaeration step> The eluate was sent to a deaerator da and concentrated under reduced pressure to 2.4 L to separate dissolved carbon dioxide and ammonia as gases.
- the L-proline concentration of the obtained eluate concentrate was 38.3 gZL.
- the separated carbon dioxide and ammonia were sent to the separation and recovery device sp and collected. Carbon dioxide can be recycled as eluent, and ammonia can be recycled as fermentation feedstock, pH adjusting solution, and eluent.
- ⁇ Adsorption step> An example in which the present invention is applied to an aqueous solution containing L-lysine, which is one of the basic amino acids, will be described.
- L-lysine carbonic acid type strongly acidic anion exchange resin S A-10A 0.4L manufactured by Mitsubishi Chemical Corporation was used as the anion exchange resin.
- An operation of adsorbing L-lysine to an anion-exchange resin was performed according to Example 1.
- the ionic form of L-lysine was adjusted to an anionic form by adjusting the pH to 12 using an aqueous ammonia solution.
- the concentration of L-lysine was 16.7 g // L.
- the feed flow rate to the pressure proof ram was 0.6 L / hr, and the liquid sending time was 3.0 hours.
- the pressure of the storage tank was 0.4 MPa, the pressure of the pressure-resistant ram was 0.5 MPa, and the temperature was 201C. Through the adsorption reaction, no bubbling of carbon dioxide gas occurred. At this time, 1.8 L of flow-through liquid was obtained.
- the operation procedure was the same as in Example 1, except that carbon dioxide gas was dissolved in an aqueous ammonia solution having a hydrogen ion concentration of 11 and used. Flow rate 1.6 LZhr, pumping time 3.0 hours, storage tank pressure 0. The pressure of the pressure-resistant ram was 5 MPa, the pressure was 0.6 MPa, and the temperature was 25. L-lysine was eluted from the anion exchange resin to obtain 4.8 L of eluent. The L-lysine concentration at this time was 3.1 g.
- Degassing step> The eluent was sent to the degassing device da, and concentrated under reduced pressure until the volume became 1.1 L, thereby separating dissolved carbon dioxide and ammonia as gases.
- the eluted concentrate obtained had an L-lysine concentration of 14.4 gZL and a carbonate ion concentration of 1.4 g / L. Residual carbon dioxide exists as carbonate ion and becomes a counter ion of L-lysine.
- the separated carbon dioxide gas and ammonia were sent to a separation and recovery device sp and collected. Carbon dioxide can be recycled as eluent, and ammonia can be recycled as fermentation feedstock, pH adjusting solution, and eluent.
- OIL L-lysine concentration: 14.4 g / L, carbonate ion concentration: 1.4 g / L
- OIL hydrochloric acid
- the solution was neutralized by adding hydrochloric acid.
- the liquid volume of the eluent became 1.111 L.
- This solution was concentrated by heating under vacuum at 86 X: until the solution volume reached 0.30 L to separate carbon dioxide gas.
- An L-lysine hydrochloride aqueous solution having a composition of 5.6 g / L was obtained. The separated carbon dioxide gas was sent to the separation and recovery unit sp and collected.
- the amount of ammonium ion W NH4 (%) in the flow-through liquid was 4.0% from Eq. (24). From the equation ( 24 ), the amount of carbonate ion W C03 (%) in the flow-through liquid was 0.4 %. Therefore, from formula (23), 96.0% of ammonium ions were recovered from the flow-through liquid. On the other hand, from equation (25), 99.6% of the carbonate ion eluted from the anion exchange resin was recovered. Similarly, 99.9% of carbonate ions could be recovered from the eluate by the degassing step described in Example 3. According to the present invention, the removal of impurities from the flow-through liquid, which is waste water, is not only favorable for environmental measures, but also the reduced impurities are reused as an eluent and as a fermentation additive.
- the present invention provides a method for producing an amino acid or an amino acid salt from an amino acid-containing aqueous solution using a carbonic acid type anion exchange resin, reduces the amount of by-products generated from the adsorption step, and elutes from the flow-through liquid and Z or the eluent.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Treatment Of Liquids With Adsorbents In General (AREA)
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP03786290A EP1580277A4 (en) | 2002-12-27 | 2003-12-24 | METHOD FOR THE PRODUCTION OF AMINO ACID OR ITS SALT BY MEANS OF PILLAR METHOD AND PRODUCTION DEVICE THEREFOR |
JP2004564510A JP4400459B2 (ja) | 2002-12-27 | 2003-12-24 | カラム法によるアミノ酸又はその塩の製造方法及びその製造装置 |
AU2003296099A AU2003296099A1 (en) | 2002-12-27 | 2003-12-24 | Process for producing amino acid or its salt by column technique and production appratus therefor |
BRPI0317778-5A BR0317778B1 (pt) | 2002-12-27 | 2003-12-24 | Processo para produzir um aminoácido ou um sal do mesmo |
US11/166,755 US7311836B2 (en) | 2002-12-27 | 2005-06-27 | Process for producing amino acid or salt thereof by column technique and production apparatus thereof |
US11/844,904 US7850852B2 (en) | 2002-12-27 | 2007-08-24 | Process for producing amino acid or salt thereof by column technique and production apparatus thereof |
Applications Claiming Priority (2)
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JP2002-381470 | 2002-12-27 | ||
JP2002381470 | 2002-12-27 |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
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US11/166,755 Continuation US7311836B2 (en) | 2002-12-27 | 2005-06-27 | Process for producing amino acid or salt thereof by column technique and production apparatus thereof |
Publications (1)
Publication Number | Publication Date |
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WO2004061114A1 true WO2004061114A1 (ja) | 2004-07-22 |
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PCT/JP2003/016636 WO2004061114A1 (ja) | 2002-12-27 | 2003-12-24 | カラム法によるアミノ酸又はその塩の製造方法及びその製造装置 |
Country Status (7)
Country | Link |
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US (2) | US7311836B2 (ja) |
EP (1) | EP1580277A4 (ja) |
JP (1) | JP4400459B2 (ja) |
CN (1) | CN100475970C (ja) |
AU (1) | AU2003296099A1 (ja) |
BR (1) | BR0317778B1 (ja) |
WO (1) | WO2004061114A1 (ja) |
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CN102775321A (zh) * | 2012-07-05 | 2012-11-14 | 广东肇庆星湖生物科技股份有限公司 | 一种l-鸟氨酸盐酸盐的提纯方法 |
WO2014020866A1 (ja) * | 2012-08-03 | 2014-02-06 | 味の素株式会社 | 塩基性アミノ酸又は塩基性アミノ酸塩の製造方法 |
CN114082222A (zh) * | 2021-10-25 | 2022-02-25 | 青海大学 | 狭果茶藨子游离氨基酸纯化方法 |
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US9266051B2 (en) | 2005-07-28 | 2016-02-23 | Carbon Sink, Inc. | Removal of carbon dioxide from air |
RU2008139902A (ru) | 2006-03-08 | 2010-04-20 | ГЛОБАЛ РИСЕРЧ ТЕКНОЛОДЖИЗ, ЭлЭлСи (US) | Воздухозаборное устройство с функционализированной ионообменной мембраной для улавливания co2 из внешней среды |
KR20090086530A (ko) * | 2006-10-02 | 2009-08-13 | 글로벌 리서치 테크놀로지스, 엘엘씨 | 공기로부터 이산화탄소를 추출하는 방법 및 장치 |
US8715393B2 (en) | 2007-04-17 | 2014-05-06 | Kilimanjaro Energy, Inc. | Capture of carbon dioxide (CO2) from air |
CN103357389B (zh) * | 2013-07-03 | 2015-04-08 | 中国科学院广州地球化学研究所 | 一种bpha萃淋树脂及利用其分离与富集环境与地质样品中钼的方法 |
CN104211610B (zh) * | 2014-07-31 | 2016-06-15 | 新疆阜丰生物科技有限公司 | 一种谷氨酸钠提取新工艺 |
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CN106699586B (zh) * | 2016-12-08 | 2019-01-25 | 陕西天宇制药有限公司 | 门冬氨酸鸟氨酸的制备方法 |
WO2019161114A1 (en) | 2018-02-16 | 2019-08-22 | Carbon Sink, Inc. | Fluidized bed extractors for capture of co2 from ambient air |
CN110642734A (zh) * | 2019-10-09 | 2020-01-03 | 福州三合元生物科技有限公司 | 一种从泔料中提取氨基酸的方法 |
CN115178074B (zh) * | 2022-07-11 | 2023-08-22 | 沈阳理工大学 | 催化提取污泥氨基酸碳捕集功能肥释放柱及其制法和使法 |
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EP0018028A1 (en) * | 1979-04-16 | 1980-10-29 | Stamicarbon B.V. | Process for the separation of ammonia and carbon dioxide from mixtures containing ammonia, carbon dioxide and water |
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2003
- 2003-12-24 BR BRPI0317778-5A patent/BR0317778B1/pt not_active IP Right Cessation
- 2003-12-24 EP EP03786290A patent/EP1580277A4/en not_active Withdrawn
- 2003-12-24 WO PCT/JP2003/016636 patent/WO2004061114A1/ja active Application Filing
- 2003-12-24 JP JP2004564510A patent/JP4400459B2/ja not_active Expired - Fee Related
- 2003-12-24 CN CNB2003801099777A patent/CN100475970C/zh not_active Expired - Fee Related
- 2003-12-24 AU AU2003296099A patent/AU2003296099A1/en not_active Abandoned
-
2005
- 2005-06-27 US US11/166,755 patent/US7311836B2/en not_active Expired - Fee Related
-
2007
- 2007-08-24 US US11/844,904 patent/US7850852B2/en not_active Expired - Fee Related
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EP0018028A1 (en) * | 1979-04-16 | 1980-10-29 | Stamicarbon B.V. | Process for the separation of ammonia and carbon dioxide from mixtures containing ammonia, carbon dioxide and water |
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Cited By (5)
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CN102775321A (zh) * | 2012-07-05 | 2012-11-14 | 广东肇庆星湖生物科技股份有限公司 | 一种l-鸟氨酸盐酸盐的提纯方法 |
WO2014020866A1 (ja) * | 2012-08-03 | 2014-02-06 | 味の素株式会社 | 塩基性アミノ酸又は塩基性アミノ酸塩の製造方法 |
US9216946B2 (en) | 2012-08-03 | 2015-12-22 | Ajinomoto Co., Inc. | Method of producing basic amino acid or basic amino acid salt |
JP5835489B2 (ja) * | 2012-08-03 | 2015-12-24 | 味の素株式会社 | 塩基性アミノ酸又は塩基性アミノ酸塩の製造方法 |
CN114082222A (zh) * | 2021-10-25 | 2022-02-25 | 青海大学 | 狭果茶藨子游离氨基酸纯化方法 |
Also Published As
Publication number | Publication date |
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CN100475970C (zh) | 2009-04-08 |
EP1580277A1 (en) | 2005-09-28 |
BR0317778A (pt) | 2005-11-22 |
JP4400459B2 (ja) | 2010-01-20 |
EP1580277A4 (en) | 2007-04-18 |
CN1753999A (zh) | 2006-03-29 |
US7311836B2 (en) | 2007-12-25 |
US7850852B2 (en) | 2010-12-14 |
US20050284813A1 (en) | 2005-12-29 |
AU2003296099A1 (en) | 2004-07-29 |
BR0317778B1 (pt) | 2014-09-02 |
US20080039647A1 (en) | 2008-02-14 |
JPWO2004061114A1 (ja) | 2006-05-11 |
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