WO2020217911A1 - 有機溶媒の精製方法及び有機溶媒の精製装置 - Google Patents
有機溶媒の精製方法及び有機溶媒の精製装置 Download PDFInfo
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- 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
- B01J41/08—Use of material as anion exchangers; Treatment of material for improving the anion exchange properties
- B01J41/12—Macromolecular compounds
- B01J41/14—Macromolecular compounds obtained by reactions only involving unsaturated carbon-to-carbon bonds
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J39/00—Cation exchange; Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
- B01J39/04—Processes using organic exchangers
- B01J39/05—Processes using organic exchangers in the strongly acidic form
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- 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
- B01J39/00—Cation exchange; Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
- B01J39/08—Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
- B01J39/16—Organic material
- B01J39/18—Macromolecular compounds
- B01J39/19—Macromolecular compounds obtained otherwise than by reactions only involving unsaturated carbon-to-carbon bonds
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- 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
- B01J39/00—Cation exchange; Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
- B01J39/08—Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
- B01J39/16—Organic material
- B01J39/18—Macromolecular compounds
- B01J39/20—Macromolecular compounds obtained by reactions only involving unsaturated carbon-to-carbon bonds
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- 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
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- 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
- B01J41/07—Processes using organic exchangers in the weakly basic form
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- 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
- B01J45/00—Ion-exchange in which a complex or a chelate is formed; Use of material as complex or chelate forming ion-exchangers; Treatment of material for improving the complex or chelate forming ion-exchange properties
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- 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
- B01J47/00—Ion-exchange processes in general; Apparatus therefor
- B01J47/02—Column or bed processes
- B01J47/026—Column or bed processes using columns or beds of different ion exchange materials in series
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- 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
- B01J47/00—Ion-exchange processes in general; Apparatus therefor
- B01J47/02—Column or bed processes
- B01J47/026—Column or bed processes using columns or beds of different ion exchange materials in series
- B01J47/028—Column or bed processes using columns or beds of different ion exchange materials in series with alternately arranged cationic and anionic exchangers
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- 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
- B01J47/00—Ion-exchange processes in general; Apparatus therefor
- B01J47/02—Column or bed processes
- B01J47/04—Mixed-bed processes
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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
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
- C07C31/02—Monohydroxylic acyclic alcohols
- C07C31/10—Monohydroxylic acyclic alcohols containing three carbon atoms
Definitions
- the present invention relates to a method for purifying an organic solvent for obtaining a high-purity organic solvent having a reduced impurity metal content, and a device for purifying the organic solvent for carrying out the method.
- IPA isopropyl alcohol
- Examples of a method for purifying an organic solvent by removing metal impurities in an organic solvent include a method using an ion exchanger, which is organic by using an ion exchanger having a strongly acidic cation exchange group such as an ion exchange resin or an ion adsorption film. It is known that metal impurities in the solvent can be reduced to the ppt level.
- Patent Document 1 describes a method for producing high-purity isopropanol having a metal content of less than 1 ppb and a water content of less than 100 ppm, wherein (a) isopropyl alcohol is contained in at least 99.9% by weight and 200 to 500 ppm is organic.
- a step of not high-purity isopropyl alcohol having a metal content of less than 1 ppb and a water content of less than 100 ppm (c) a step of obtaining the high-purity isopropyl alcohol as a steam side flow at the following points, (i) the feed flow. Is below the point where is flowing into the separation tower and above the bottom flow, or (ii) above where the supply flow is flowing into the separation tower and is above the head flow. Methods are disclosed that include points below.
- the diffusion rate of metal impurities is low in an organic solvent and the reaction rate of the ion exchange reaction with an ion exchange resin is also low, when removing ionic impurities in an organic solvent, ionic impurities in an aqueous solution are used.
- the liquid passing rate to the ion exchange resin is set to be smaller than that in the case of removing. For example, in the case of treatment using a strongly acidic cation exchange resin, it is difficult to obtain the same metal removal rate at the same flow velocity as in water.
- the present inventors have found that it is difficult to reduce all the metals in a solvent such as IPA by using a strongly acidic cation exchanger, and in particular, there are metals having a poor removal rate such as Cr and As. confirmed.
- an object of the present invention is to provide a purification method and a purification apparatus for an organic solvent having excellent removability of metal impurities for both monovalent and polyvalent metal species in the organic solvent.
- metals having a valence of 2 or more such as Cr have a poor removal rate with a strongly acidic cation exchange resin, and these metals are further examined. Some of them may have an anionic morphology in an organic solvent, and it is effective to use an H-type chelate exchanger to remove these metals.
- H-type chelate exchanger When the H-type chelate exchanger is used, a small amount of mineral acid such as hydrochloric acid present in the H-type chelate exchanger is transferred to the treatment liquid, and the treatment liquid contains the mineral acid derived from the H-type chelate exchanger.
- the monovalent and divalent or higher valent metals in the organic solvent are removed with an H-type strongly acidic cation exchanger, and then further treated with an anion exchanger and an H-type strongly acidic ion exchanger.
- metals such as Cr having an anionic morphology with an anion exchanger and bringing them into contact with a strongly acidic ion exchanger again, monovalent and divalent or higher valent metals that could not be completely removed in the previous stage can be effectively removed.
- the present invention was completed by finding that it can be removed.
- the present invention (1) includes a first treatment step of bringing the organic solvent to be treated into contact with the H-type cation exchanger (1).
- the second treatment step of bringing the treatment liquid of the first treatment step into contact with the anion exchanger (2) and the H-type strongly acidic cation exchanger (3),
- the present invention provides a method for purifying an organic solvent, which is characterized by having.
- the treatment liquid of the first treatment step is passed through a mixed bed of the anion exchanger (2) and the H-type strongly acidic cation exchanger (3).
- the present invention provides a method for purifying an organic solvent according to (1), which comprises performing a treatment step.
- the treatment liquid of the first treatment step is first contacted with the anion exchanger (2) and then with the H-type strongly acidic cation exchanger (3).
- the present invention provides the method for purifying an organic solvent according to (1), which comprises performing the second treatment step.
- the present invention (4) provides a method for purifying an organic solvent according to any one of (1) to (3), wherein the H-type cation exchanger (1) is an H-type chelate exchanger. It is a thing.
- the present invention (5) is a method for purifying an organic solvent according to any one of (1) to (3), wherein the H-type cation exchanger (1) is an H-type strongly acidic cation exchanger. It is to provide.
- the present invention (6) has a treatment step of bringing the organic solvent to be treated into contact with a mixed bed of an H-type chelate exchanger, an anion exchanger (2) and an H-type strongly acidic cation exchanger (3). It provides a method for purifying a characteristic organic solvent.
- the present invention (7) is characterized in that the functional group of the H-type chelate exchanger is an iminodiacetic acid group, an aminomethylphosphate group or an iminopropionic acid group, which is the organic substance of (4) or (6). It provides a method for purifying a solvent.
- the present invention (8) is characterized in that the ratio of the volume of the anion exchanger to the volume of the H-type chelate exchanger is 0.1 to 99.0% by volume (4), (6). ) And (7) for purifying the organic solvent.
- the present invention (9) is characterized in that the ratio of the volume of the cation exchanger (2) to the volume of the H-type chelate exchanger is 0.1 to 99.0% by volume (4).
- (6) to (8) provide a method for purifying an organic solvent.
- the present invention provides a method for purifying an organic solvent according to any one of (1) to (9), wherein the organic solvent is a polar organic solvent.
- the single bed of the H-type cation exchanger (1) through which the organic solvent to be treated is passed and the treatment liquid of the single bed of the H-type cation exchanger (1) are passed.
- an apparatus for purifying an organic solvent which comprises a mixed bed of an anion exchanger (2) and an H-type strongly acidic cation exchanger (3).
- the single bed of the H-type cation exchanger (1) through which the organic solvent to be treated is passed and the treatment liquid of the single bed of the H-type cation exchanger (1) are passed. It is characterized by having a single bed of the anion exchanger (2) and a single bed of the H-type strongly acidic cation exchanger (3) through which the treatment liquid of the single bed of the anion exchanger (2) is passed.
- an apparatus for purifying an organic solvent is provided.
- the present invention (13) is characterized by having a mixed bed of an H-type chelate exchanger, an anion exchanger (2) and an H-type strongly acidic cation exchanger (3) through which an organic solvent to be treated is passed.
- an apparatus for purifying an organic solvent is provided.
- the method for purifying an organic solvent according to the first aspect of the present invention includes a first treatment step of bringing the organic solvent to be treated into contact with the H-type chelate exchanger (1a).
- the first treatment step according to the method for purifying an organic solvent according to the first aspect of the present invention is a step of bringing the organic solvent to be treated into contact with the H-type chelate exchanger (1a).
- the organic solvent to be treated according to the method for purifying an organic solvent according to the first aspect of the present invention is not particularly limited, and is, for example, alcohols such as isopropyl alcohol, methanol and ethanol, cyclohexanenon, methylisobutylketone, acetone and methylethylketone. Ketones such as 2,4-diphenyl-4-methyl-1-pentene, 2-phenyl-1-propene and other alkene-based organic solvents, N-methylpyrrolidone and mixed organic solvents thereof.
- the organic solvent to be treated may be either a polar organic solvent or a non-polar organic solvent, and a polar organic solvent is preferable. Further, the polar organic solvent may be a protonic polar organic solvent and may be an aprotonic organic solvent.
- the organic solvent to be treated is a monovalent metal such as Na, K or Li as a metal impurity and a divalent or higher valent metal such as Cr, As, Ca, Cu, Fe, Mg, Mn, Ni, Pb or Zn. It contains both a metal that is easy to remove with a chelate resin.
- the content of each metal impurity in the organic solvent to be treated is not particularly limited, but is usually about 100 mass ppb to 20 mass ppt.
- the H-type cation exchanger (1) according to the method for purifying an organic solvent according to the first aspect of the present invention is an H-type chelate exchanger (1a).
- the H-type chelate exchanger (1a) is obtained by subjecting a metal ion-type chelate exchanger such as Na-type, Ca-type, or Mg-type to contact with a mineral acid to be acid-treated and converted into H-type. is there. That is, the H-type chelate exchanger (1a) is a mineral acid contact-treated product of the metal ion-type chelate exchanger.
- a metal ion-type chelate exchanger such as Na-type, Ca-type, or Mg-type
- the functional group of the H-type chelate exchanger (1a) is not particularly limited as long as it can coordinate with a metal ion to form a chelate, and for example, an iminodiacetic acid group, an aminomethylphosphate group, and the like.
- examples thereof include a functional group having an amino group such as an iminopropionic acid group, a thiol group and the like.
- a functional group having an amino group is preferable in that a large number of polyvalent metal ions can be easily removed, and an iminodiacetic acid group, an aminomethylphosphate group, and an iminopropionic acid are used. Groups are particularly preferred.
- H-type chelate exchanger (1a) examples include granular H-type chelate exchange resins.
- the substrate of the H-type chelate exchange resin include a styrene-divinylbenzene copolymer.
- the H-type chelate exchange resin may have any of a gel-type structure, a macroporous-type structure, and a porous-type structure.
- the exchange capacity of the H-type chelate exchange resin is preferably 0.5 to 2.5 eq / LR, particularly preferably 1.0 to 2.5 eq / LR.
- the average particle size (harmonic mean diameter) of the H-type chelate exchange resin is not particularly limited, but is preferably 300 to 1000 ⁇ m, and particularly preferably 500 to 800 ⁇ m.
- the average particle size of the H-type chelate exchange resin is a value measured by a laser diffraction type particle size distribution measuring device.
- the H-type organic porous chelate exchanger is an organic porous body into which a functional group having a chelating ability, for example, a functional group having a chelating ability listed above is introduced.
- the exchange capacity in the H-shaped organic porous chelate exchanger is preferably 0.3 to 2 mg equivalent / mL (water-wet state), and particularly preferably 1 to 2 mg equivalent / mL (water-wet state).
- the H-type chelate exchanger (1a) is obtained by contacting a metal ion-type chelate exchanger such as Na-type, Ca-type, or Mg-type with a mineral acid and treating it with an acid.
- a metal ion-type chelate exchanger such as Na-type, Ca-type, or Mg-type
- the mineral acid to be brought into contact with the metal ion-type chelate exchanger include hydrochloric acid, sulfuric acid, and nitric acid. Of these, hydrochloric acid and sulfuric acid are preferable as the mineral acid from the viewpoint of safety. Further, in the case of conversion from Ca form, hydrochloric acid is preferable because there is a risk of precipitation of calcium sulfate.
- the concentration of mineral acid is preferably 0.1 to 6N, particularly preferably 1 to 4N.
- the method of contacting the mineral acid with the metal ion type chelate exchanger is not particularly limited, and the contact mode, contact temperature, contact time, etc. are appropriately selected.
- the H-form chelate exchanger converted to H-form is washed with water to remove excess mineral acid, but the functional groups in the chelate exchanger are Since it is bonded by hydrogen bonds with mineral acids, excess mineral acids cannot be completely removed by washing with water. Therefore, the mineral acid used for the acid treatment remains in the H-type chelate exchanger.
- metal ion type chelate exchange resins CR-10 and CR-11 manufactured by Mitsubishi Chemical Corporation, Duolite C-467 manufactured by Sumika Chemtex Co., Ltd., MC-700 manufactured by Sumitomo Chemical Corporation, and Lanxess Co., Ltd.
- metal ion type chelate exchange resins CR-10 and CR-11 manufactured by Mitsubishi Chemical Corporation, Duolite C-467 manufactured by Sumika Chemtex Co., Ltd., MC-700 manufactured by Sumitomo Chemical Corporation, and Lanxess Co., Ltd.
- the organic solvent to be treated is brought into contact with the H-type chelate exchanger (1a) to treat the organic solvent to be treated with the H-type chelate exchanger (1a), and the organic solvent to be treated is contained in the organic solvent to be treated. It mainly removes divalent or higher valent metals and some monovalent metals.
- the flow rate (SV) when the organic solvent to be treated is passed through the H-type chelate exchanger (1a) is not particularly limited and is appropriately selected, but is preferably 0.1 to 1. It is 100h -1 , particularly preferably 2 to 30h -1 , and even more preferably 4 to 25h -1 .
- the temperature at which the organic solvent to be treated is passed through the H-type chelate exchanger (1a) is not particularly limited and is appropriately selected, but is usually 0 to 50 ° C. Further, depending on the type of the organic solvent to be treated, the organic solvent to be treated may be passed through the H-type chelate exchanger (1a) at 0 to 80 ° C. in the first treatment step.
- the treatment liquid of the first treatment step is brought into contact with the anion exchanger (2) and the H-type strongly acidic cation exchanger (3). It is a process.
- the anion exchanger (2) according to the method for purifying an organic solvent according to the first aspect of the present invention includes a strongly basic anion exchanger (2a) having a strongly basic anion exchange group as an anion exchange group and as an anion exchange group. There is a weakly basic anion exchanger (2b) having a weakly basic anion exchanger.
- Examples of the strongly basic anion exchanging group according to the strongly basic anion exchanger (2a) include an OH-type quaternary ammonium group and the like.
- examples of the weakly basic anion exchanger related to the weakly basic anion exchanger (2b) include a tertiary amino group, a secondary amino group, a primary amino group, a polyamine group and the like.
- Examples of the anion exchange body (2) according to the method for purifying an organic solvent according to the first aspect of the present invention include granular anion exchange resins.
- the substrate of the anion exchange resin is a styrene-divinylbenzene copolymer.
- the anion exchange resin may have any of a gel structure, a macroporous structure, and a porous structure.
- the wet ion exchange capacity of the anion exchange resin is preferably 0.5 to 2 (eq / LR), particularly preferably 0.9 to 2 (eq / LR).
- the harmonic mean diameter of the anion exchange resin is preferably 400 to 900 ⁇ m, particularly preferably 500 to 800 ⁇ m.
- anion exchange resin examples include Amberlite IRA900, 402, 96SB, 98, Amberjet 4400, 4002, 4010 manufactured by Dow Chemical Corporation, Diaion UBA120, PA306S, PA308, PA312, PA316, PA318L manufactured by Mitsubishi Chemical Corporation. WA21J, WA30, DS-2, DS-5, DS-6 manufactured by Organo Corporation, A400, A600, SGA550, A500, A501P, A502PS, A503, A100, A103S, A110, A111S, A133S, Rebatit Co., Ltd. manufactured by Purolite. Monoplus M500, M800, MP62WS, MP64, etc.
- an organic porous anion exchanger is an organic porous body into which an anion exchange group, for example, the strongly basic anion exchange group or the weak basic anion exchange group mentioned above is introduced.
- the exchange capacity in the organic porous anion exchanger is preferably 1 to 6 mg equivalent / mL (dry state), particularly preferably 2 to 5 mg equivalent / mL (dry state).
- the H-type strongly acidic cation exchanger (3) according to the method for purifying an organic solvent according to the first aspect of the present invention is obtained by converting a strongly acidic cation exchange group such as a sulfonic acid group into an H-type.
- H-type strongly acidic cation exchange resin (3) examples include granular strongly acidic cation exchange resins.
- the substrate of the H-type strongly acidic cation exchange resin is a styrene-divinylbenzene copolymer.
- the H-type strongly acidic cation exchange resin may have any of a gel-type structure, a macroporous-type structure, and a porous-type structure.
- the wet ion exchange capacity of the H-type strongly acidic cation exchange resin is preferably 1.5 to 3.0 (eq / LR), particularly preferably 1.7 to 2.7 (eq / LR). Is.
- the harmonic mean diameter of the H-type strongly acidic cation exchange resin is preferably 400 to 900 ⁇ m, particularly preferably 500 to 800 ⁇ m.
- the H-type strongly acidic cation exchange resin include Amberlite IR120B, IR124, 200CT252, Amberjet 1020, 1024, 1060, 1220 manufactured by Dow Chemical Co., Ltd., and Diaion SK104, SK1B, SK110, SK112 manufactured by Mitsubishi Chemical Co., Ltd.
- the H-type organic porous strongly acidic cation exchanger (3) an H-type organic porous strongly acidic cation exchanger can be mentioned.
- the H-type organic porous strong acid cation exchanger is an organic porous body into which a strongly acidic cation exchange group, for example, the strongly acidic cation exchange group mentioned above is introduced.
- the exchange capacity in the H-shaped organic porous strongly acidic cation exchanger is preferably 1 to 3 mg equivalent / mL (dry state), and particularly preferably 1.5 to 3 mg equivalent / mL (dry state).
- the treatment liquid of the first treatment step is brought into contact with the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) to bring the organic solvent to be treated to the anion exchanger (2). And the remainder of the monovalent metal that could not be completely removed by the H-type chelate exchanger (1a) in the first treatment step after treatment with the H-type strongly acidic cation exchanger (3), and the H-type chelate exchanger (1a). ) And the mineral acid released from) are removed. Further, although NaOH is used as a regenerating agent for the regeneration of the anion exchanger, if it is thoroughly washed after the regeneration, NaOH hardly remains in the anion exchanger.
- the H-type strongly acidic cation exchanger (3) in the second treatment step can remove Na.
- the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) to be brought into contact with the liquid to be treated in the second treatment step the above-mentioned cation exchanger and anion exchanger are mixed and used in an arbitrary ratio.
- an ion exchanger sold as a mixture of the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) may be used.
- Examples of the mixed product of the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) include DS-3, DS-7, MSPS2-1 / DRY, EG-4A-HG, and EG- manufactured by Organo. Examples thereof include 5A-HG, ESP-1, ESP-2, AmberTec UP6040 manufactured by DUPONT, MB378, MB378LT, MB400, MB424, MB46, MB47 / 4914 and MB478 manufactured by Purple.
- the flow rate (SV) when the treatment liquid in the first treatment step is passed through the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) is not particularly limited. , But it is preferably 0.1 to 100h -1 , particularly preferably 2 to 50h -1 .
- the temperature at which the treatment liquid in the first treatment step is passed through the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) is not particularly limited and is appropriately selected. However, it is usually 0 to 50 ° C. Further, depending on the type of the organic solvent to be treated, in the second treatment step, the treatment liquid of the first treatment step is applied to the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) at 0 to 80 ° C. Liquid may be passed.
- the anion exchanger (2) when the treatment liquid of the first treatment step is passed through the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) at 60 to 80 ° C., the anion exchanger (2) ),
- the strongly basic anion exchanger (2a) when the strongly basic anion exchanger (2a) is used, the strongly basic anion exchanger (2a) is easily decomposed. Therefore, the weakly basic anion exchanger (2b) is used as the anion exchanger (2). ..
- the method for purifying an organic solvent according to the second aspect of the present invention includes a first treatment step of bringing the organic solvent to be treated into contact with the H-type strongly acidic cation exchanger (1b).
- the second treatment step of contacting the treatment liquid of the first treatment step with the anion exchanger (2) and the H-type strongly acidic cation exchanger (3), It is a method for purifying an organic solvent, which is characterized by having.
- the first treatment step according to the method for purifying an organic solvent according to the second aspect of the present invention is a step of bringing the organic solvent to be treated into contact with the H-type strongly acidic cation exchanger (1b).
- the organic solvent to be treated according to the method for purifying an organic solvent according to the second aspect of the present invention is the same as the organic solvent to be treated according to the method for purifying an organic solvent according to the first aspect of the present invention.
- the H-type cation exchanger (1) according to the method for purifying an organic solvent according to the second aspect of the present invention is an H-type strongly acidic cation exchanger (1b).
- the H-type strongly acidic cation exchanger (1b) according to the method for purifying an organic solvent according to the second aspect of the present invention is an H-type strongly acidic cation exchanger (1b) according to the method for purifying an organic solvent according to the first aspect of the present invention. It is the same as 3).
- the organic solvent to be treated is brought into contact with the H-type strongly acidic cation exchanger (1b), so that the organic solvent to be treated is treated with the H-type strongly acidic cation exchanger (1b) and treated.
- a part of the divalent or higher valent metal and a part of the monovalent metal in the organic solvent are removed.
- the flow rate (SV) when the organic solvent to be treated is passed through the H-type strongly acidic cation exchanger (1b) is not particularly limited and is appropriately selected, but is preferably 0. It is 1 to 100 h -1 , particularly preferably 2 to 30 h -1 .
- the temperature at which the organic solvent to be treated is passed through the H-type strongly acidic cation exchanger (1b) is not particularly limited and is appropriately selected, but is usually 0 to 50 ° C. Further, depending on the type of the organic solvent to be treated, the organic solvent to be treated may be passed through the H-type strongly acidic cation exchanger (1b) at 0 to 80 ° C. in the first treatment step.
- the treatment liquid of the first treatment step is brought into contact with the anion exchanger (2) and the H-type strongly acidic cation exchanger (3). It is a process.
- the anion exchanger (2) according to the method for purifying an organic solvent according to the second aspect of the present invention is the same as the anion exchanger (2) according to the method for purifying an organic solvent according to the first aspect of the present invention.
- the H-type strongly acidic cation exchanger (3) according to the method for purifying an organic solvent according to the second aspect of the present invention is an H-type strongly acidic cation exchanger according to the method for purifying an organic solvent according to the first aspect of the present invention. It is the same as the body (3).
- the H-type strongly acidic cation exchanger (1b) used in the first treatment step and the H-type strongly acidic cation exchanger (3) used in the second treatment step are ,
- the same H-type strongly acidic cation exchanger may be used, or different H-type strongly acidic cation exchangers may be used.
- the treatment liquid of the first treatment step is brought into contact with the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) to bring the organic solvent to be treated to the anion exchanger (2). And the remainder of the divalent or higher valent metal and the monovalent metal that could not be completely removed by the H-type strongly acidic cation exchanger (1b) in the first treatment step after treatment with the H-type strongly acidic cation exchanger (3). Remove the rest. Further, in the second treatment step, the anion exchanger removes metals that may have metal ions in the anion form such as Cr and As, and acids such as mineral acids and organic acids.
- the organic solvent to be treated is once brought into contact with the H-type strongly acidic cation exchanger and then brought into contact with the H-type strongly acidic cation exchanger again.
- the removal rate of the divalent or higher metal becomes higher than in the case where the organic solvent to be treated is brought into contact with the same amount of the H-type strongly acidic cation exchanger.
- the flow rate (SV) when the treatment liquid in the first treatment step is passed through the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) is not particularly limited. , But it is preferably 0.1 to 100 h -1 , particularly preferably 2 to 30 h -1 .
- the temperature at which the treatment liquid in the first treatment step is passed through the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) is not particularly limited and is appropriately selected. However, it is usually 0 to 50 ° C. Further, depending on the type of the organic solvent to be treated, in the second treatment step, the treatment liquid of the first treatment step is applied to the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) at 0 to 80 ° C. Liquid may be passed.
- the anion exchanger (2) when the treatment liquid of the first treatment step is passed through the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) at 0 to 80 ° C., the anion exchanger (2) ),
- the strongly basic anion exchanger (2a) when used, the strongly basic anion exchanger (2a) is easily decomposed. Therefore, the weakly basic anion exchanger (2b) is used as the anion exchanger (2). ..
- Examples of the second treatment step according to the method for purifying an organic solvent according to the first embodiment of the present invention and the second treatment step according to the method for purifying an organic solvent according to the second embodiment of the present invention include the following. ..
- the treatment liquid of the first treatment step is passed through a mixed bed of the anion exchanger (2) and the H-type strongly acidic cation exchanger (3), whereby the second treatment step I do.
- the mixed bed of the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) is composed of a mixture of the anion exchanger (2) and the H-type strongly acidic cation exchanger (3).
- the anion exchanger (2) is an organic porous anion exchanger, a cubic organic porous anion exchanger having a shape cut out to an arbitrary size, for example, a side of about 3 mm to about 10 mm is used.
- the H-type strongly acidic cation exchanger (3) is an organic porous strongly acidic cation exchanger, it has a shape cut out to an arbitrary size, for example, a cubic organic porous strong acid having a side of about 3 mm to about 10 mm.
- a sex cation exchanger is used.
- FIG. 1 An example in which the second treatment step of the method for purifying an organic solvent according to the first embodiment of the present invention or the method for purifying an organic solvent according to the second embodiment of the present invention is the first embodiment is shown in FIG.
- the organic solvent 20 to be treated is first filled with an H-type cation exchanger (H-type chelate exchanger (1a) or H-type strongly acidic cation exchanger (1b)).
- a method of passing the liquid through 2 to obtain the purified organic solvent 23 can be mentioned.
- the range indicated by reference numeral 21 is the first processing step
- the range indicated by reference numeral 22 is the second processing step.
- the treatment liquid of the first treatment step is passed through the single bed of the anion exchanger (2) in the first stage, and then the H-type strongly acidic cation exchanger (3) in the second stage.
- the second treatment step is performed by passing the liquid through a single bed.
- FIG. 2 An example in which the second treatment step of the method for purifying an organic solvent according to the first embodiment of the present invention or the method for purifying an organic solvent according to the second embodiment of the present invention is the second form is shown in FIG. 2, for example.
- the organic solvent 20 to be treated is first filled with an H-type cation exchanger (H-type chelate exchanger (1a) or H-type strongly acidic cation exchanger (1b)). Pass the liquid through 1 and then pass the treatment liquid treated in the H-type cation exchanger filling tower 1 through the anion exchanger filling tower 3 filled with the anion exchanger (2), and then pass the anion exchange.
- H-type cation exchanger H-type chelate exchanger (1a) or H-type strongly acidic cation exchanger (1b)
- a method of passing the treatment liquid treated in the body filling tower 3 through the strongly acidic cation exchanger filling tower 4 filled with the strongly acidic cation exchanger (3) to obtain the purified organic solvent 23 can be mentioned.
- the range indicated by reference numeral 21 is the first processing step
- the range indicated by reference numeral 22 is the second processing step.
- the treatment liquid of the first treatment step is composed of a layer of the anion exchanger (2) in the first stage and a layer of the H-type strongly acidic cation exchanger (3) in the second stage.
- the second treatment step is performed by passing the liquid through the floor.
- the anion exchanger (2) is an organic porous anion exchanger
- the filled container or column is filled with the organic porous anion exchanger cut out to the desired thickness according to the inner diameter of the filling container or column.
- the H-type strongly acidic cation exchanger (3) is an H-type organic porous cation exchanger
- the H-type organic porous cation exchanger is cut out at a desired thickness according to the inner diameter of the filling container or column.
- the body is filled in a filling container or column.
- the organic solvent 20 to be treated is first filled with an H-type cation exchanger (H-type chelate exchanger (1a) or H-type strongly acidic cation exchanger (1b)).
- H-type chelate exchanger (1a) or H-type strongly acidic cation exchanger (1b) The treatment liquid that was passed through 1 and then treated in the H-type cation exchanger packing tower 1 was applied to the layer 5 of the anion exchanger (2) in the first stage and the H-type strongly acidic cation exchanger (3) in the second stage.
- Examples thereof include a method of obtaining a purified organic solvent 23 by passing a liquid through a double bed filling tower 7 filled with the double bed 7 composed of the layer 6.
- the range indicated by reference numeral 21 is the first processing step
- the range indicated by reference numeral 22 is the second processing step.
- the treatment liquid of the first treatment step is a repeating unit of a single bed of the anion exchanger (2) in the first stage and a single bed of the H-type strongly acidic cation exchanger (3) in the second stage.
- the second treatment step is performed by passing the liquid through two or more sets of repeated beds.
- FIG. 4 An example in which the second treatment step of the method for purifying an organic solvent according to the first embodiment of the present invention or the method for purifying an organic solvent according to the second embodiment of the present invention is the fourth form is shown in FIG. 4, for example.
- the organic solvent 20 to be treated is first filled with an H-type cation exchanger (H-type chelate exchanger (1a) or H-type strongly acidic cation exchanger (1b)).
- the treatment liquid that was passed through 1 and then treated in the H-type cation exchanger packing tower 1 was "filled with the anion exchanger (2) in the first stage 8a and the H-type strongly acidic cation exchanger (3) in the latter stage.
- a method of obtaining the purified organic solvent 23 by passing the liquid in the order of "the second repeating unit 10b" is mentioned.
- the range indicated by reference numeral 21 is the first processing step
- the range indicated by reference numeral 22 is the second processing step.
- two repeating units including a filling tower of the anion exchanger (2) in the first stage and a filling tower of the H-type strongly acidic cation exchanger (3) in the second stage are repeated.
- the example is shown, even if the number of repeating units including the filling tower of the anion exchanger (2) in the first stage and the filling tower of the H-type strongly acidic cation exchanger (3) in the second stage is 3 or more. Good.
- the treatment liquid of the first treatment step is subjected to the repeating unit of the layer of the anion exchanger (2) in the first stage and the layer of the H-type strongly acidic cation exchanger (3) in the second stage.
- the second treatment step is performed by passing the liquid through a double bed in which two or more sets are laminated.
- FIG. 5 An example in which the second treatment step of the method for purifying an organic solvent according to the first embodiment of the present invention or the method for purifying an organic solvent according to the second embodiment of the present invention is the fifth form is shown in FIG. 5, for example.
- the organic solvent 20 to be treated is first filled with an H-type cation exchanger (H-type chelate exchanger (1a) or H-type strongly acidic cation exchanger (1b)).
- the treatment liquid that was passed through 1 and then treated in the H-type cation exchanger packing tower 1 was subjected to "the layer 11a of the anion exchanger (2) in the first stage and the H-type strongly acidic cation exchanger (3) in the second stage.
- the first repeating unit 13a composed of the layer 12a and the second repeating unit 13b composed of the layer 11b of the anion exchanger (2) in the first stage and the layer 12b of the H-type strongly acidic cation exchanger (3) in the second stage.
- a method of obtaining a purified organic solvent 23 by passing a liquid through a double-bed filling tower 14 in which the above-mentioned substances are sequentially laminated and filled can be mentioned.
- the range indicated by reference numeral 21 is the first processing step
- the range indicated by reference numeral 22 is the second processing step.
- two repeating units consisting of a layer of the anion exchanger (2) in the first stage and a layer of the H-type strongly acidic cation exchanger (3) in the second stage are repeated.
- the number of repeating units including the layer of the anion exchanger (2) in the first stage and the layer of the H-type strongly acidic cation exchanger (3) in the second stage may be 3 or more.
- the organic solvent to be treated is a mixed bed of an H-type chelate exchanger (1a), an anion exchanger (2) and an H-type strongly acidic cation exchanger (3). It is a method for purifying an organic solvent, which comprises a treatment step (3) of contacting with.
- the organic solvent to be treated is exchanged with an H-type chelate exchanger (1a), an anion exchanger (2) and an H-type strongly acidic cation exchanger. This is a step of contacting the mixed bed of the body (3).
- the organic solvent to be treated, the H-type chelate exchanger (1a), the anion exchanger (2), and the H-type strongly acidic cation exchanger (3) according to the method for purifying an organic solvent according to the third aspect of the present invention are the present invention. This is the same as the organic solvent to be treated, the H-type chelate exchanger (1a), the anion exchanger (2), and the H-type strongly acidic cation exchanger (3) according to the method for purifying the organic solvent of the first embodiment.
- the mixed bed of the H-type chelate exchanger (1a), the anion exchanger (2), and the H-type strongly acidic cation exchanger (3) according to the method for purifying the organic solvent of the third embodiment of the present invention is an H-type chelate exchanger. It consists of a mixture of the body (1a), the anion exchanger (2) and the H-type strongly acidic cation exchanger (3).
- the H-type chelate exchanger (1a) is an H-type organic porous chelate exchanger, it has a shape cut out to an arbitrary size, for example, a cubic H-shaped organic porous body having a side of about 3 mm to about 10 mm. A strong acid chelate exchanger is used.
- the anion exchanger (2) is an organic porous anion exchanger
- a cubic organic porous anion exchanger having a shape cut out to an arbitrary size, for example, a side of about 3 mm to about 10 mm is used.
- the H-type strongly acidic cation exchanger (3) is an organic porous strongly acidic cation exchanger, it has a shape cut out to an arbitrary size, for example, a cubic organic porous strong acid having a side of about 3 mm to about 10 mm.
- a sex cation exchanger is used.
- the organic solvent to be treated is brought into contact with a mixed bed of the H-type chelate exchanger (1a), the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) to be treated.
- the organic solvent is treated with a mixed bed of an H-type chelate exchanger (1a), an anion exchanger (2) and an H-type strongly acidic cation exchanger (3), and a divalent or higher valent metal in the organic solvent to be treated is used. Remove the monovalent metal.
- the anion exchanger (2) removes the mineral acid released from the H-type chelate exchanger (1a) into the organic solvent to be treated.
- the liquid to be treated is passed through the mixed bed of the H-type chelate exchanger (1a), the anion exchanger (2) and the H-type strongly acidic cation exchanger (3).
- the speed (SV) is not particularly limited and is appropriately selected, but is preferably 0.1 to 100 h -1 , particularly preferably 2 to 30 h -1 , and even more preferably 4 to 25 h -1 .
- the organic solvent to be treated is passed through the mixed bed (3) of the H-type chelate exchanger (1a), the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) in the treatment step (3).
- the temperature of the above is not particularly limited and is appropriately selected, but is usually 0 to 50 ° C. Further, depending on the type of the organic solvent to be treated, in the treatment step (3), at 0 to 80 ° C., an H-type chelate exchanger (1a), an anion exchanger (2) and an H-type strongly acidic cation exchanger (3) The organic solvent to be treated may be passed through the mixed bed.
- the organic solvent to be treated is passed through a mixed bed of the H-type chelate exchanger (1a), the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) at 0 to 80 ° C.
- the anion exchanger (2) is easily decomposed, so that the anion exchanger (2) is weak.
- a basic anion exchanger (2b) is used.
- the organic solvent 20 to be treated is an H-type chelate exchanger (1a), an anion exchanger (2) and an H-type.
- examples thereof include a method of obtaining a purified organic solvent 23 by passing the liquid through a mixed bed filling tower 24 filled with a mixture of the strongly acidic cation exchanger (3).
- the range indicated by reference numeral 25 is the processing step (3).
- the ratio of the volume of the anion exchanger (2) to the volume of the H-type chelate exchanger (1a). ((Volume of anion exchanger (2) / Volume of H-type chelate exchanger (1a)) ⁇ 100) is preferably 0.1 to 99.0% by volume, more preferably 0.1 to 70.0 volumes. %, Especially preferably 0.1 to 50.0% by volume.
- the volume of the strongly acidic cation exchanger (3) relative to the volume of the H-type chelate exchanger (1a). ((Volume of strongly acidic cation exchanger (3) / Volume of H-type chelate exchanger (1a)) ⁇ 100) is preferably 0.1 to 99.0% by volume, more preferably 0.1 to It is 70.0% by volume, particularly preferably 0.1 to 50.0% by volume.
- Ion exchangers are introduced as the H-type cation exchanger (H-type chelate exchanger (1a), strongly acidic cation exchanger (1b)), anion exchanger (2) and H-type strongly acidic cation exchanger (3).
- the substrate to be formed may be an organic porous body.
- the organic porous material according to the present invention will be described below.
- An H-type chelate exchange group, a strongly acidic cation group or an anion exchange group is introduced into the organic porous ion exchanger. That is, the one in which the H-type chelate exchange group is introduced into the organic porous body is the H-type organic porous chelate exchanger (1a), and the H-type strongly acidic cation exchange group is introduced into the organic porous body.
- the H-type organic porous strongly acidic cation exchanger (1b) or (3) Is an H-type organic porous strongly acidic cation exchanger (1b) or (3), and an organic porous body having an anion exchange group introduced is organic porous. It is an anion exchanger.
- the functional groups introduced into the organic porous ion exchanger are the above-mentioned (H-type chelate exchanger (1a), strongly acidic cation exchanger (1b)), anion exchanger (2) or H-type strongly acidic. It is the same as the functional group introduced into the cation exchanger (3).
- the organic porous ion exchanger is composed of, for example, a continuous skeleton phase and a continuous pore phase, the thickness of the continuous skeleton is 1 to 100 ⁇ m, the average diameter of the continuous pores is 1 to 1000 ⁇ m, and the total pore volume is 0.5. It is ⁇ 50 mL / g, an ion exchange group (chelate exchange group, H-type strongly acidic cation exchange group or anion exchange group) is introduced, and the ion exchange capacity per weight in the dry state is 1 to 6 mg equivalent / g.
- examples thereof include an organic porous ion exchanger in which ion exchange groups are uniformly distributed in the organic porous ion exchanger (hereinafter, also referred to as an organic porous ion exchanger of the first form).
- the organic porous ion exchanger of the first form has an open cell structure in which bubble-shaped macropores overlap each other and the overlapping portion has an opening with an average diameter of 1 to 1000 ⁇ m, and the total pore volume is 1 to 50 mL. / G, the ion exchange group is introduced, the ion exchange capacity per weight in the dry state is 1 to 6 mg equivalent / g, and the ion exchange group is uniformly distributed in the organic porous ion exchanger. Examples thereof include organic porous ion exchangers.
- the organic porous ion exchanger of the first form is a continuous macropore structure in which bubble-shaped macropores overlap each other and the overlapping portion has an opening with an average diameter of 30 to 300 ⁇ m, and the total pore volume is 0. .5 to 10 ml / g, cation exchange group or anion exchange group is introduced, the ion exchange capacity per weight in the dry state is 1 to 6 mg equivalent / g, and the ion exchange group is an organic porous ion exchanger.
- organic porous ion exchanger of the first form all of the organic porous ion exchangers into which ion exchange groups (chelate exchange groups, H-type strongly acidic cation exchange groups or anion exchange groups) have been introduced.
- a three-dimensionally continuous skeleton composed of an aromatic vinyl polymer containing 0.1 to 5.0 mol% of crosslinked structural units in the structural units and having an average thickness of 1 to 60 ⁇ m, and an average diameter of 10 between the skeletons. It is a co-continuous structure consisting of three-dimensionally continuous pores of up to 200 ⁇ m, has a total pore volume of 0.5 to 10 mL / g, has a cation exchange group introduced, and weighs in a dry state. Examples thereof include an organic porous ion exchanger in which the ion exchange capacity per unit is 1 to 6 mg equivalent / g and the ion exchange groups are uniformly distributed in the organic porous ion exchanger.
- the purified organic solvent obtained by performing the method for purifying an organic solvent according to the first embodiment of the present invention the method for purifying an organic solvent according to the second embodiment of the present invention, and the method for purifying an organic solvent according to the third embodiment of the present invention.
- the content of each metal is appropriately selected depending on the use of the organic solvent after purification, and all of them are preferably 10 mass ppt or less. That is, a purified organic solvent obtained by performing the method for purifying an organic solvent according to the first embodiment of the present invention, the method for purifying an organic solvent according to the second embodiment of the present invention, and the method for purifying an organic solvent according to the third embodiment of the present invention.
- each metal having a valence of 2 or more is appropriately selected depending on the use of the organic solvent after purification, and all of them are preferably 10 mass ppt or less, and the content of the monovalent metal is after purification. It is appropriately selected depending on the use of the organic solvent, and all of them are preferably 10 mass ppt or less.
- the method for purifying the organic solvent of the first embodiment of the present invention, the method for purifying the organic solvent of the second embodiment of the present invention, and the method for purifying the organic solvent of the third embodiment of the present invention 1 mass ppt Since the following impurity levels can be purified, the method for purifying the organic solvent of the first embodiment of the present invention, the method for purifying the organic solvent of the second embodiment of the present invention, and the organic solvent of the third embodiment of the present invention can be performed.
- the purified organic solvent obtained by the purification method of is the solvent for diluting the standard solution (blank solution for calibration line) used for preparing the calibration line for trace metal analysis, the solvent for diluting the sample, and the instruments and analyzers. It is preferably used as a cleaning solvent.
- the organic solvent purification apparatus of the first aspect of the present invention comprises a single bed of the H-type cation exchanger (1) through which the organic solvent to be treated is passed and a single bed of the H-type cation exchanger (1). It is an organic solvent purification apparatus characterized by having a mixed bed of an anion exchanger (2) and an H-type strongly acidic cation exchanger (3) through which a treatment liquid is passed.
- Examples of the flow of the organic solvent purification apparatus of the first aspect of the present invention include the embodiment shown in FIG.
- the organic solvent purification apparatus of the second embodiment of the present invention comprises a single bed of the H-type cation exchanger (1) through which the organic solvent to be treated is passed and a single bed of the H-type cation exchanger (1).
- Examples of the flow of the organic solvent purification apparatus of the second aspect of the present invention include the embodiment shown in FIG.
- the organic solvent purification apparatus of the third aspect of the present invention comprises a single bed of the H-type cation exchanger (1) through which the organic solvent to be treated is passed and a single bed of the H-type cation exchanger (1).
- An organic solvent purification apparatus characterized by having a double bed composed of a layer of an anion exchanger (2) in the first stage and a layer of an H-type strongly acidic cation exchanger (3) in the second stage through which the treatment liquid is passed. Is.
- Examples of the flow of the organic solvent purification apparatus of the third aspect of the present invention include the embodiment shown in FIG.
- Examples of the organic solvent purification apparatus of the first to third embodiments of the present invention include an organic solvent purification apparatus in which the H-type cation exchanger (1) is an H-type chelate exchanger.
- examples of the organic solvent purification apparatus of the first to third embodiments of the present invention include an organic solvent purification apparatus in which the H-type cation exchanger (1) is an H-type strongly acidic cation exchanger.
- the organic solvent purification apparatus of the fourth aspect of the present invention is a mixed bed of an H-type chelate exchanger, an anion exchanger (2), and an H-type strongly acidic cation exchanger (3) through which the organic solvent to be treated is passed. It is an organic solvent purification apparatus characterized by having.
- Examples of the flow of the organic solvent purification apparatus according to the fourth aspect of the present invention include the example shown in FIG.
- Examples of the organic solvent purification apparatus according to the fourth aspect of the present invention include an organic solvent purification apparatus in which the H-type cation exchanger (1) is an H-type chelate exchanger.
- the H-type cation exchanger (1), the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) according to the organic solvent purification apparatus of the first to fourth aspects of the present invention are the first of the present invention. This is the same as the H-type cation exchanger (1), the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) according to the methods for purifying the organic solvent of the first to third forms.
- the H-type cation exchanger (1) is an H-type chelate exchanger
- anion exchange with respect to the volume of the H-type chelate exchanger (1a) is preferably 0.1 to 99.0% by volume, more preferably. It is 0.1 to 70.0% by volume, particularly preferably 0.1 to 50.0% by volume.
- the H-type cation exchanger (1) when the H-type cation exchanger (1) is an H-type chelate exchanger, it is strongly acidic with respect to the volume of the H-type chelate exchanger (1a).
- the volume ratio of the cation exchanger (3) ((volume of the strongly acidic cation exchanger (3) / volume of the H-type chelate exchanger (1a)) ⁇ 100) is preferably 0.1 to 99.0% by volume. , More preferably 0.1 to 70.0% by volume, and particularly preferably 0.1 to 50.0% by volume.
- the first treatment step and the second treatment step are carried out using two or more connected filling towers, but the floor on which the first treatment step is performed is filled in the previous stage and then.
- a double bed filled with a floor to be subjected to the second treatment step may be formed on the stage, and the first treatment step and the second treatment step may be carried out using one filling tower.
- An example of a form consisting of a floor can be mentioned.
- the first treatment step is carried out on the bed of the H-type chelate exchanger (1a) in the first stage
- the second treatment is carried out on the mixed bed of the anion exchanger (2) and the H-type strongly acidic cation exchanger (3) in the second stage. The process is carried out.
- the metal content of the obtained treatment liquid was measured with an Agilent 8900 ICP-QQQ (manufactured by Agilent). The results are shown in Table 2.
- the water content of the IPA simulated solution and the treatment solution was measured, and it was confirmed that both were 30 mass ppm or less. Further, in the same manner, the liquid was passed using the IPA simulated liquid 2. The results are shown in Table 2.
- H-type chelate exchange resin H-type aminophosphate-type chelate resin (manufactured by Organo Corporation, Orlite DS-21 (cation exchange capacity 1.8 eq / L-resin, harmonic mean diameter 500 ⁇ m))
- IPA simulation solution A paraffin oil-based organometallic standard solution Conostan (manufactured by CONOSTAN) was added to IPA XE (manufactured by Tokuyama Corporation) as a standard solution for ICP-AES / ICP-MS to prepare an IPA simulated solution 1 having a mass of 1000 mass. .. Further, in the same manner, a 100 mass ppt IPA simulated solution 2 was prepared. Table 1 shows the content of each metal in the IPA simulated solution.
- Example 1 H-type chelate exchange resin (DS-21), OH-type strongly basic anion exchange resin (DS-2), and H-type strongly acidic cation exchange resin (DS-1) in a volume ratio of 3: 1: 1.
- 50 mL of the mixed mixture was packed in a column having an inner diameter of 16 mm and a height of 300 mm (H-type C / OH-type A / H-type K mixed bed 1).
- the IPA simulated liquid 2 was passed through the H-type C / OH-type A / H-type K mixed bed 1 with SV5h- 1 , and when 20 BV (20 times the resin volume) was passed, the treatment liquid was sampled. Then, the metal content of the obtained treatment liquid was measured.
- Table 3 The results are shown in Table 3.
- DS-2 -OH type strongly basic anion exchange resin
- DS-1 -H-type strongly acidic cation exchange resin
- DS-1 manufactured by Organo Corporation (cation exchange capacity 2.0 eq / L-resin)
- Example 2 30 mL of H-type chelate exchange resin (DS-21) was filled in a column having an inner diameter of 16 mm and a height of 300 mm (H-type C single bed 1). Further, on a column having an inner diameter of 16 mm and a height of 300 mm, an OH-type strongly basic anion exchange resin (DS-2) is placed in the first stage and an H-type strongly acidic cation exchange resin (DS-1) is placed in the second stage, and the layer thickness ratio is 1: 1. In No. 1, a total of 20 mL was filled (OH type A / H type K double bed 1).
- the H-type C single floor 1 in the front stage and the OH-type A / H-type K double floor 1 in the rear stage were connected.
- the IPA simulated solution 2 was passed through the H-type C single bed 1 in the first stage and the OH-type A / H-K double bed 1 in the second stage with SV5h- 1 , and 20 BV (20 times the resin volume) was passed.
- the treatment liquid was sampled.
- the metal content of the obtained treatment liquid was measured. The results are shown in Table 3.
- H-type C single bed 1 30 mL of H-type chelate exchange resin (DS-21) was filled in a column having an inner diameter of 16 mm and a height of 300 mm (H-type C single bed 1). Further, 20 mL of an OH type strongly basic anion exchange resin (DS-2) was filled in a column having an inner diameter of 16 mm and a height of 300 mm (OH type A single bed 1). Next, the H-type C single bed 1 in the front stage and the OH-type A single bed 1 in the rear stage were connected.
- DS-21 H-type chelate exchange resin
- DS-2 an OH type strongly basic anion exchange resin
- the IPA simulated solution 2 was passed through the H-type C single bed 1 in the first stage and the OH-type A single bed 1 in the second stage with SV5h- 1 , and when 20 BV (20 times the resin volume) was passed, the treatment liquid was passed. Sampled. Then, the metal content of the obtained treatment liquid was measured. The results are shown in Table 3.
- Examples 3 to 6 The same procedure as in Example 1 was carried out except that the SV shown in Table 4 was used instead of the SV5h- 1 . The results are shown in Table 4.
- Example 7 On a column with an inner diameter of 16 mm and a height of 300 mm, 18 ml of H-type strong acid cation exchange resin (DS-1) is exchanged in the first stage, and 9 mL of H-type strongly acidic cation exchange resin (DS-1) is exchanged with OH-type strongly basic anion exchange in the second stage. 18 ml of a mixed bed of 9 ml of a resin mixed resin (DS-2) was filled with a layer thickness ratio of 1: 1 in a total of 36 mL (H-type K / H-type, OH-type mixed bed 1).
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Abstract
Description
該第一処理工程の処理液を、アニオン交換体(2)及びH形強酸性カチオン交換体(3)に接触させる第二処理工程と、
を有することを特徴とする有機溶媒の精製方法を提供するものである。
該第一処理工程の処理液を、アニオン交換体(2)及びH形強酸性カチオン交換体(3)に接触させる第二処理工程と、
を有することを特徴とする有機溶媒の精製方法である。
第二処理工程において被処理液を接触させるアニオン交換体(2)及びH形強酸性カチオン交換体(3)として、前記に挙げたカチオン交換体及びアニオン交換体を任意の割合で混合して使ってもよいし、また、アニオン交換体(2)及びH形強酸性カチオン交換体(3)の混合品として販売されているイオン交換体を用いてもよい。アニオン交換体(2)及びH形強酸性カチオン交換体(3)の混合品としては、例えば、オルガノ製のDS-3、DS-7、MSPS2-1・DRY、EG-4A-HG、EG-5A-HG、ESP-1、ESP-2、DUPONT製のAmberTec UP6040、Purolite製MB378、MB378LT、MB400、MB424、MB46、MB47/4914、MB478が挙げられる。
該第一処理工程の処理液を、アニオン交換体(2)及びH形強酸性カチオン交換体(3)に接触させる第二処理工程と、
を有することを特徴とする有機溶媒の精製方法である。
H形キレート交換樹脂(DS-21)(50mL)を、内径16mm、高さ300mmのカラムに充填した。次いで、水分含有量20質量ppm以下のイソプロピルアルコール(IPA)をカラムの上部から下部へ向けて通液し、出口の水分量が30質量ppm以下に低下するまで、通液を続けて、樹脂内部の水分をIPAに置換した。
次いで、カラムにIPA模擬液1をSV5h-1で通液し、20BV(樹脂体積の20倍量)通液したところで、処理液をサンプリングした。
次いで、得られた処理液を、Agilent 8900 ICP-QQQ(Agilent社製)で金属含有量を測定した。その結果を表2に示す。また、IPA模擬液と処理液の水分含有量を測定し、いずれも、30質量ppm以下であることを確認した。
また、同様にして、IPA模擬液2を用いて通液を行った。その結果を表2に示す。
IPA XE(トクヤマ社製)に、ICP-AES/ICP-MS用標準液でパラフィンオイルベースの有機金属標準液Conostan(CONOSTAN社製)を添加して、1000質量pptのIPA模擬液1を調製した。また、同様にして、100質量pptのIPA模擬液2を調製した。IPA模擬液中の各金属含有量を表1に示す。
Aquacounter AQ-2200(平沼産業株式会社製)を用いて、水分含有量を測定した。
H形キレート交換樹脂(DS-21)と、OH形強塩基性アニオン交換樹脂(DS-2)と、H形強酸性カチオン交換樹脂(DS-1)を、体積割合で3:1:1で混合した混合物50mLを、内径16mm、高さ300mmのカラムに充填した(H形C/OH形A/H型K混床1)。
次いで、H形C/OH形A/H型K混床1にIPA模擬液2をSV5h-1で通液し、20BV(樹脂体積の20倍量)通液したところで、処理液をサンプリングした。
次いで、得られた処理液の金属含有量を測定した。その結果を表3に示す。
・H形強酸性カチオン交換樹脂(DS-1):オルガノ社製、(カチオン交換容量2.0eq/L-樹脂)
H形キレート交換樹脂(DS-21)30mLを、内径16mm、高さ300mmのカラムに充填した(H形C単床1)。また、内径16mm、高さ300mmのカラムに、前段にOH形強塩基性アニオン交換樹脂(DS-2)を、後段にH形強酸性カチオン交換樹脂(DS-1)を、層厚比1:1で、合計で20mL充填した(OH形A/H型K複床1)。次いで、前段のH形C単床1と後段のOH形A/H型K複床1を連結した。
次いで、前段のH形C単床1及び後段のOH形A/H型K複床1にIPA模擬液2をSV5h-1で通液し、20BV(樹脂体積の20倍量)通液したところで、処理液をサンプリングした。
次いで、得られた処理液の金属含有量を測定した。その結果を表3に示す。
H形強酸性カチオン交換樹脂(DS-1)50mLを、内径16mm、高さ300mmのカラムに充填した(H形K単床1)。
次いで、H形K単床1にIPA模擬液1をSV5h-1で通液し、20BV(樹脂体積の20倍量)通液したところで、処理液をサンプリングした。
次いで、得られた処理液の金属含有量を測定した。その結果を表3に示す。
OH形強塩基性アニオン交換樹脂(DS-2)と、H形強酸性カチオン交換樹脂(DS-1)を、体積割合で1:1で混合した混合物50mLを、内径16mm、高さ300mmのカラムに充填した(OH形A/H型K混床1)。
次いで、OH形A/H型K混床1にIPA模擬液1をSV5h-1で通液し、20BV(樹脂体積の20倍量)通液したところで、処理液をサンプリングした。
次いで、得られた処理液の金属含有量を測定した。その結果を表3に示す。
H形キレート交換樹脂(DS-21)30mLを、内径16mm、高さ300mmのカラムに充填した(H形C単床1)。また、OH形強塩基性アニオン交換樹脂(DS-2)20mLを、内径16mm、高さ300mmのカラムに充填した(OH形A単床1)。次いで、前段のH形C単床1と後段のOH形A単床1を連結した。
次いで、前段のH形C単床1及び後段のOH形A単床1にIPA模擬液2をSV5h-1で通液し、20BV(樹脂体積の20倍量)通液したところで、処理液をサンプリングした。
次いで、得られた処理液の金属含有量を測定した。その結果を表3に示す。
OH形強塩基性アニオン交換樹脂(DS-2)50mLを、内径16mm、高さ300mmのカラムに充填した(OH形A単床1)。
次いで、OH形A単床1にIPA模擬液1をSV5h-1で通液し、20BV(樹脂体積の20倍量)通液したところで、処理液をサンプリングした。
次いで、得られた処理液の金属含有量を測定した。その結果を表3に示す。
H形強酸性カチオン交換樹脂(DS-1)36mLを、内径16mm、高さ300mmのカラムに充填した(H形K単床1)。次いでIPA模擬液3(表5に示す。)をSV5h-1で通液し、20BV(樹脂体積の20倍量)通液したところで、処理液をサンプリングした。
次いで、得られた処理液の金属含有量を測定した。その結果を表6に示す。
内径16mm、高さ300mmのカラムに、前段にH形強酸性カチオン交換樹脂(DS-1)18mlを、後段にH形強酸性カチオン交換樹脂(DS-1)9mLとOH形強塩基性アニオン交換樹脂の混合樹脂(DS-2)9mlの混床18mlを、層厚比1:1で、合計で36mL充填した(H型K/H形、OH形混床1)。
次いで、H型K/H形、OH形混床1にIPA模擬液4(表5に示す。)をSV5h-1で通液し、20BV(樹脂体積の20倍量)通液したところで、処理液をサンプリングした。
次いで、得られた処理液の金属含有量を測定した。その結果を表6に示す。
・H形強酸性カチオン交換樹脂(DS-1):オルガノ社製(カチオン交換容量≧2.1eq/L-樹脂)
・OH形強塩基性アニオン交換樹脂(DS-2):オルガノ社製(アニオン交換容量≧1.0eq/L-樹脂)
2、24 混床充填塔
3、8a、8b アニオン交換体充填塔
4、9a、9b 強酸性カチオン交換体充填塔
5、11a、11b アニオン交換体の層
6、12a、12b H形強酸性カチオン交換体の層
7、14 複床充填塔
10a、10b、13a、13b 繰り返し単位
20 被処理有機溶媒
21 第一処理工程
22 第二処理工程
23 処理液
25 処理工程(3)
Claims (13)
- 被処理有機溶媒を、H形カチオン交換体(1)に接触させる第一処理工程と、
該第一処理工程の処理液を、アニオン交換体(2)及びH形強酸性カチオン交換体(3)に接触させる第二処理工程と、
を有することを特徴とする有機溶媒の精製方法。 - 前記第一処理工程の処理液を、前記アニオン交換体(2)と前記H形強酸性カチオン交換体(3)の混床に通液することより、前記第二処理工程を行うことを特徴とする請求項1記載の有機溶剤の精製方法。
- 前記第一処理工程の処理液を、先に、前記アニオン交換体(2)に接触させ、次いで、前記H形強酸性カチオン交換体(3)に接触させることにより、前記第二処理工程を行うことを特徴とする請求項1記載の有機溶剤の精製方法。
- 前記H形カチオン交換体(1)が、H形キレート交換体であることを特徴とする請求項1~3いずれか1項記載の有機溶媒の精製方法。
- 前記H形カチオン交換体(1)が、H形強酸性カチオン交換体であることを特徴とする請求項1~3いずれか1項記載の有機溶媒の精製方法。
- 被処理有機溶媒を、H形キレート交換体とアニオン交換体(2)とH形強酸性カチオン交換体(3)の混床に接触させる処理工程を有することを特徴とする有機溶媒の精製方法。
- 前記H形キレート交換体の官能基が、イミノジ酢酸基、アミノメチルリン酸基又はイミノプロピオン酸基であることを特徴とする請求項4又は6記載の有機溶媒の精製方法。
- 前記H形キレート交換体の体積に対する前記アニオン交換体の体積の割合が、0.1~99.0体積%であることを特徴とする請求項4、6及び7のいずれか1項記載の有機溶媒の精製方法。
- 前記H形キレート交換体の体積に対する前記カチオン交換体(2)の体積の割合が、0.1~99.0体積%であることを特徴とする請求項4及び6~8のいずれか1項記載の有機溶媒の精製方法。
- 前記有機溶媒が、極性有機溶媒であること特徴とする請求項1~9いずれか1項記載の有機溶媒の精製方法。
- 被処理有機溶媒が通液されるH形カチオン交換体(1)の単床と、該H形カチオン交換体(1)の単床の処理液が通液されるアニオン交換体(2)及びH形強酸性カチオン交換体(3)の混床と、を有することを特徴とする有機溶媒の精製装置。
- 被処理有機溶媒が通液されるH形カチオン交換体(1)の単床と、該H形カチオン交換体(1)の単床の処理液が通液されるアニオン交換体(2)の単床と、該アニオン交換体(2)の単床の処理液が通液されるH形強酸性カチオン交換体(3)の単床と、を有することを特徴とする有機溶剤の精製装置。
- 被処理有機溶媒が通液されるH形キレート交換体とアニオン交換体(2)とH形強酸性カチオン交換体(3)の混床を有することを特徴とする有機溶媒の精製装置。
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WO2023021895A1 (ja) * | 2021-08-17 | 2023-02-23 | 日清紡ホールディングス株式会社 | イオン液体およびその製造方法 |
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