WO2019088152A1 - ジヒドロキシインドール類の製造方法 - Google Patents
ジヒドロキシインドール類の製造方法 Download PDFInfo
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- WO2019088152A1 WO2019088152A1 PCT/JP2018/040458 JP2018040458W WO2019088152A1 WO 2019088152 A1 WO2019088152 A1 WO 2019088152A1 JP 2018040458 W JP2018040458 W JP 2018040458W WO 2019088152 A1 WO2019088152 A1 WO 2019088152A1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D209/00—Heterocyclic compounds containing five-membered rings, condensed with other rings, with one nitrogen atom as the only ring hetero atom
- C07D209/02—Heterocyclic compounds containing five-membered rings, condensed with other rings, with one nitrogen atom as the only ring hetero atom condensed with one carbocyclic ring
- C07D209/04—Indoles; Hydrogenated indoles
- C07D209/08—Indoles; Hydrogenated indoles with only hydrogen atoms or radicals containing only hydrogen and carbon atoms, directly attached to carbon atoms of the hetero ring
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- the present invention relates to a process for the preparation of dihydroxy indoles.
- Melanin is a yellow to black pigment formed in animals and plants, and is known to have an ultraviolet absorbing function, a radical trapping function, an antioxidant function, and the like.
- melanin is a highly safe substance derived from living bodies, it is widely used to be contained in cosmetics, foods, plastic products, etc. For example, it is used as a UV absorber in sun protection creams, sunglasses, etc.
- it is used as an antioxidant in food and plastic products, etc., and is further used as a pigment in gray hair dyeing and the like.
- melanin is oxidized by catalytic action of a substrate compound 3- (3,4-dihydroxyphenyl) alanine (DOPA) by tyrosinase which is a melanin-forming enzyme, and passes through dopa quinone to be a melanin precursor dihydroxyindole.
- DOPA 3,4-dihydroxyphenyl) alanine
- tyrosinase which is a melanin-forming enzyme, and passes through dopa quinone to be a melanin precursor dihydroxyindole.
- the dihydroxyindoles are biosynthesized by producing the group (5,6-dihydroxyindole, 5,6-dihydroxyindole-2-carboxylic acid, etc.).
- the melanin biosynthesized in this way is present in small particles in melanin-producing cells such as skin and hair, and is stable and insoluble in water and organic solvents that do not dissolve unless hot concentrated sulfuric acid or strong alkali is used. It is a molecular compound. Therefore, for example, when melanin is used as a dye for fibers and leather, even if melanin is used as an additive as it is, melanin insoluble in water or organic solvents can not be permeated into the tissue of the object to be dyed. Water-soluble dihydroxy indoles are used as additives to form melanin in the object to be dyed.
- Patent Document 1 discloses a reaction by adding hexacyanoferrate (III) to an aqueous solution containing 3- (3,4-dihydroxyphenyl) alanine It is disclosed that dihydroxyindoles are produced by carrying out the reaction and the hexacyanoferrate (II) is complexed and removed from the resulting aqueous solution containing dihydroxyindoles. Further, in Non-Patent Documents 1 and 2, dihydroxyindoles are obtained by adding a hexacyanoferrate (III) salt to an aqueous solution containing 3- (3,4-dihydroxyphenyl) alanine and reacting the resulting solution. It is disclosed to extract dihydroxyindoles by adding the extractant ethyl acetate to an aqueous solution containing the dihydroxyindoles.
- the present invention relates to an aqueous first liquid in which one or more selected from the group of 3- (3,4-dihydroxyphenyl) alanine and derivatives thereof are reacted with an oxidizing agent to form dihydroxyindoles.
- a dihydroxyindoles comprising: obtaining step 1; and step 2 of mixing the first solution obtained in step 1 and an extractant to obtain an oily second solution in which the dihydroxyindoles are extracted into the extractant.
- the first liquid obtained in the step 1 is subjected to an operation of removing a water-insoluble by-product before being mixed with the extractant in the step 2.
- the method for producing dihydroxyindoles includes a reaction step (step 1), a purification step (step 2), and a solvent substitution step (step 3) as an optional step.
- a reaction step step 1
- a purification step step 2
- a solvent substitution step step 3
- DOPA 3- (3,4-dihydroxyphenyl) alanine
- DOPA 5,6-dihydroxyindole
- DHI dihydroxyindoles
- ⁇ Reaction step (step 1)> DOPAs are reacted with an oxidizing agent to obtain an aqueous first liquid L1 in which DHIs are formed. At this time, it is preferable to mix DOPA liquid D of an aqueous solution or aqueous suspension of DOPAs with oxidizing solution O of an aqueous solution or aqueous suspension of an oxidizing agent.
- the reaction between DOPAs and an oxidizing agent is a redox reaction.
- FIG. 1 shows an example of the reaction apparatus 10 used in the reaction step (step 1).
- the reactor 10 has a reaction tank 11 and an oxidant tank 12.
- An oxidizing agent supply pipe 13 extending from the bottom of the oxidizing agent tank 12 is introduced at the top of the reaction tank 11.
- a discharge pipe 14 extends from the bottom of the reaction tank 11.
- stirrers 151 and 152 are provided, respectively.
- the stirring blades 151a and 152a of the stirrers 151 and 152 may be any ones capable of sufficiently stirring the low viscosity liquid, and examples thereof include a paddle blade, a disk turbine, an inclined paddle blade, and an anchor blade.
- the reaction vessel 11 is provided with a jacket 16 for controlling the temperature in the vessel.
- the reaction vessel 11 is charged with water.
- water for example, ion exchange water or distilled water is preferably used.
- inert gas such as nitrogen gas and argon gas.
- the dissolved oxygen concentration of water is preferably 1.0 mg / L or less, more preferably 0.5 mg / L or less.
- the dissolved oxygen concentration of this water is measured using a commercially available dissolved oxygen meter (the same applies hereinafter).
- the reaction tank 11 it is preferable to reduce the oxygen concentration by supplying an inert gas such as nitrogen gas or argon gas before or after charging water.
- the oxygen concentration in the gas phase in the reaction vessel 11 is preferably 1.0% by volume or less, and most preferably 0% by volume.
- the oxygen concentration in the gas phase in the reaction tank 11 is measured by a commercially available oximeter (the same applies hereinafter). It is preferable to continuously supply the inert gas to the gas phase in the reaction tank 11 in the operation of this reaction step.
- the stirrer 151 provided in the reaction tank 11 is activated to charge DOPAs while stirring water, thereby dissolving or dispersing the DOPAs, thereby obtaining DOPA liquid D.
- the preparation method of this DOPA class liquid D is a suitable example, first, DOPAs may be charged to the reaction tank 11, and then water may be supplied to the reaction tank 11, or water and DOPAs are simultaneously processed. It may be supplied to the reaction tank 11, or water and DOPAs may be divided and supplied to the reaction tank 11 alternately.
- DOPA includes D-DOPA (3,4-dihydroxy-D-phenylalanine) and L-DOPA (3,4-dihydroxy-L-phenylalanine).
- DOPA derivatives among DOPAs for example, 2-3 ′, 4′-dihydroxyphenylethylamine derivative (N-octanoyl-4- (2-aminoethyl) benzene-1,2-diol, N-octanoyl-4 , 2- (3,4-dihydrophenyl) ethylamine etc., 4- (2-aminoethyl) benzene-1,2-diol (dopamine), salts of D-DOPA (potassium salts, sodium salts etc.), L- Salts of DOPA (potassium salts, sodium salts and the like), lower (C1-C4) alkyl esters of DOPA, ⁇ -lower (C1-C4) alkyl DOPA, and iso
- the content of DOPAs in DOPA liquid D is preferably 0.10 mass% or more, more preferably 0.20 mass% or more, and still more preferably 0.30 mass% or more from the viewpoint of obtaining high productivity. Also, from the viewpoint of suppressing the progress of side reactions and increasing the yield of DHIs, it is preferably at most 1.0 mass%, more preferably at most 0.70 mass%, still more preferably at most 0.50 mass% is there.
- the content of DOPAs in DOPA liquid D is preferably 0.10% by mass or more and 1.0% by mass or less, more preferably 0.20% by mass or more and 0.70% by mass or less, still more preferably 0.30% by mass % Or more and 0.50 mass% or less.
- water is charged into the oxidant tank 12.
- water for example, ion exchange water or distilled water is preferably used.
- inert gas such as nitrogen gas and argon gas.
- the dissolved oxygen concentration of water is preferably 1.0 mg / L or less, more preferably 0.5 mg / L or less.
- the agitator 152 provided in the oxidizing agent tank 12 is activated to charge the oxidizing agent while stirring the water to dissolve or disperse it, thereby obtaining the oxidizing agent liquid O.
- the method of preparing the oxidizing agent solution O is a preferred example, and the oxidizing agent may be charged into the oxidizing agent tank 12 first, and then water may be supplied to the oxidizing agent tank 12, or the water and the oxidizing agent May be supplied to the oxidizing agent tank 12 simultaneously or alternately, or water and an oxidizing agent may be separately supplied to the oxidizing agent tank 12 separately.
- alkali metal salts of hexacyanoferrate (III) such as potassium hexacyanoferrate (III), sodium hexacyanoferrate (III), lithium hexacyanoferrate (III), and hexacyanoferrate (III) Acid salts; metal oxides such as manganese dioxide, silver oxide, palladium dioxide and potassium permanganate; and metal salts such as iron chloride, vanadium trichloride oxide (V), cerium (IV) sulfate and the like.
- the oxidizing agent it is preferable to use one or more of these, and from the viewpoint of productivity, it is preferable to use a hexacyanoferrate (III) salt, and an alkali metal salt of hexacyanoferrate (III). It is more preferable to use, and from the viewpoint of versatility, it is further preferable to use potassium hexacyanoferrate (III).
- a metal catalyst such as copper, manganese or nickel, oxygen can be used as an oxidant.
- hexacyanoferrate (III) such as alkali metal salt of hexacyanoferrate (III)
- hexacyanoferrate (III) such as an alkali metal salt of hexacyanoferrate (III) in the oxidant solution O
- the content of the acid salt is preferably 2.0 equivalents or more, more preferably 2. equivalents or more, with respect to the number of moles of DOPAs in DOPA liquid D, from the viewpoint of promoting the reaction to increase the yield of DHIs.
- hexacyanoferrate (III) such as an alkali metal salt of hexacyanoferrate (III) as the oxidant in the oxidant solution O is preferably 2.% with respect to the number of moles of DOPA in the DOPA solution D. It is 0 equivalent or more and 6.0 equivalents or less, more preferably 2.6 equivalents or more and 5.5 equivalents or less, still more preferably 3.5 equivalents or more and 4.6 equivalents or less.
- the oxidizing agent solution O preferably contains a basic agent from the viewpoint of promoting the reaction by maintaining the pH during the reaction weakly basic.
- the base agent include alkali metal salts of hydrogen carbonate ions such as potassium hydrogen carbonate and sodium hydrogen carbonate, and alkali metal salts of carbonate ions such as potassium carbonate and sodium carbonate. It is preferable to use one or two or more of these as the basic agent.
- the oxidant solution O may additionally contain a chemical substance inert to an oxidant such as benzoates.
- the content of the basic agent in the oxidant liquid O is preferably 3.% with respect to the number of moles of DOPA in the DOPA liquid D from the viewpoint of promoting the reaction by maintaining the pH at the time of reaction moderately weakly basic. 9 equivalents or more, more preferably 5.1 equivalents or more, further preferably 5.9 equivalents or more, and from the same viewpoint, preferably 9.0 equivalents or less, more preferably 7.8 equivalents or less, more preferably Is less than 6.3 equivalents.
- the content of the basic agent in the oxidizing agent solution O is preferably 3.9 equivalents or more and 9.0 equivalents or less, more preferably 5.1 equivalents or more based on the number of moles of DOPAs in the DOPAs solution D. It is the equivalent or less, more preferably 5.9 or more and 6.3 or less.
- the dripping time of the oxidant liquid O is preferably 1 minute or more, more preferably 3 minutes or more, still more preferably 5 minutes or more, from the viewpoint of the applicability to mass production, and also suppresses the progress of the side reaction In order to increase the yield of DHIs, it is preferably 1 hour or less, more preferably 30 minutes or less, and still more preferably 10 minutes or less.
- the dropping time of the oxidizing agent solution O is preferably 1 minute to 1 hour, more preferably 3 minutes to 30 minutes, and still more preferably 5 minutes to 10 minutes.
- the oxidizing agent solution O from the oxidizing agent tank 12 is added to the DOPAs solution D in the reaction tank 11, but the configuration is such that the DOPA liquids D and the oxidizing agent solution O are mixed. It is not particularly limited thereto, for example, it may be configured that DOPAs solution D is added to oxidant solution O, and DOPAs solution D and oxidant solution O may be added to the liquid tank. May be supplied simultaneously or alternately.
- the reaction temperature of the DOPAs with the oxidizing agent is preferably 10 ° C. or more, more preferably 25 ° C. or more, still more preferably 30 ° C. or more, from the viewpoint of increasing the reaction rate and shortening the reaction time.
- the temperature is 50 ° C. or less, more preferably 45 ° C. or less, and still more preferably 40 ° C. or less from the viewpoint of suppressing the progress of DHI and increasing the yield of DHI.
- the reaction temperature of the DOPA with the oxidizing agent is preferably 10 ° C. to 50 ° C., more preferably 25 ° C. to 45 ° C., and still more preferably 30 ° C. to 40 ° C.
- the reaction temperature can be controlled by setting the liquid temperature by the jacket 16 provided in the reaction tank 11, and when the DOPA liquid D is prepared in the reaction tank 11, the liquid temperature of the DOPA liquid D is adjusted. It is preferable to set to this reaction temperature.
- the reaction time (aging time) of the DOPAs with the oxidizing agent is preferably 2 hours or more, more preferably 3 hours or more, more preferably from the start of dropwise addition of the oxidizing agent solution O from the viewpoint of increasing the yield of DHIs. Is 4 hours or more, and preferably 22 hours or less, more preferably 6 hours or less, and still more preferably 5 hours or less from the viewpoint of enhancing the productivity.
- the reaction time of the DOPA with the oxidizing agent is preferably 2 hours or more and 22 hours or less, more preferably 3 hours or more and 6 hours or less, and still more preferably 4 hours or more and 5 hours or less.
- the resulting DHIs correspond to the starting DOPAs, for example DHI and its salts (potassium salts, sodium salts etc.), 5,6-dihydroxyindole-2-carboxylic acid and its salts (potassium salts, sodium salts) Etc.). It is preferable that DHIs contain one or more of them.
- the aqueous first liquid L1 containing DHIs is obtained.
- the pH of the first liquid L1 after pH adjustment is preferably 3.0 or more, more preferably 3.3 or more, and still more preferably 3.5 or more from the viewpoint of stabilizing the DHIs and increasing the yield thereof. In addition, it is preferably 5.5 or less, more preferably 5.3 or less, and still more preferably 5.0 or less, from the viewpoint of increasing the filtration rate during filtration described later and obtaining good phase separation during extraction.
- the pH of the first liquid L1 after pH adjustment is preferably 3.0 to 5.5, more preferably 3.3 to 5.3, and still more preferably 3.5 to 5.0.
- the first liquid L1 obtained in this reaction step is subjected to the removal operation of the water-insoluble by-product before the extraction agent is mixed in the purification step of the next step.
- the "water-insoluble by-product” refers to a by-product of the oxidation-reduction reaction of DOPAs with an oxidizing agent and having a solubility at 20 ° C of 1 mg / 100 g-H 2 O or less.
- water insoluble by-products include melanin and its intermediates.
- hexacyanoferrate (II) is complexed and removed from the reaction solution in which DHIs are generated.
- the reaction solution additionally contains impurities such as unreacted starting materials, dihydroxyindoles are disclosed as disclosed in Non-Patent Documents 1 and 2 from the viewpoint of improving the purity of DHIs. It is preferable to extract and separate into extractant. And, in the extraction of DHIs using such extractant, improvement of the extraction yield is required.
- the present inventors mixed the extractant into the first liquid L1 containing the water-insoluble by-product, the water-insoluble by-product was powder emulsified near the interface between the first liquid L1 and the extractant. It has been discovered that the third phase is formed to inhibit the phase separation between the first liquid L1 and the second liquid L2. It has also been discovered that the formation of this third phase is a factor that reduces the extraction yield of DHIs. As a means for solving this problem, the extraction yield of DHIs to the extractant can be obtained by removing the water-insoluble by-product from the first liquid L1 and appropriately phase separating the first liquid L1 and the extractant. It has been found that it can be enhanced and phase separation can be rapidly.
- the aqueous first liquid L1 obtained by generating DHIs in this reaction step is mixed with the extractant in the purification step of the next step.
- the extraction yield of DHIs by the extractant in the next purification step can be enhanced.
- extraction yield refers to the percentage of the molar amount of DHIs contained in the extractant recovered after extraction and separation relative to the molar amount of DHIs produced in the reaction contained in the reaction liquid.
- examples of the operation for removing the water-insoluble by-product include filtration, centrifugation and the like.
- the removal operation of the water-insoluble by-product is preferably filtration among these in terms of the simplicity of the operation.
- the method for removing the water-insoluble by-product of the first liquid L1 by filtration is not particularly limited.
- a circulation pipe 181 provided with a filter 171 interposed therein is used as a reaction tank.
- 11 may be a method of circulating the first liquid L1 and circulatingly filtering it, and storing the first liquid L1, which is a filtrate after filtration, in the reaction tank 11.
- the number of passes of the circulation pipe 181 of the first liquid L1 is obtained by dividing the total circulating liquid volume obtained by multiplying the flow rate of the first liquid L1 in the circulation pipe 181 by the circulation time by the volume of the first liquid L1 in the reaction tank 11.
- a filter 172 is interposed in an inter-tank connection pipe 182 extending from the reaction tank 11, and the inter-tank connection pipe 182 is connected to the filtrate tank 19 to allow the first liquid L1 to flow therethrough.
- One-pass filtration may be performed, and the first solution L1 which is the filtrate after filtration may be stored in the filtrate tank 19.
- the filter 171, 172 may be provided with a single filter medium 17a, or may be provided with a plurality of filter medium 17a.
- the plurality of filter media 17a may be provided in series along the flow direction of the first liquid L1, as shown in FIG. 4A.
- a plurality of filter media 17a provided in series may be provided mutually spaced apart.
- the plurality of filter media 17a provided in series may have the same mesh size or may have different mesh sizes. In the latter case, it is preferable that the plurality of filter media 17a provided in series be provided with the filter media 17a having a large opening on the upstream side and the filter media 17a having a small opening on the downstream side.
- the openings are provided so as to gradually decrease toward the side.
- several filter media 17a may be provided in parallel so that each of 1st liquid L1 which flow-divided in filter 171,172 may pass.
- the plurality of filter media 17a provided in parallel preferably have the same mesh size.
- the plurality of filter media 17a may be provided by combining the configurations of FIGS. 4A and 4B. That is, as shown in FIG. 4C, the plurality of filter media 17a are provided in parallel so that each of the first liquids L1 separated in the filters 171 and 172 passes through, and for each of them, It may be provided in series along the flow direction of the one liquid L1.
- the mesh size of the filter medium 17a provided in the filters 171 and 172 is preferably 0.1 ⁇ m or more, more preferably 0.5 ⁇ m or more, still more preferably 1.0 ⁇ m or more, from the viewpoint of increasing the filtration rate. It is preferably 5.0 ⁇ m or less, more preferably 2.0 ⁇ m or less, and still more preferably 1.5 ⁇ m or less, from the viewpoint of removing the insoluble by-products to increase the extraction yield of DHIs into the extractant.
- the mesh size of the filter medium 17a provided in the filters 171 and 172 is 0.1 ⁇ m to 5.0 ⁇ m, more preferably 0.5 ⁇ m to 2.0 ⁇ m, and still more preferably 1.0 ⁇ m to 1.5 ⁇ m.
- the material of the filter medium 17a is not particularly limited from the viewpoint of removal of the water-insoluble by-product, but is preferably formed of a hydrophilic material from the viewpoint of increasing the filtration rate.
- ⁇ Purification step (step 2)> In the purification step (step 2), the first liquid L1 obtained in the reaction step (step 1) and the extractant are mixed to obtain an oily second liquid L2 in which DHIs are extracted as extractant.
- the extractant is added while stirring the first liquid L1 to extract the extractant.
- the DHIs are extracted, and this time, the first liquid L1 of the lower aqueous phase and the second liquid L2 of the oil phase from which the DHIs are extracted as the upper extract are separated.
- the lower layer first liquid L1 is discharged from the bottom of the tank A 20A to obtain an oily second liquid L2.
- the tank A 20A may be the reaction tank 11 shown in FIG. 1 and FIGS. 2A and 2B used in the reaction step, or may be the filtrate storage tank 19 shown in FIG.
- the extractant is added to the first liquid L1, but when the first liquid L1 is transferred from the reaction tank 11, the first liquid L1 and the extractant are mixed.
- the first solution L1 may be added to the extractant, and the first solution L1 and the extractant may be added simultaneously or alternately to the liquid tank. It may be configured to be supplied.
- the tank A it is preferable to reduce the oxygen concentration by supplying an inert gas such as nitrogen gas or argon gas.
- the oxygen concentration in the gas phase in tank A 20A is preferably 1.0% by volume or less, most preferably 0% by volume. It is preferable to continuously supply the inert gas to the gas phase in the tank A 20A in the operation of this purification step.
- the extractant is preferably an organic solvent having an octanol / water distribution coefficient (LogP) of 0 or more and 4.0 or less, from the viewpoint of separation.
- the extractant for example, ethyl acetate (0.73), which is an organic solvent having an octanol / water distribution coefficient of less than 0.90, diethyl ether (0.89); an octanol / water distribution coefficient of more than 0.90
- the organic solvent methyl isobutyl ketone (1.4), dichloromethane (1.3), cyclohexane (3.4), etc. may be mentioned (the value in the parentheses is octanol / water partition coefficient).
- an octanol / water partition coefficient is preferably an organic solvent having a coefficient of 1.5 or less, more preferably less than 0.90. It is more preferable to use including, and it is further more preferable to use including ethyl acetate.
- a chemical substance inert to DHIs such as benzoates and phosphates may be added together with the extractant.
- the mixing amount of the extractant to the first liquid L1 is preferably 20% by volume or more, more preferably to the volume of the first liquid L1 at the end of the reaction from the viewpoint of enhancing the extraction yield of DHIs to the extractant. Is 30% by volume or more, more preferably 50% by volume or more, and from the viewpoint of reducing the amount of waste liquid to reduce the manufacturing cost, preferably 400% by volume or less, more preferably 200% by volume or less, more preferably It is 100 volume% or less.
- the mixing amount of the extractant with respect to the first liquid L1 is preferably 20% to 400% by volume, more preferably 30% to 200% by volume, further preferably, relative to the volume of the first liquid L1 at the end of the reaction. Preferably, they are 50% by volume or more and 100% by volume or less.
- the mixture is stirred after or while adding the extractant to the first liquid L1.
- the stirring time (extraction time) of the mixture is preferably 10 minutes or more, more preferably 15 from the viewpoint of enhancing the extraction yield of DHIs to the extractant. It is preferably at least 120 minutes, more preferably at most 90 minutes, still more preferably at most 60 minutes, in view of enhancing the productivity.
- the stirring time (extraction time) of the mixed solution is preferably 10 minutes to 120 minutes, more preferably 15 minutes to 90 minutes, and still more preferably 20 minutes to 60 minutes.
- the stirring time (extraction time) from the start of the extractant addition of the first solution L1 increases the extraction yield of DHIs to the extractant. It is preferably 10 minutes or more, more preferably 15 minutes or more, still more preferably 20 minutes or more, and from the viewpoint of enhancing the productivity, preferably 120 minutes or less, more preferably 90 minutes or less, still more preferably 60 It is less than a minute.
- the stirring time (extraction time) of the first liquid L1 is preferably 10 minutes to 120 minutes, more preferably 15 minutes to 90 minutes, and still more preferably 20 minutes to 60 minutes.
- the oily second liquid L2 formed is preferably separated from the aqueous liquid from the viewpoint of removing impurities, and then the second liquid L2 obtained is further subjected to From the viewpoint of removing impurities, it is preferable to perform washing with washing water.
- a cleaning method in the tank A for storing the obtained second liquid L2, after making the second liquid L2 sufficiently contact with the second liquid L2 by adding the washing water while stirring the second liquid L2, There is a method of discharging the latter of the oil phase of the second liquid L2 in the upper layer and the lower aqueous phase, which are phase-separated, from the bottom of the A tank 20A.
- the amount of washing water added to the second liquid L2 is preferably 10% by volume or more, more preferably 20 volumes, with respect to the volume of the second liquid L2, from the viewpoint of keeping the pH of the washing water stable near neutrality. % Or more, more preferably 30% by volume or more, and preferably 100% by volume or less, more preferably 80% by volume or less, still more preferably 50% by volume or less from the viewpoint of enhancing the yield of DHIs.
- the amount of washing water added to the second liquid L2 is preferably 10% to 100% by volume, more preferably 20% to 80% by volume, still more preferably 30% by volume, relative to the volume of the second liquid L2. It is volume% or more and 50 volume% or less.
- the washing time of the second liquid L2 with washing water is preferably 30 minutes or more, more preferably 45 minutes or more, and still more preferably 60 minutes or more, from the viewpoint of keeping the pH of the washing water stable near neutrality. Also, from the viewpoint of increasing the yield of DHIs, it is preferably 120 minutes or less, more preferably 105 minutes or less, and still more preferably 90 minutes or less.
- the washing time of the second liquid L2 with washing water is preferably 30 minutes to 120 minutes, more preferably 45 minutes to 105 minutes, and still more preferably 60 minutes to 90 minutes.
- the washing water may contain a polybasic acid salt from the viewpoint of adjusting the pH to around neutral.
- polybasic acid salts include potassium salts of phosphoric acid, potassium salts of citric acid, potassium salts of carbonic acid, sodium salts of phosphoric acid, sodium salts of citric acid, sodium salts of carbonic acid and the like. It is preferable to use one or more of these polybasic acids, and it is more preferable to use a potassium salt of phosphoric acid (dipotassium hydrogen phosphate and dipotassium hydrogen phosphate).
- the extraction yield of DHIs into the extractant is preferably 25 mol% or more, more preferably 50 mol% or more, and still more preferably 75 mol% or more.
- solvent substitution step (step 3) solvent substitution is carried out by mixing the second liquid L2 obtained in the purification step (step 2) and water W and distilling off the extractant, and It is preferable to obtain a DHI liquid of an aqueous solution or an aqueous dispersion containing DHIs, which is the third liquid L3. Further, from the viewpoint of the efficiency at the time of production, it is preferable to adjust the concentration together with this solvent substitution.
- the solvent replacement step is preferably performed in the B tank 20B in which the inside of the tank is washed, from the viewpoint of increasing the purity of the DHI liquid. Therefore, first, as shown in FIG. 6A, the second liquid L2 obtained in the purification step is discharged from the tank A and transferred, and then the second liquid L2 is transferred to the tank B which cleans the inside of the tank. Supply and store.
- the B tank 20B may be a liquid tank different from the A tank 20A, or may be the original A tank 20A in which the inside of the tank is washed after discharging the second liquid L2.
- the oxygen concentration in the gas phase in the tank of tank B 20B is preferably 1.0% by volume or less, and most preferably 0% by volume. It is preferable that the supply of the inert gas to the gas phase in the tank of tank B 20B be continuously performed in the operation of the solvent replacement step.
- water W is added to the second liquid L2 in the tank B 20B, and subsequently, the second liquid L2 to which the water W is added in the tank B 20B is heated to extract the extractant.
- the solvent is distilled off and the extractant is solvent-replaced with water W.
- the number of times of solvent substitution is preferably 2 or more and 4 or less.
- water W to be added for example, ion exchange water or distilled water is preferably used.
- water W it is preferable to use what reduced dissolved oxygen concentration by supplying inert gas, such as nitrogen gas and argon gas.
- the dissolved oxygen concentration of water W is preferably 1.0 mg / L or less, more preferably 0.5 mg / L or less.
- the addition of water W to the second liquid L2 at the time of the first solvent substitution may be performed on the second liquid L2 after being supplied to the B tank 20B, or may be discharged from the A tank 20A and the B tank It may be performed on the second liquid L2 until it is supplied to 20B.
- the water W may be added to the liquid remaining in the B tank 20B in the second or subsequent solvent replacement.
- the amount of water W added is the volume of the liquid remaining in tank B 20B with respect to the volume of the second liquid L2 in the first solvent substitution, or in the second or later solvent substitution.
- the amount of water W added is preferably 50% by volume or more with respect to the volume of the second liquid L2 in the first solvent substitution, or with respect to the volume of the liquid remaining in the tank B 20B in the second and subsequent solvent substitution. It is 150% by volume or less, more preferably 80% by volume or more and 120% by volume or less, and further preferably 100% by volume or more and 110% by volume or less.
- the liquid temperature when distilling off the extractant is preferably 40 ° C. or more, more preferably 50 ° C. or more, still more preferably 60 ° C. or more, from the viewpoint of increasing the evaporation rate of the extractant From the viewpoint of suppressing thermal decomposition, it is preferably 90 ° C. or less, more preferably 85 ° C. or less, and further preferably 80 ° C. or less.
- the liquid temperature when distilling off the extractant is preferably 40 ° C. or more and 90 ° C. or less, more preferably 50 ° C. or more and 85 ° C. or less, still more preferably 60 ° C. or more and 80 ° C. or less.
- the pressure when distilling the extraction agent in the first solvent substitution is preferably atmospheric pressure (101.325 kPa (abs)) or less, more preferably 90 kPa (abs) or less, from the viewpoint of increasing the evaporation rate of the extraction agent. More preferably, it is 80 kPa (abs) or less.
- the pressure for distilling off the extractant in the second or subsequent solvent substitution is preferably 80 kPa (abs) or less, more preferably 40 kPa (abs) or less, still more preferably 10 kPa, from the viewpoint of increasing the evaporation rate of the extractant. (Abs) or less.
- DHIs in the form of DHI liquid which is an aqueous third liquid L3, by adding water and a water-soluble solvent to the liquid remaining in tank B after solvent substitution and adjusting the concentration
- You can get As a water-soluble solvent, ethanol etc. are mentioned, for example.
- the content of DHIs in the DHI solution of the third solution L3 obtained is preferably 0.3% by mass or more, more preferably 0.5% by mass or more, and still more preferably 1.0% by mass or more.
- the content of DHIs is measured by high performance liquid chromatography (HPLC).
- the content of the organic solvent in the DHI liquid of the third liquid L3 obtained is preferably 1.5% by mass or less, more preferably 1.0% by mass or less, and still more preferably 0.5% by mass or less.
- the content of the organic solvent is measured by gas chromatography (GC).
- DHI class liquid of the 3rd liquid L3 after solvent substitution when used for dyeing applications, such as hair dyeing, it is desirable for DHI class content to be about 1 mass%. From such a viewpoint, it is preferable to concentrate the second liquid L2 before solvent substitution.
- the concentration operation of the second liquid L2 is carried out by concentrating the second liquid L2 obtained in the purification step by distilling off the extractant in the A tank 20A, and then discharging the concentrated second liquid L2 from the A tank 20A, May be supplied to and stored in the tank B 20B.
- the second liquid L2 obtained in the purification step is discharged from tank A 20A, supplied to tank B 20B and stored, and then the extractant is distilled off in tank B 20B to concentrate second liquid L2 You may Furthermore, the second liquid L2 obtained in the purification step is discharged from the tank A, supplied to another liquid tank, concentrated by distilling off the extractant, and then discharged from the liquid tank and concentrated.
- the second liquid L2 may be supplied to and stored in the B tank 20B.
- the liquid temperature when concentrating the second liquid L2 is preferably 40 ° C. or higher, more preferably 50 ° C. or higher, still more preferably 60 ° C. or higher, from the viewpoint of increasing the distillation rate of the extractant, and DHI From the viewpoint of suppressing the thermal decomposition of the above, it is preferably 90 ° C. or less, more preferably 85 ° C. or less, still more preferably 80 ° C. or less.
- the liquid temperature when concentrating the second liquid L2 is preferably 40 ° C to 90 ° C, more preferably 50 ° C to 85 ° C, and still more preferably 60 ° C to 80 ° C.
- the pressure for concentrating the second liquid L2 is preferably atmospheric pressure (101.325 kPa (abs)) or less, more preferably 100 kPa (abs) or less, still more preferably 90 kPa, from the viewpoint of increasing the distillation rate of the extractant. (Abs) or less.
- DOPAs and an oxidizing agent are made to react, the process 1 of obtaining the aqueous
- ⁇ 3-2> The method according to ⁇ 2>, wherein the opening of the filter medium used in the filtration is 1.5 ⁇ m or less.
- ⁇ 4> The method according to any one of ⁇ 2> to ⁇ 3-2>, wherein the opening of the filter medium used in the filtration is 0.1 ⁇ m or more.
- ⁇ 4-1> The production method according to any one of ⁇ 2> to ⁇ 3-2>, wherein the opening of the filter medium used in the filtration is 0.5 ⁇ m or more.
- ⁇ 4-2> The method according to any one of ⁇ 2> to ⁇ 3-2>, wherein the opening of the filter medium used in the filtration is 1.0 ⁇ m or more.
- ⁇ 5> The method according to any one of ⁇ 2> to ⁇ 4-2>, wherein the filtration is performed by circulating the first liquid through a circulation pipe provided with a filter provided with the filter medium. Manufacturing method.
- the number of times of circulation of the first liquid to the circulation pipe is preferably 2 or more, more preferably 3 or more, still more preferably 4 or more, and preferably 10 or less, more preferably
- the manufacturing method described in ⁇ 5> which is 8 times or less, more preferably 6 times or less.
- ⁇ 7> The manufacturing method according to any one of ⁇ 2> to ⁇ 4>, wherein the filtration is performed by flowing through a pipe provided with a filter provided with the filter medium and performing one-pass filtration.
- ⁇ 8> The method according to any one of ⁇ 5> to ⁇ 7>, wherein the filter medium provided in the filter is single.
- ⁇ 9> The method according to any one of ⁇ 5> to ⁇ 7>, wherein a plurality of the filter media are provided in the filter.
- ⁇ 12> The manufacturing method according to any one of ⁇ 9> to ⁇ 11>, wherein the plurality of filter media are provided in parallel so that each of the first liquids separated in the filter passes therethrough.
- step 1 an aqueous solution or an aqueous suspension containing 0.20% by mass or more of the DOPAs and an aqueous solution or an aqueous suspension of the oxidizing agent are mixed, ⁇ 1> to ⁇ 13> The manufacturing method described in any of the above.
- the content of ⁇ 15> the DOPAs is preferably 0.30% by mass or more, and is preferably 1.0% by mass or less, more preferably 0.70% by mass or less, still more preferably 0.50% by mass
- the manufacturing method as described in ⁇ 14> which is% or less.
- ⁇ 16> The method according to ⁇ 14> or ⁇ 15>, wherein the oxidizing agent comprises an alkali metal salt of hexacyanoferrate (III).
- the content of the alkali metal of hexacyanoferrate (III) of the ⁇ 17> oxidizing agent is preferably 2.0 equivalents or more, more preferably 2.6 equivalents or more, further preferably to the number of moles of the DOPA. Is 3.5 equivalents or more, preferably 6.0 equivalents or less, more preferably 5.5 equivalents or less, still more preferably 4.6 equivalents or less.
- ⁇ 18> The method according to any one of ⁇ 14> to ⁇ 17>, wherein the aqueous solution or aqueous suspension of the oxidizing agent contains a base.
- the content of the ⁇ 20> base is preferably 3.9 equivalents or more, more preferably 5.1 equivalents or more, still more preferably 5.9 equivalents or more, relative to the number of moles of the DOPA.
- the production method according to ⁇ 18> or ⁇ 19> which is preferably 9.0 equivalents or less, more preferably 7.8 equivalents or less, still more preferably 6.3 equivalents or less.
- ⁇ 21> The production method according to any one of ⁇ 1> to ⁇ 20>, wherein the extractant contains an organic solvent having an octanol / water distribution coefficient of 0 or more and 4.0 or less.
- the mixing amount of the extractant with respect to the ⁇ 23> first liquid is preferably 20% by volume or more, more preferably 30% by volume or more, still more preferably 50% by volume with respect to the volume of the first solution at the end of the reaction.
- DHI content HPLC
- a 0.1 wt% aqueous phosphoric acid solution containing 1.0 g of sodium ascorbate as an antioxidant and 0.2 wt% of potassium benzoate was added. 0g and 1.0g of DHI solution were mixed. The solution was then adjusted to 50 mL with a 0.1 wt% aqueous phosphoric acid solution in a volumetric flask and measured by HPLC to calculate the DHI content.
- the solution which blew in nitrogen gas and made the dissolved oxygen concentration 1.0 mg / L or less also used any solution.
- Method of measuring purity The purity of DHI was calculated as a percentage of the DHI peak area value to the value obtained by subtracting the area values of sodium ascorbate and potassium benzoate from the peak area values of all the substances measured by HPLC. .
- Example 1 -Reaction process (Step 1)- In Example 1, a reaction vessel and an oxidant vessel are provided in the same manner as shown in FIG. 1, and a reaction vessel is provided with a circulation pipe having a filter interposed in the same manner as shown in FIG. 2A. I prepared the device.
- the reaction vessel had a volume of 300 L and was provided with a stirrer having anchor wings and a jacket for temperature control.
- the oxidant tank was provided with a stirrer.
- the filter was provided with a single filter medium having an opening of 1.2 ⁇ m.
- the potassium hexacyanoferrate (III) aqueous solution in the oxidizing agent tank is dropped over 10 minutes, and the solution is aged for 4 hours from the start of dropwise addition, DOPA and hexacyanoiron (III 2.)
- the reaction mixture was subjected to oxidation reduction reaction with potassium acid to obtain an aqueous first liquid in which DHI was formed. During this time, the liquid temperature of the reaction liquid in the reaction tank was maintained at 35 ° C.
- a pH adjustment agent is added with an aqueous phosphoric acid solution having a concentration of 10% by mass at a dissolved oxygen concentration of 1.0 mg / L or less to obtain a pH of 4. Adjusted to 7. A part of the obtained first liquid was taken out, the content of DHI was measured by HPLC, and the molar amount of DHI in the first liquid was calculated.
- the first liquid in the reaction tank was circulated to a circulation pipe and filtered by a filter to remove water insoluble by-products.
- the number of passes of the circulation piping of the first liquid was five.
- step 2 A part of the first liquid from which water insoluble by-products were removed by filtration was taken out and No. 1 Transfer to 7 screw tube. Then, add 50% by volume of ethyl acetate as an extractant to the first solution in the screw tube with respect to the first solution, shake the screw tube by hand, and stir them well to obtain ethyl acetate as the extractant. An oily second liquid from which DHI was extracted was obtained. After that, the stirring was stopped, and the aqueous first liquid and the oily second liquid were phase separated. Thereafter, only the second solution in the upper layer is recovered using a pipette, a part of the obtained second solution is taken out, the DHI content is measured by HPLC, and the molar amount of DHI in the recovered second solution is determined. Calculated.
- Example 2 -Reaction process (Step 1)- In Example 2, first, nitrogen gas was continuously supplied to a reaction vessel having a volume of 500 mL, and nitrogen gas was blown into the reactor to charge water having a dissolved oxygen concentration of 1.0 mg / L or less. While stirring the water in the reaction tank, DOPA was added and dissolved therein to prepare 348 mL of DOPA aqueous solution (DOPA-like liquid) having a concentration of 0.33% by mass. At this time, the liquid temperature of the DOPA aqueous solution was adjusted to 35 ° C.
- DOPA aqueous solution DOPA-like liquid
- potassium hexacyanoferrate (III) aqueous solution having a concentration of 16.8% by mass is added by dissolving the oxidizing agent potassium hexacyanoferrate (III) and the basic agent potassium hydrogencarbonate in ion-exchanged water and dissolving it
- the preparation solution (41 mL) was prepared.
- the content of potassium hexacyanoferrate (III) in the aqueous potassium hexacyanoferrate (III) solution is 4.0 equivalents relative to the number of moles of DOPA in the aqueous DOPA solution.
- the content of potassium hydrogen carbonate of the basic agent in the aqueous potassium hexacyanoferrate (III) solution is 6.0 equivalents relative to the number of moles of DOPA in the aqueous solution of DOPA.
- a pH adjustment agent is added with an aqueous phosphoric acid solution having a concentration of 10% by mass at a dissolved oxygen concentration of 1.0 mg / L or less to obtain a pH of 4. Adjusted to 7. A part of the obtained first liquid was taken out, the content of DHI was measured by HPLC, and the molar amount of DHI in the first liquid was calculated.
- step 2 The first solution from which water insoluble by-products were removed by filtration was No. 1 solution. Transfer to 7 screw tube. Then, add 50% by volume of ethyl acetate as an extractant to the first solution in the screw tube with respect to the first solution, shake the screw tube by hand, and stir them well to obtain ethyl acetate as the extractant. An oily second liquid from which DHI was extracted was obtained. After that, the stirring was stopped, and the aqueous first liquid and the oily second liquid were phase separated. Thereafter, only the second solution in the upper layer is recovered using a pipette, a part of the obtained second solution is taken out, the DHI content is measured by HPLC, and the molar amount of DHI in the recovered second solution is determined. Calculated.
- Example 3 In Example 3, the same operation as in Example 2 was performed except that a filter medium having an opening of 5.0 ⁇ m was used.
- Example 4 In Example 4, the same operation as in Example 2 was performed except that the removal of the water-insoluble by-product was performed by centrifuging the first solution. Centrifugation was performed by taking 7 mL of the first solution in a reaction vessel in a centrifuge tube with a volume of 15 mL, and making the rotation speed 5000 rpm and the rotation time 2 minutes.
- Comparative Example In the comparative example, the same operation as in Example 2 was performed except that the removal operation of the water-insoluble by-product by filtration was not performed.
- phase separation speed was determined for each of Examples 1 to 4 and Comparative Example.
- the phase separation speed was calculated by dividing the liquid height when ethyl acetate as the extractant was added to the first liquid by the time required for phase separation after stopping the agitation of the screw pipe.
- the present invention is useful for the technical field of methods for producing dihydroxy indoles.
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Abstract
Description
反応工程では、DOPA類と酸化剤とを反応させてDHI類を生成させた水性の第1液L1を得る。このとき、DOPA類の水溶液又は水性懸濁液のDOPA類液Dと、酸化剤の水溶液又は水性懸濁液の酸化剤液Oとを混合することが好ましい。また、DOPA類と酸化剤との反応は、酸化還元反応である。
精製工程(工程2)では、反応工程(工程1)で得た第1液L1と抽剤とを混合して抽剤にDHI類を抽出した油性の第2液L2を得る。
任意工程としての溶媒置換工程(工程3)では、精製工程(工程2)で得た第2液L2と水Wとを混合して抽剤を留去することにより溶媒置換を行い、水性の第3液L3であるDHI類を含有する水溶液又は水分散液のDHI類液を得ることが好ましい。また、生産時の効率性の観点からは、この溶媒置換と共に濃度調整を行うことが好ましい。
以下の実施例1~4及び比較例のDHIの製造実験を行った。なお、いずれの工程も窒素雰囲気下にて行った。それぞれの構成については表1にも示す。
・DHIの含有量(HPLC)
まず、容器内を窒素で置換した50mLのメスフラスコに、酸化防止剤であるアスコルビン酸ナトリウムを1.0g、安息香酸カリウムを0.2重量%含有した0.1重量%りん酸水溶液を2.0g及びDHI溶液を1.0gを混合した。次いで、メスフラスコに0.1重量%りん酸水溶液を50mLになるまで加えて溶液を調整し、それをHPLCにより測定してDHIの含有量を算出した。なお、いずれの溶液も窒素ガスを吹き込んで溶存酸素濃度を1.0mg/L以下にした溶液を使用した。
・純度の測定方法
DHIの純度は、HPLCにより測定された全ての物質のピーク面積値より、アスコルビン酸ナトリウム及び安息香酸カリウムの面積値を減じた値に対する、DHIのピーク面積値の百分率として算出した。
-反応工程(工程1)-
実施例1では、図1に示すのと同様に反応槽及び酸化剤槽を備え、また、図2Aに示すのと同様に反応槽に、濾過器が介設された循環配管が設けられた反応装置を準備した。反応槽は、容量が300Lであって、アンカー翼を有する撹拌機及び温度調節用のジャケットが設けられたものであった。酸化剤槽は、撹拌機が設けられたものであった。濾過器は、目開きが1.2μmの単一の濾材が設けられたものであった。
濾過により水不溶性副生成物を除去した第1液の一部を取出してNo.7スクリュー管に移した。次いで、スクリュー管内の第1液に、抽剤として酢酸エチルを、第1液に対して50体積%添加し、スクリュー管を手で振ってそれらをよく撹拌することにより、抽剤の酢酸エチルにDHIを抽出した油性の第2液を得た。その後、撹拌を止め、水性の第1液と油性の第2液とを相分離させた。その後、ピペットを用いて上層の第2液のみを回収し、得られた第2液の一部を取出し、そのDHIの含有量をHPLCにより測定し、回収した第2液におけるDHIのモル量を算出した。
-反応工程(工程1)-
実施例2では、まず、容量が500mLの反応槽に窒素ガスを継続的に供給し、そこに窒素ガスを吹き込んで溶存酸素濃度を1.0mg/L以下にした水を仕込んだ。反応槽内の水を撹拌しながら、そこにDOPAを投入して溶解させることにより、濃度が0.33質量%のDOPA水溶液(DOPA類液)を348mL調製した。このとき、DOPA水溶液の液温を35℃に調整した。
濾過により水不溶性副生成物を除去した第1液をNo.7スクリュー管に移した。次いで、スクリュー管内の第1液に、抽剤として酢酸エチルを、第1液に対して50体積%添加し、スクリュー管を手で振ってそれらをよく撹拌することにより、抽剤の酢酸エチルにDHIを抽出した油性の第2液を得た。その後、撹拌を止め、水性の第1液と油性の第2液とを相分離させた。その後、ピペットを用いて上層の第2液のみを回収し、得られた第2液の一部を取出し、そのDHIの含有量をHPLCにより測定し、回収した第2液におけるDHIのモル量を算出した。
実施例3では、目開きが5.0μmの濾材を用いたことを除いて実施例2と同様の操作を行った。
実施例4では、水不溶性副生成物の除去を、第1液を遠心分離することにより行ったことを除いて実施例2と同様の操作を行った。遠心分離は、反応槽内の第1液を容量が15mLの遠沈管に7mL取り、回転数を5000rpm及び回転時間を2分として行った。
比較例では、濾過による水不溶性副生成物の除去操作を行わなかったことを除いて実施例2と同様の操作を行った。
実施例1~4及び比較例それぞれで得た油性の第2液について抽出収率を求めた。抽出収率は、第1液におけるDHIの含有モル量に対する、第2液におけるDHIの含有モル量の百分率として算出した。
O 酸化剤液
L1 第1液
L2 第2液
L3 第3液
W 水
10 反応装置
11 反応槽
12 酸化剤槽
13 酸化剤供給管
14 排出管
151,152 撹拌機
151a,152a 撹拌翼
16 ジャケット
171,172 濾過器
17a 濾材
181 循環配管
182 槽間連結配管
19 濾液槽
Claims (9)
- 3-(3,4-ジヒドロキシフェニル)アラニン及びその誘導体の群から選ばれる1種又は2種以上と酸化剤とを反応させてジヒドロキシインドール類を生成させた水性の第1液を得る工程1と、
前記工程1で得た前記第1液と抽剤とを混合して前記抽剤に前記ジヒドロキシインドール類を抽出した油性の第2液を得る工程2と、
を含むジヒドロキシインドール類の製造方法であって、
前記工程1で得た前記第1液に、前記工程2で前記抽剤と混合する前に、水不溶性副生成物の除去操作を行う製造方法。 - 前記水不溶性副生成物の除去操作が濾過である、請求項1に記載された製造方法。
- 前記濾過で用いる濾材の目開きが5.0μm以下である、請求項2に記載された製造方法。
- 前記濾過で用いる濾材の目開きが2.5μm以下である、請求項2に記載された製造方法。
- 前記濾過で用いる濾材の目開きが2.0μm以下である、請求項2に記載された製造方法。
- 前記濾過で用いる濾材の目開きが1.5μm以下である、請求項2に記載された製造方法。
- 前記工程1では、前記3-(3,4-ジヒドロキシフェニル)アラニン及びその誘導体の群から選ばれる1種又は2種以上を0.2質量%以上含有する水溶液又は水性懸濁液と、前記酸化剤の水溶液又は水性懸濁液とを混合する、請求項1乃至6のいずれかに記載された製造方法。
- 前記工程1では、前記3-(3,4-ジヒドロキシフェニル)アラニン及びその誘導体の群から選ばれる1種又は2種以上を0.3質量%以上含有する水溶液又は水性懸濁液と、前記酸化剤の水溶液又は水性懸濁液とを混合する、請求項1乃至7のいずれかに記載された製造方法。
- 前記抽剤が、オクタノール/水分配係数が0以上4.0以下の有機溶剤を含む、請求項1乃至8のいずれかに記載された製造方法。
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TRAN, M. L. ET AL.: "Chemical and Structural Disorder in Eumelanins: A Possible Explanation for Broadband Absorbance", BIOPHYSICAL JOURNAL, vol. 90, no. 3, 2006, pages 743 - 752, XP055617964, DOI: 10.1529/biophysj.105.069096 * |
WAKAMATSU, K. ET AL.: "Preparation of Eumelanin-Related Metabolites 5,6-Dihydroxyindole, 5,6-Dihydroxyindole-2-carboxylic Acid, and Their 0-Methyl Derivatives", ANALYTICAL BIOCHEMISTRY, vol. 170, 1988, pages 335 - 340, XP024820504, DOI: 10.1016/0003-2697(88)90639-2 * |
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Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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CN110981782A (zh) * | 2019-12-25 | 2020-04-10 | 广州星业科技股份有限公司 | 一种高效制备5,6-二羟基吲哚的方法 |
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US10947195B2 (en) | 2021-03-16 |
SG11202004021RA (en) | 2020-05-28 |
EP3705473A4 (en) | 2021-07-07 |
JPWO2019088152A1 (ja) | 2020-11-12 |
US20200270208A1 (en) | 2020-08-27 |
CN111225902A (zh) | 2020-06-02 |
TW201922701A (zh) | 2019-06-16 |
EP3705473A1 (en) | 2020-09-09 |
EP3705473B1 (en) | 2024-02-28 |
BR112020008675A2 (pt) | 2020-10-27 |
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