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Publication numberUS20020010373 A1
Publication typeApplication
Application numberUS 09/741,092
Publication dateJan 24, 2002
Filing dateDec 21, 2000
Priority dateJan 5, 2000
Also published asDE10100213A1, DE10100213B4, US6392101
Publication number09741092, 741092, US 2002/0010373 A1, US 2002/010373 A1, US 20020010373 A1, US 20020010373A1, US 2002010373 A1, US 2002010373A1, US-A1-20020010373, US-A1-2002010373, US2002/0010373A1, US2002/010373A1, US20020010373 A1, US20020010373A1, US2002010373 A1, US2002010373A1
InventorsTakeo Komata, Nariaki Ii, Yoshiki Hirotsu
Original AssigneeTakeo Komata, Nariaki Ii, Yoshiki Hirotsu
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Solvent extraction
US 20020010373 A1
Abstract
The invention relates to a process for purifying a crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate containing an impurity. The process includes bringing the crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate into contact with a poor solvent in which 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate is substantially insoluble, thereby removing the impurity from the crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate. Alternatively, the process includes precipitating crystals of 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate from a solution of the crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate. Thus, it is possible to produce 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate of high purity. This product makes it easy to produce 1,1,1,5,5,5-hexafluoroacetylacetone of high purity.
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Claims(22)
What is claimed is:
1. A process for purifying a crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate containing an impurity, said process comprising bringing said crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate into contact with a poor solvent in which 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate is substantially insoluble, thereby removing said impurity from said crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate.
2. A process according to claim 1, wherein said poor solvent has a boiling point of not higher than about 200° C.
3. A process according to claim 1, wherein said poor solvent is at least one selected from the group consisting of aromatic hydrocarbons, aliphatic hydrocarbons, alicyclic hydrocarbons, industrial gasolines, and fluorine-containing solvents.
4. A process according to claim 3, wherein said aromatic hydrocarbons are benzene, toluene, o-xylene, m-xylene, p-xylene, ethyl benzene, and mesitylene,
wherein said aliphatic hydrocarbons are n-pentane, n-hexane, n-heptane, n-octane, n-nonane, n-decane, and isomers thereof, each of said isomers being in a liquid at about 5° C.,
wherein said alicyclic hydrocarbons are cyclopentane, cyclohexane, methylcyclopentane, methylcyclohexane, tetralin, and decalin,
wherein said industrial gasolines are ligroin and petroleum ether,
wherein said fluorine-containing solvents are
1,2-bis(trifluoromethyl)benzene,
1,3-bis(trifluoromethyl)benzene,
1,4-bis(trifluoromethyl)benzene, 1,1,1,3,3-pentafluoropropane,
1,1,1,3,3-pentafluorobutane, heptafluorocyclopentane, and perfluorinated cyclic ethers.
5. A process according to claim 1, wherein said crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate is brought into contact with a mixture of said poor solvent and a good solvent that is in an amount of not greater than 30 parts by weight per 100 parts by weight of said poor solvent, said good solvent being such that 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate has a higher solubility in said good solvent than in said poor solvent.
6. A process according to claim 5, wherein said good solvent is at least one selected from the group consisting of ethers and alcohols.
7. A process according to claim 6, wherein each of said ethers has a boiling point of about 30-140° C.
8. A process according to claim 6, wherein said ethers are diethyl ether, dibutyl ether, t-butyl methyl ether, diisopropyl ether, and tetrahydrofuran.
9. A process according to claim 6, wherein said alcohols are methanol, ethanol, n-propanol, isopropanol, and n-butanol.
10. A process according to claim 1, wherein said crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate is prepared by reacting 1,1,1-trifluoroacetone with an ester of trifluoroacetic acid.
11. A process for purifying a crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate containing an impurity, said process comprising precipitating crystals of 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate from a solution of said crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate.
12. A process according to claim 11, wherein said precipitating is conducted by adding a poor solvent, in which 1,1,1,5,5,5-hexafluoroacetylacetone is substantially insoluble, to said solution containing a good solvent in which 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate has a higher solubility than in said poor solvent.
13. A process according to claim 12, wherein said poor solvent has a boiling point of not higher than about 200° C.
14. A process according to claim 12, wherein said poor solvent is at least one selected from the group consisting of aromatic hydrocarbons, aliphatic hydrocarbons, alicyclic hydrocarbons, industrial gasolines, and fluorine-containing solvents.
15. A process according to claim 14, wherein said aromatic hydrocarbons are benzene, toluene, o-xylene, m-xylene, p-xylene, ethyl benzene, and mesitylene,
wherein said aliphatic hydrocarbons are n-pentane, n-hexane, n-heptane, n-octane, n-nonane, n-decane, and isomers thereof, each of said isomers being in a liquid at about 5° C.,
wherein said alicyclic hydrocarbons are cyclopentane, cyclohexane, methylcyclopentane, methylcyclohexane, tetralin, and decalin,
wherein said industrial gasolines are ligroin and petroleum ether,
wherein said fluorine-containing solvents are
1,2-bis(trifluoromethyl)benzene,
1,3-bis(trifluoromethyl)benzene,
1,4-bis(trifluoromethyl)benzene, 1,1,1,3,3-pentafluoropropane,
1,1,1,3,3-pentafluorobutane, heptafluorocyclopentane, and perfluorinated cyclic ethers.
16. A process according to claim 12, wherein said good solvent is at least one selected from the group consisting of ethers and alcohols.
17. A process according to claim 16, wherein each of said ethers has a boiling point of about 30-140° C.
18. A process according to claim 16, wherein said ethers are diethyl ether, dibutyl ether, t-butyl methyl ether, diisopropyl ether, and tetrahydrofuran.
19. A process according to claim 16, wherein said alcohols are methanol, ethanol, n-propanol, isopropanol, and n-butanol.
20. A process according to claim 11, wherein said crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate is prepared by reacting 1,1,1-trifluoroacetone with an ester of trifluoroacetic acid.
21. A process according to claim 11, wherein said precipitating is conducted by lowering temperature of said solution.
22. A process according to claim 12, wherein said solution further contains a poor solvent in which 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate is substantially insoluble.
Description
BACKGROUND OF THE INVENTION

[0001] The present invention relates to a process for producing 1,1,1,5,5,5-hexafluoroacetylacetone with high purity, which is useful as a raw material for producing medicines, agricultural chemicals and low-boiling-point chelate compounds used in the process for manufacturing electric parts.

[0002] H. Gilman et al., J. Am. Chem. Soc., Vol. 78, pp. 2790-2792 (1956) teaches a process for producing 1,1,1,5,5,5-hexafluoroacetylacetone, which is shown by the following reaction formulas:

[0003] A. Henne et al., J. Amer. Chem. Soc., Vol. 69, pp. 1819-1820 (1947) discloses a process for producing anhydrous 1,1,1,5,5,5-hexafluoroacetylacetone by turning a sodium salt of 1,1,1,5,5,5-hexafluoroacetylacetone into a copper chelate compound, then recrystallizing the copper chelate compound, and then removing the copper with hydrogen sulfide.

[0004] R. Haszeldine et al., J. Chem. Soc. London, 1951, pp. 609-612 discloses that a reaction liquid is treated with dilute sulfuric acid and then extracted with ether, and the resulting organic layer is distilled to obtain distillates over the range 36-90° C. It is disclosed therein that the portion of boiling point 85-90° C. appears to be 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate.

[0005] H. Gilman et al., J. Am. Chem. Soc., Vol. 78, pp. 2790-2792 (1956) further discloses the precipitation of 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate by concentrating an organic layer extracted with ether.

[0006] In general, raw materials, including 1,1,1,5,5,5-hexafluoroacetylacetone, for producing medicines, agricultural chemicals and electronic parts are required to have higher purity, as compared with raw materials for other uses.

SUMMARY OF THE INVENTION

[0007] It is therefore an object of the present invention to provide a process for producing 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate with high purity, which is an intermediate for 1,1,1,5,5,5-hexafluoroacetylacetone.

[0008] According to the present invention, there is provided a first process for purifying a crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate containing an impurity. The first process comprises bringing said crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate into contact with a poor solvent, thereby removing said impurity from said crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate. In the specification, “poor solvent” means an organic solvent in which 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate is substantially insoluble.

[0009] According to the present invention, there is provided a second process for purifying a crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate containing an impurity. The second process comprises precipitating crystals of 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate from a specific solution of said crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate.

DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0010] The process for producing a crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate, which is to be purified by the first or second process of the invention, is not particularly limited. For example, such crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate can be produced, as follows. At first, a reaction vessel is charged with a reaction solvent and a base. Then, a mixture of 1,1,1-trifluoroacetone, a trifluoroacetic acid ester and a solvent is gradually added to the reaction vessel with stirring or the like to homogenize the reaction mixture, while the reaction mixture was maintained at a predetermined temperature lower than the reaction temperature. Then, according to need, the temperature of the reaction vessel is raised to accelerate the reaction, thereby forming a salt of 1,1,1,5,5,5-hexafluoroacetylacetone.

[0011] In the process for producing a crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate, the reaction vessel may be made of glass, fluororesin or a material lined with one of these. The reaction solvent may be an ether having a boiling point preferably of about 30-140° C. Examples of such ether are diethyl ether, dibutyl ether, t-butyl methyl ether, diisopropyl ether, and tetrahydrofuran (THF). The base may be an inorganic base. Examples of this inorganic base are alkali metals and alkali earth metals, alkoxides of such metals, and hydrides of such metals. More concrete examples are sodium methoxide, sodium ethoxide, sodium hydride, sodium, potassium methoxide, potassium ethoxide, potassium hydride, potassium, and lithium hydride. The trifluoroacetic acid ester is not particularly limited, since its ester moiety acts as a leaving group. Its examples may be methyltrifluoroacetate and ethyltrifluoroacetate, which are easily available in an industrial scale. The solvent for dissolving 1,1,1-trifluoroacetone and the trifluoroacetic acid ester may or may not be the same ether as that for the reaction solvent. As mentioned above, a mixture of 1,1,1-trifluoroacetone, a trifluoroacetic acid ester, and a solvent may be added to the reaction vessel, in view of operability of the reaction. It is, however, not necessary to mix these components to be added to the reaction vessel. Furthermore, this solvent may be omitted. As mentioned above, it is preferable to cool the reaction mixture during the addition of these components in order to prevent the temperature increase. The reaction temperature is preferably about 0-90° C., more preferably about 20-70° C. If it is lower than 0° C., the reaction rate may become too low. If it is higher than 90° C., the yield of 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate may become too low.

[0012] After the completion of the above reaction, a salt of crude 1,1,1,5,5,5-hexafluoroacetylacetone is obtained by removing the reaction solvent. The removal of the reaction solvent is conducted by applying heat and/or vacuum. After that, the reaction liquid of the residue is put into another reaction vessel, followed by the addition of water and then acid (e.g., sulfuric acid, hydrochloric acid, or nitric acid), thereby decomposing the salt. Then, solvent extraction is conducted by adding a solvent to the reaction liquid. Then, the solvent is removed from the obtained organic layer, thereby obtaining a crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate containing impurities, in the form of solid.

[0013] In the first process, the manner of bringing the crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate into contact with a poor solvent is not particularly limited. For example, the crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate may be dispersed in the poor solvent. Then, the precipitated 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate can be separated by filtration. As another example, it is possible to apply the poor solvent as a washing liquid to the crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate supported on a filter of a filtration device. The resulting 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate is usually dried. However, if it is used as a raw material for producing 1,1,1,5,5,5-hexafluoroacetylacetone, the drying is not necessary.

[0014] In the second process, it is possible to dissolve the crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate in an organic solvent to form a solution. To this solution it is possible to add a poor solvent, thereby precipitating 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate. Then, this product can be separated by filtration. Alternatively, the above solution can be cooled to reduce solubility, thereby precipitating 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate.

[0015] The temperature for conducting the above-mentioned procedures is not particularly limited. It is preferably about 0-90° C., more preferably about 20-60° C. In view of operability, it is preferably a temperature requiring no heating nor cooling.

[0016] The above-mentioned poor solvent used in the first or second process can be selected from hydrocarbons and fluorine-containing solvents free from chlorine. It is needless to say that this poor solvent is in the form of liquid upon its use. This poor solvent is not particularly limited, and its boiling point is preferably not higher than about 200° C. Examples of the hydrocarbons are (1) aliphatic hydrocarbons such as n-pentane, n-hexane, n-heptane, n-octane, n-nonane, n-decane and isomers of these, the isomers being in liquid at about 5° C.; (2) aromatic hydrocarbons such as benzene, toluene, o-xylene, m-xylene, p-xylene, ethyl benzene, and mesitylene; (3) alicyclic hydrocarbons such as cyclopentane, cyclohexane, methylcyclopentane, methylcyclohexane, tetralin, and decalin; and (4) industrial gasolines (mixtures of hydrocarbon solvents) such as ligroin and petroleum ether. Examples of the fluorine-containing solvents are

[0017] 1,2-bis(trifluoromethyl)benzene,

[0018] 1,3-bis(trifluoromethyl)benzene,

[0019] 1,4-bis(trifluoromethyl)benzene, 1,1,1,3,3-pentafluoropropane,

[0020] 1,1,1,3,3-pentafluorobutane, heptafluorocyclopentane, and perfluorinated cyclic ethers (FLORINAT®). It is possible to use a mixture of at least two of these.

[0021] In the first process, it is optional to mix the poor solvent with a small amount of a good solvent in which solubility of 1,1,1,5,5,5-hexafluoroacetylacetone is higher than in the poor solvent. The amount of the good solvent may be not greater than 30 parts by weight per 100 parts by weight of the poor solvent. The good solvent in the invention is not particularly limited. Its examples are ethers such as diethyl ether, dibutyl ether, t-butyl methyl ether, diisopropyl ether, and tetrahydrofuran (THF); and alcohols such as methanol, ethanol, n-propanol, isopropanol, and n-butanol.

[0022] In the second process, it is optional to add a poor solvent to the solvent used for preparing the solution of the crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate, in order to adjust the solubility in the solution. This addition is particularly preferable, if crystals of 1,1,1,5,5,5-hexafluoroacetylacetone are precipitated by lowering the temperature of the solution.

[0023] It is possible to dehydrate 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate, which has been purified in accordance with the invention, by a conventional method, thereby obtaining its anhydride. R. Belford, J. Inorganic and Nuclear Chemistry, 1956, Vol. 2, pp. 11-31 discloses such method in which a dispersion is prepared by shaking 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate with approximately three times its volume of 98% sulfuric acid. After the dispersion has been allowed to stand overnight, dehydration of the product is repeated with a fresh batch of sulfuric acid. The resulting upper layer is siphoned off and distilled, thereby obtaining the anhydride (yield: 98%) as a distillate between 70.0-70.2° C. J. Amer. Chem. Soc., 78, 2790 (1956) discloses another method in which anhydrous calcium sulfate is mixed with 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate. Then, the resulting mixture is heated. The distillate is again treated with anhydrous calcium sulfate and distilled, thereby obtaining the anhydride of a boiling point of 68° C. (736 mm.). There is known a still another method in which 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate, together with phosphorus pentoxide, is heated in ether.

[0024] The following nonlimitative examples are illustrative of the present invention.

EXAMPLE 1 Production of 1,1,1,5,5,5-Hexafluoroacetylacetone Dihydrate

[0025] A 500-ml three-necked flask, equipped with a thermometer, a dropping funnel and a reflux condenser, was charged with 34.6 g (0.64 mol) of sodium methoxide and 240 ml of t-butyl methyl ether. A mixture was prepared by mixing together 71.7 g (0.64 mol) of 1,1,1-trifluoroacetone, 90.9 g (0.64 mol) of ethyltrifluoroacetate, and 120 ml of t-butyl methyl ether. Then, the mixture was dropped into the flask by spending 30 min, while the reaction mixture was maintained at a temperature of not higher than 30° C. with stirring by a magnetic mixer. After the completion of the dropping, the reaction was conducted for 4 hr at 40° C.. After the reaction, the reaction product was concentrated by distilling t-butyl methyl ether off using an evaporator, thereby obtaining a sodium salt of a crude 1,1,1,5,5,5-hexafluoroacetylacetone. This sodium salt was put into a 500-ml three-necked flask equipped with a thermometer and a reflux condenser. Then, 120 ml of water were added. Then, 160 g of 24% sulfuric acid aqueous solution were added at a temperature of not higher than 20° C. with stirring by a magnetic mixer. Then, the reaction was conducted for 6 hr at 60° C., followed by cooling to room temperature. The resulting reaction liquid was extracted with 200 ml of t-butyl methyl ether. The resulting water layer was again extracted with 100 ml of t-butyl methyl ether. The total of these organic layers was distilled with an evaporator to remove t-butyl methyl ether, thereby obtaining 118.8 g of a crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate.

Production of 1,1,1,5,5,5-Hexafluoroacetylacetone

[0026] As shown in Table, 12 ml of toluene were added to 6.0 g of the obtained crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate. The resulting mixture was stirred for 1 hr at room temperature with a magnetic mixer, followed by filtration and drying, thereby obtaining 5.3 g of 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate. Then, a 20-ml eggplant-type flask was charged with 5.3 g of the obtained 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate and 20 g of 98% sulfuric acid. Then, the flask was stopped, and the mixture was stirred for 4 hr at room temperature with a magnetic mixer, followed by standing still for 1 hr to have two layers separated from each other. Then, 4.0 g of 1,1,1,5,5,5-hexafluoroacetone were obtained from the organic layer. This product was found by a gas chromatography (detector: FID, column: DB-1, column size: 0.25 mm×60 m) to be 1,1,1,5,5,5-hexafluoroacetone having a purity of 99.9% (areal % in gas chromatography).

EXAMPLES 2-1- 2-8 Production of 1,1,1,5,5,5-Hexafluoroacetylacetone

[0027] In each of Examples 2-1 to 2-8, the production of 1,1,1,5,5,5-hexafluoroacetylacetone of Example 1 was repeated except that a solvent shown in Table was added to 6.0 g of the crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate obtained in Example 1. The results are shown in Table.

TABLE
Purity of
Yield after Yield after 1,1,1,5,5,5-
Puri- De- Hexafluoro-
fication hydration acetylacetone
Solvent (g) (g) (areal %)
Example 1 toluene 12 ml 5.3 4.0 99.9
Example 2-1 n-hexane 12 ml 5.4 4.1 99.8
Example 2-2 n-hexane 10 ml & 5.2 4.0 99.8
t-butyl methyl
ether 2 ml
Example 2-3 n-hexane 10 ml & 4.2 3.2 99.9
THF 2 ml
Example 2-4 n-hexane 11 ml & 5.0 3.8 99.7
methanol 2 ml
Example 2-5 toluene 10 ml & 3.9 3.0 99.9
THF 2 ml
Example 2-6 toluene 10 ml & 4.8 3.7 99.9
t-butyl methyl
ether 2 ml
Example 2-7 toluene 10 ml & 5.3 4.1 99.9
dibutyl ether 2 ml
Example 2-8 1,3-bis(trifluoro- 5.1 3.9 99.8
methyl)benzene
12 ml
Example 3 toluene 70 ml 27.3 21.0 99.9
Com. Ex. No Solvent 29.1 21.3 93.5
Treatment

EXAMPLE 3 Production of 1,1,1,5,5,5-Hexafluoroacetylacetone Dihydrate

[0028] A 300-ml three-necked flask, equipped with a thermometer, a dropping funnel and a reflux condenser, was charged with 8.67 g (0.16 mol) of sodium methoxide and 60 ml of dibutyl ether. A mixture was prepared by mixing together 18.0 g (0.16 mol) of 1,1,1-trifluoroacetone, 22.8 g (0.16 mol) of ethyltrifluoroacetate, and 30 ml of dibutyl ether. Then, the mixture was dropped into the flask by spending 30 min, while the reaction mixture was maintained at a temperature of not higher than 30° C. with stirring by a magnetic mixer. After the completion of the dropping, the reaction was conducted for 4 hr at 40° C. After the reaction, the reaction product was concentrated by distilling dibutyl ether off with an evaporator, thereby obtaining a sodium salt of a crude 1,1,1,5,5,5-hexafluoroacetylacetone. This sodium salt was put into a 300-ml three-necked flask equipped with a thermometer and a reflux condenser. Then, 30 ml of water were added. Then, 40 g of 24% sulfuric acid aqueous solution were added at a temperature of not higher than 20° C. with stirring by a magnetic mixer. Then, the reaction was conducted for 6 hr at 60° C., followed by cooling to room temperature. The resulting reaction liquid was extracted with 50 ml of THF. The resulting water layer was again extracted with 40 ml of THF. The total of these organic layers was distilled with an evaporator to remove THF, thereby obtaining a crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate.

Production of 1,1,1,5,5,5-Hexafluoroacetylacetone

[0029] To the obtained crude 1,1,1,5,5,5 -hexafluoroacetylacetone dihydrate 70 ml of toluene were added, followed by stirring for 1 hr at room temperature with a magnetic mixer, then filtration and then drying, thereby obtaining 27.3 g of 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate (see Table). A 100-ml glass reaction vessel, equipped with a thermometer, a stirrer and a reflux condenser filled with glass spheres, was charged with 27.3 g of the obtained 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate and 55 g of 98% sulfuric acid, while nitrogen gas was allowed to flow through the reaction vessel. Then, the mixture was gradually heated to 80° C. with stirring by a magnetic mixer. During this heating, 21.0 g of a distillate of about 70° C. was collected. This distillate was found by the same gas chromatography as that of Example 1 to be 1,1,1,5,5,5-hexafluoroacetylacetone having a purity of 99.9%.

COMPARATIVE EXAMPLE Production of 1,1,1,5,5,5-Hexafluoroacetylacetone Dihydrate

[0030] The production of 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate of Example 3 was repeated, thereby obtaining 29.1 g of a crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate.

Production of 1,1,1,5,5-Hexafluoroacetylacetone

[0031] A 100-ml glass reaction vessel, which is the same as that of Example 3, was charged with 29.1 g of the obtained crude 1,1,1,5,5,5-hexafluoroacetylacetone dihydrate and 58 g of 98% sulfuric acid. Then, the mixture was gradually heated to 80° C. with stirring by a magnetic mixer. During this heating, 21.3 g of a distillate of 70° C. was collected. This distillate was found by the same gas chromatography as that of Example 1 to be 1,1,1,5,5,5-hexafluoroacetylacetone having a purity of 93.5%.

[0032] The entire disclosure of Japanese Patent Application No. 2000-000526 filed on Jan. 5, 2000, including specification, claims and summary, is incorporated herein by reference in its entirety.

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Classifications
U.S. Classification568/410, 568/382, 570/123, 570/177, 570/180
International ClassificationC07C45/45, C07C45/81, C07C45/79, C07C49/167
Cooperative ClassificationC07C45/81, C07C45/79, C07C45/455
European ClassificationC07C45/81, C07C45/45F, C07C45/79
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Apr 25, 2001ASAssignment
Owner name: CENTRAL GLASS COMPANY, LIMITED, JAPAN
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