Patent Application
20110150747
The present invention relates to a method for manufacturing an oxygen-containing halogenated fluoride.
An oxygen-containing halogenated fluoride is utilized as a monofluoromethylation agent for production of 1-fluoro-1,1-bis(arylsulfonyl)methane, which is a physiologically active substance useful as a pharmaceutical product (cf. Patent Document 1).
As methods for manufacturing the oxygen-containing halogenated fluoride, it is conventionally known to produce ClO2F by, for example, reaction of Cl2O and ClF (Non-Patent Document 1) and reaction of ClF5 and CsNO3 (Non-Patent Document 2).
These manufacturing methods of the oxygen-containing halogenated fluoride each generally involve a solid-gas reaction or a reaction using an explosive compound. As F2 gas or fluoride gas used in the solid-gas reaction is a very active substance, the temperature increases with the progress of the reaction. The development of such temperature increase can result in the occurrence of an explosive reaction or decomposition of the solid raw material. It is thus necessary in the above conventional manufacturing methods to prevent temperature increases, which makes it difficult to produce the target oxygen-containing halogenated fluoride efficiently and continuously.
On the other hand, there has been no report made on a method for manufacturing the oxygen-containing halogenated fluoride by a solid-gas reaction process.
The present invention has been made in order to solve the above problems. It is therefore an object of the present invention to provide a method for producing an oxygen-containing halogenated fluoride efficiently and continuously.
As a result of extensive researches, the present inventors have found that a gas-liquid reaction process can suitably be used for production of an oxygen-containing halogenated fluoride. The present invention is based on this finding.
Namely, there is provided according to the present invention a method for manufacturing an oxygen-containing halogenated fluoride of the general formula: XO2F, the method comprising reacting a halogen fluoride of the general formula: XF with a H2O source, where X represents a halogen element selected from Cl, Br and I in the general formulas.
Hereinafter, the present invention will be described in detail.
In the present invention, an oxygen-containing halogenated fluoride of the general formula: XO2F is produced by reaction of a halogen fluoride of the general formula: XF with an H2O source. Herein, X represents a halogen element selected from Cl, Br and I in the general formulas.
Examples of the halogen fluoride XF used as raw material gas are ClF3, IF3, IF7, IF5, CIF, BrF, BrF3 and BrF5.
Examples of the H2O source used as raw material liquid are water and aqueous solutions with a pH of 1 to 13, such as an aqueous HF solution, an aqueous KF solution, an aqueous KOH solution, an aqueous NaOH solution, an aqueous K2CO3 solution, an aqueous NaF solution and an aqueous Al(OH)2 suspended solution. There is no particular limitation on the temperature of use of the raw material liquid.
Specific examples of the oxygen-containing halogenated fluride XO2F produced by the gas-liquid reaction of the halogen fluoride XF and the H2O source according to the present invention are ClO2F, BrO2F and IO2F.
Either a counter-flow contact technique or a parallel-flow contact technique can be adopted for the gas-liquid contact reaction of the raw material gas and the raw material liquid. Among others, the counter-flow contact is more preferred in view of the gas-contact contact efficiency. Further, there is no concern about the reaction temperature of the gas-liquid reaction of the raw material gas and the raw material liquid as long as the reaction temperature is that at which the raw material liquid can be brought in the form of a liquid into contact with the raw material gas.
There is no particular limitation on the production apparatus of the oxygen-containing halogenated fluoride XO2F according to the present invention as long as the production apparatus is equipped with a reactor for the contact reaction of the raw material gas and the raw material liquid and is so structured as to supply the raw material gas and the raw material liquid into the reactor and discharge the resulting gas from the reactor. The reactor may also include a mechanism for recirculation of the raw material liquid. There is also no particular limitation on the material of the reactor as long as the reactor material is sufficiently resistant to the raw material gas and the raw material liquid. Preferred examples of the reactor material are stainless steel, Ni steel, iron steel, Monel, Inconel and aluminium.
The diluent gas cylinder 1 and the raw material gas cylinder 2 store therein diluent gas (e.g. N2) and raw material gas (e.g. ClF3), respectively. The flow rates of the diluent gas and the raw material gas are controlled by the MFCs 3 and 4 so as to mix these gases to a predetermined gas composition and introduce the mixed gas into the reactor 5.
The reactor 5 has a packed tower 7 in which a filler is packed, a liquid chamber 10 provided with a sufficient capacity for storing therein the raw material liquid 8 and having an inner wall lined with polytetrafluoroethylene, and a liquid transfer pump 6 for transferring the raw material liquid 8 from the liquid chamber 10 to the top of the filler. The raw material gas is introduced into the packed tower 7 from the bottom and brought into counter contact with the raw material liquid 8 within the packed tower 7. The resulting gas is discharged from the top of the reactor 5.
The gas discharged from the reactor 5 is collected into the empty container 9. The gas collected in the container 9 is analyzed by a Fourier transform infrared spectrometer (FT-IR) etc. to determine the concentration of the produced oxygen-containing halogenated fluoride XO2F (e.g. ClO2F) in the gas.
As described above, the present invention adopts the gas-liquid reaction of the halogen fluoride and the H2O source so that it is easier to control the temperature of the reaction than that of the conventional solid-gas reaction or reaction using explosive compound and is thus possible to produce the target oxygen-containing halogenated fluoride XO2F efficiently and continuously.
The oxygen-containing halogenated fluoride XO2F obtained according to the present invention can be utilized as a selective fluorination agent for fluorination at the α-position of an ester.
The present invention will be described in more detail below by way of the following examples. It should be noted that these examples are illustrative and are not intended to limit the present invention thereto.
Using the above-mentioned production apparatus, the gas-liquid reaction of the halogen fluoride XF and H2O source was carried out. In the reactor 5, a tube of SUS316 having a length of 650 mm, an inner diameter of 25 mm and an inner wall lining of polytetrafluoroethylene with a thickness of 0.1 mm was used as the packed tower 7; and 4φ PTFE (polytetrafluoroethylene) Raschig ring was packed as the filler in the packed tower 7. Further, F2 gas and ClF3 gas were used as the diluent gas and the raw material gas (halogen fluoride XF), respectively. The flow rates of these gases were controlled by the MFCs 3 and 4 in such a manner as to provide a mixed gas with a gas composition of ClF3: N2=2 vol %:98 vol %. As the raw material liquid 8 (H2O source), an aqueous solution of 4.0 mass % hydrogen fluoride (pH=1) was used. The above-prepared mixed gas was introduced into the reactor 5 at a flow rate of 0.274 l/min (superficial linear velocity of 9.31×10−3 m/sec) and at a reaction temperature of 24° C. After that, the gas discharged from the reactor 5 was collected into the empty container 9.
The concentration of ClO2F in the gas collected in the empty container 9 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.). As a result, the ClO2F concentration was 3872 ppm. The generation of ClO2F was thus confirmed. The product yield on Cl basis was 19.36%.
The gas-liquid reaction was carried out under the same conditions as in Example 1, except that the gas composition of the mixed gas was controlled to ClF3: N2=4.4 vol %:95.6 vol % by the MFCs 3 and 4. The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Example 1.
As a result, the ClO2F concentration was 10864 ppm; and the generation of ClO2F was confirmed. The product yield on Cl basis was 24.69%.
The gas-liquid reaction was carried out under the same conditions as in Example 1, except that the gas composition of the mixed gas was controlled to ClF3: N2=6.2 vol %:93.8 vol % by the MFCs 3 and 4. The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Example 1.
As a result, the ClO2F concentration was 19562 ppm; and the generation of ClO2F was confirmed. The product yield on Cl basis was 31.55%.
The gas-liquid reaction was carried out under the same conditions as in Example 1, except that the gas composition of the mixed gas was controlled to ClF3: N2=24.8 vol %:75.2 vol % by the MFCs 3 and 4. The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Example 1.
As a result, the ClO2F concentration was 70672 ppm; and the generation of ClO2F was confirmed. The product yield on Cl basis was 28.50%.
The gas-liquid reaction was carried out under the same conditions as in Example 1, except that: the gas composition of the mixed was controlled to ClF3: N2=2 vol %:98 vol % by the MFCs 3 and 4; and the mixed gas was introduced into the reactor 5 at a flow rate of 1.0961/min (superficial linear velocity of 3.72×10−2 m/sec). The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Example 1.
As a result, the ClO2F concentration was 3569 ppm; and the generation of ClO2F was confirmed. The product yield on Cl basis was 17.85%.
The gas-liquid reaction was carried out under the same conditions as in Example 1, except that: the gas composition of the mixed gas was controlled to ClF3:N2=10 vol %:90 vol % by the MFCs 3 and 4; and the mixed gas was introduced into the reactor 5 at a flow rate of 1.096 l/min (superficial linear velocity of 3.72×10−2 m/sec). The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Example 1.
As a result, the ClO2F concentration was 8901 ppm; and the generation of ClO2F was confirmed. The product yield on Cl basis was 8.90%.
The gas-liquid reaction was carried out under the same conditions as in Example 1, except that: the gas composition of the mixed gas was controlled to ClF3:N2=6.9 vol %:93.1 vol % by the MFCs 3 and 4; and the mixed gas was introduced into the reactor 5 at a flow rate of 1.096 l/min (superficial linear velocity of 3.72×10−2 m/sec). The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Example 1.
As a result, the ClO2F concentration was 8434 ppm; and the generation of ClO2F was confirmed. The product yield on Cl basis was 12.22%.
The gas-liquid reaction was carried out under the same conditions as in Example 1, except that: an aqueous suspended solution of 5 mass % aluminum hydroxide (pH=7) was used as the raw material liquid 8; the gas composition of the mixed gas was controlled to ClF3:N2=4.3 vol %:95.7 vol % by the MFCs 3 and 4; and the reaction temperature was set to 40° C. The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Example 1.
As a result, the ClO2F concentration was 3076 ppm; and the generation of ClO2F was confirmed. The product yield on Cl basis was 7.15%.
The gas-liquid reaction was carried out under the same conditions as in Example 1, except that: water (pH=7) was used as the raw material liquid 8; and the gas composition of the mixed gas was controlled to ClF3: N2=2.7 vol %:97.3 vol % by the MFCs 3 and 4. The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Example 1.
As a result, the ClO2F concentration was 14879 ppm; and the generation of ClO2F was confirmed. The product yield on Cl basis was 55.11%.
The gas-liquid reaction was carried out under the same conditions as in Example 9, except that the gas composition of the mixed gas was controlled to ClF3:N2=5.6 vol %:94.4 vol % by the MFCs 3 and 4. The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Example 9.
As a result, the ClO2F concentration was 22765 ppm; and the generation of ClO2F was confirmed. The product yield on Cl basis was 40.65%.
The gas-liquid reaction was carried out under the same conditions as in Example 1, except that: an aqueous solution of 40 mass % potassium hydroxide (pH=13) was used as the raw material liquid 8; and the gas composition of the mixed gas was controlled to ClF3: N2=2.7 vol %:97.3 vol % by the MFCs 3 and 4. The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Example 1.
As a result, the ClO2F concentration was 9831 ppm; and the generation of ClO2F was confirmed. The product yield on Cl basis was 36.41%.
The gas-liquid reaction was carried out under the same conditions as in Example 1, except that: an aqueous solution of 10 mass % potassium carbonate (pH=10) was used as the raw material liquid 8; and the gas composition of the mixed gas was controlled to ClF3:N2=2.7 vol %:97.3 vol % by the MFCs 3 and 4. The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Example 1.
As a result, the ClO2F concentration was 9856 ppm; and the generation of ClO2F was confirmed. The product yield on Cl basis was 36.50%.
The gas-liquid reaction was carried out under the same conditions as in Example 9, except that: the gas composition of the mixed gas was controlled to ClF3:N2=0 vol %:100 vol % by the MFCs 3 and 4; and the mixed gas was introduced into the reactor 5 at a flow rate of 0.274 l/min. The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Example 9.
As a result, the generation of ClO2F was not confirmed.
The gas-liquid reaction was carried out under the same conditions as in Comparative Example 1, except that an aqueous solution of 4.0 mass % hydrogen fluoride (pH=1) was used as the raw material liquid 8. The concentration of ClO2F in the gas collected after discharged from the reactor 5 was analyzed by a FT-IR (“IG-1000” available from Otsuka Electronics Co., Ltd.) in the same manner as in Comparative Example 1.
As a result, the generation of ClO2F was not confirmed.
The above measurements results are indicated in TABLE 1.
As seen in TABLE 1, the ClO2F was produced with favorable yield by the gas-liquid reaction of the ClF3 and the H2O source (water or aqueous solution) in Examples 1 to 12. The temperature control was easier in the gas-liquid reaction than in the conventional solid-gas reaction or reaction using explosive compound.
It has thus been shown that it is possible to produce the target oxygen-containing halogenated fluoride XO2F efficiently and continuously by the gas-liquid reaction of the halogen fluoride and the H2O source.
Although the present invention has been described with reference to the above specific embodiments, the invention is not limited to these exemplary embodiments. Various modifications and variations of the embodiments described above will occur to those skilled in the art without departing from the scope of the present invention.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2008-144616 | Jun 2008 | JP | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/JP2009/058357 | 4/28/2009 | WO | 00 | 11/5/2010 |
