Patent Application
20080145304
This invention relates to inorganic chemistry and a method of manufacturing a manganese compound and more particularly to a method of manufacturing a halogenated product thereof, i.e. a method of manufacturing manganese tetrafluoride, MnF4.
Manganese tetrafluoride is used in the chemical industry as a strong oxidizing agent and as a source of manufacture for pure fluorine. As regards manganese tetrafluoride, for example, there is known a method of manufacturing fluorine [Russian Federation Patent 2,221,739, Class C01B 7/20, Date of Publication: Apr. 1, 2004]. This method employs as starting compounds, for example, salts having a high fluorine content (potassium hexafluoride, KF6 and manganese tetrafluoride, MnF4) and other salts, such as K3NiF7, K2NiF6 and K2CuF6 and compounds similar to them.
There is also known a method of manufacturing MnF4 which employs terbium tetrafluoride as a fluorinating agent and performs the fluorination of MnF2 by condensing a vapor product obtained at a high temperature (380-460° C.) under a pressure of 10−1 to 10−5 torr [Soviet Union Inventor Certificate 1,428,702, Class C01G 45/06, Date of Publication: Oct. 7, 1988]. Such use of a fluorinating agent makes the separation of a product difficult and brings about an increase of cost.
There is also a description concerning a method of manufacturing manganese tetrafluoride, including a method of manufacture from manganese difluoride and manganese tri-fluoride [Russian Journal of Inorganic Chemistry, Vol. 43, No. 4, 1998, pp. 465-469, Synthesis of Manganese Tetrafluoride at Atmospheric Pressure] . This description shows that a method of manufacture from manganese trifluoride has an advantage. This method is carried out in a reactor having a cooling device in its inside and a solid product is formed around the cooling device. A starting substance (MnF3) in the form of tablets in the amount of about 90 to 120 g is placed in a heating region around the cooling device. Fluorination takes place at a temperature of 450-700° C. and fluorine feed rate of 3.2-12.6 g/h. For continuing fluorination, the product which has been formed is shaken off into a collector every five minutes by a vibration method or by using a cylinder type scraper, whereby a grayish blue powder of manganese tetrafluoride is obtained.
There is a method of obtaining MnF4 as an intermediate product by the synthesis of fluorine gas [Soviet Union Inventor Certificate 1,432,001, Class C01G 45/06, Publication Number: 1,932,001]. It describes the stage of preparing MnF4 from manganese trifluoride, MnF3. Manganese trifluoride is fluorinated by industrial fluorine at a temperature of 450-650° C. and the resulting manganese tetrafluoride is condensed at (70° C. or less) . When MnF4 is used, fluorine gas is obtained in accordance with the following reaction formula:
MnF4→MnF3+½F2
The above patent describes a method of manufacture which obtains MnF4 by interacting MnF3 in a gas stream containing fluorine at a temperature of 450-650° C. to sublimate MnF4 and condensing its vapor at a temperature of 70° C. or below. Then, the manganese tetrafluoride as obtained is heated to 70-300° C. so that fluorine gas of high purity maybe obtained. Drawbacks of this method lie in a low conversion to MnF4 and the necessity for complicated equipment for sublimation by heating and collection for the synthesis of MnF4. Another drawback thereof lies in that the necessity of carrying out processes for sublimation and condensation makes it difficult to organize commercial production.
We have made an attempt to synthesize MnF4 by reacting MnF2 with fluorine gas without sublimating MnF4. This attempt has, however, ended in the melting and vitrification of the compound. Thus, it has been confirmed that it is impossible to obtain MnF4 by a simple process as in the past.
It has been found during the process of work that the fluorination of the starting manganese salt proceeds on the surfaces of its particles and is accompanied by the sintering of the particles which obstructs the penetration of fluorine into the particles.
We, the inventors of this proposed invention, have found it necessary to solve the object of carrying out the method in a manner ensuring the complete fluorination of the salt, or the problem of having fluorine penetrate into the deepest possible interior of the particles. This object is attained by a method including grinding any starting compound and solid particles under reaction.
The method of manufacturing manganese tetrafluoride according to the present invention is characterized by reacting a manganese compound and a fluorinating agent at a temperature of 250-350° C. and a pressure of 1.0-10.0 MPa to fluorinate the compound, while constantly or discontinuously crushing or grinding the starting compound and the manganese compound being reacted.
The starting compound and the manganese compound being reacted are crushed or ground constantly or discontinuously in a reactor without being removed therefrom.
The starting compound and the manganese compound being reacted are crushed or ground constantly or discontinuously in a ball mill or a rod mill in a reactor without being removed from the reactor.
As the starting compound, one or more divalent manganese compounds selected from the group consisting of MnF2, MnF2 hydrate, MnCl2, MnCO3 and MnO are used.
The starting compound preferably comprises MnF2 and/or its hydrate.
The fluorinating agent comprises one or more substances selected from among F2, ClF and ClF3.
The fluorinating agent preferably comprises F2.
The starting compound is pre-treated with an inert gas having a dew point of −40° C. or below at a temperature of 100-400° C.
This invention is essentially characterized by not relying upon sublimation at a high temperature and the cooling and condensation of a product thereof for the fluorination of a manganese compound by a fluorinating agent, but performing its fluorination in its solid form at a temperature of 250-350° C. and a pressure of 1.0-10.0 MPa, while grinding the starting compound and reaction product constantly or discontinuously. This method is characterized by treating the starting manganese compound with an inert gas having a dew point of −40° C. or below, preferably −60° C. or below at a temperature of 100-400° C., preferably 150-350° C. before or while the method is carried out. This method is preferably carried out in a reactor containing a grinding apparatus, for example, a ball mill or a rod mill.
In connection with this invention, we express the composition of the intended compound as MnF4, but as this compound usually partially contains an intermediate product from MnF2 to MnF4 and a dimmer thereof, its general composition is expressed as MnFx (x=3.5-4).
According to this invention relating to a method of manufacturing MnF4, it is possible to use as the manganese compound a commercially available divalent manganese compound, such as MnF2, MnCl2, MnCO3 or MnO. It is desirable to use first MnF2 as no removal of anions is necessary, and then MnCO3 in view of reactivity. The use of a hydrate of a manganese compound is also permissible, but is likely to form HF as a by-product. In order to avoid this, it is necessary to treat it with an inert gas having a dew point of −40° C. or below at a temperature of 150-350° C. This makes it possible to prevent the formation of a sintered product and thereby improve the speed and ratio of conversion to MnF4. Even when anhydrous MnF2 is used, for example, it is desirable to dry it before using it, since it contains a small amount of water.
Although no particular requirement is made as to the purity of MnF2, an excessively high percentage of impurities is likely to hinder fluorination. While a purity of 90% or above is, for example, considered satisfactory, a purity of 95% or above is more desirable and the optimum purity is 97% or above. The same is true with the purity of the fluorinating agent. Although no particular requirement is made, either, when, for example, F2 is used as the fluorinating agent, a purity of 95% or above is acceptable, a purity of 99% or above is more desirable and the optimum purity is 99.9% or above.
As to the particle diameter of MnF2, it is desirable to use particles having an average particle diameter of 0.4 mm or less, more desirably an average particle diameter of 100 μm or less and most desirably 10 μm or less, considering that the efficiency of fluorination depends on the surface area, and the surface area increases in inverse proportion to the particle diameter.
It is necessary to point out that MnF2 is often synthesized from MnCO3 and HF on a commercial basis (MnCO3+2HF→MnF2+CO2+H2O). The use of anhydrous MnF2 obtained by this method is recommended for the manufacture of MnF4. This makes possible a reduction in the cost of production.
For example, MnF2 obtained by taking the above factor into account is placed in a reaction vessel for preliminary drying. Its drying treatment is carried out for removing water of crystallization remaining from the process for MnF2 manufacture and water adhering to the surfaces of MnF2 crystals. Its drying is carried out as described below. Its water is removed by heating MnF2 at a low pressure. The efficient removal of water is achieved by repeating a cycle including interrupting a reduction of the pressure—purging with an inert gas (e.g. He) having a dew point of −40° C. or below and thereby raising the pressure—reducing the pressure again. While the percentage of water removal is improved with the number of times the cycle is repeated, five to ten times are usually sufficient for water removal. While a temperature of 100° C. is considered satisfactory for the purpose, a temperature of 300-400° C. makes drying more efficient.
One or more substances selected from among F2, ClF and ClF3 can be used as the fluorinating agent (or agents). Among these, a fluorinating agent containing F2 is preferred.
As regards the valence of manganese mentioned in connection with this invention, manganese fluoride was dissolved in an aqueous solution of nitric or hydrochloric acid, manganese was analyzed by ICP (inductively coupled plasma) spectrometry and fluorine by ion chromatography, and the ratio of manganese and fluorine in manganese fluoride was calculated.
The synthesis of MnF4 can be performed by the operation described above. If MnF4 as thereby obtained is heated in a nickel vessel, fluorine gas can be obtained. When the amount of impurities in the gas was measured by gas chromatography and infrared Fourier-transform spectrophotometry, a fluorine purity of 99.95% or more was confirmed.
The present invention will be described in more detail below with reference to the following Examples, however, the present invention should not be construed as being limited to these Examples.
In a glove box(6) having a controlled dew point, 4500 g of manganese difluoride (MnF2) were placed on the tray ((5) in
The reactor (4) was evacuated and supplied with fluorine gas until it had a pressure P of 2.0 MPa, and the reactor (4) was held at a temperature T of 250° C. until its pressure became constant.
When its pressure P dropped less than 1.0 MPa, the reactor (4) was supplied with fluorine gas until its pressure P rose to 2.0 MPa.
The process was regarded as having been completed when the pressure P of the reactor (4) was stabilized.
After the reactor (4) was evacuated and fed with nitrogen gas until its pressure reached the ambient pressure, a product of fluorine gas treatment was taken out.
The product was weighed and the composition of each reaction product was calculated in accordance with an increase in weight.
Then, the reaction product was ground in a slit type grinding mill (7) and placed in the reactor (4), in which the fluorinating operation as described above was repeated. The composition of the final product was analyzed by ICP and ion chromatography and the composition based on weight was ascertained.
Table 1 shows the test results based on the parameters mentioned above.
According to the example, the starting material and the reaction product after each run were each ground by a slit type grinding mill (7) and subjected discontinuously to fluorine gas treatment. If each grinding timing is shown by the above run numbers, it was before 1 (the starting material was ground by a slit type grinding mill (7)), between 1 and 2, between 2 and 3, between 3 and 4 and after 4 (the final product was ground) When fluorination treatment according to Run No. 2 was performed without any grinding done between Run Nos. 1 and 2, hardly any fluorination took place, and no MnF3.5 was obtained despite a long time spent.
In a glove box having a controlled dew point, a reactor (4) ((1) in
The reactor (4) was held until it had a constant temperature T of 250° C. The reactor (4) was evacuated and supplied with fluorine gas until it had a pressure P1 of 2.0 MPa, and it was closed. The reactor having a ball mill (4) was rotated to carry out the reaction, while the manganese compound was crushed and ground therein.
When an occasional check of pressure indicated a pressure P2 less than 1.0 MPa, the reactor (4) was supplied with fluorine gas until its pressure P1 of 2.0 MPa was recovered, and it was closed.
The process was regarded as having been completed when the pressure P of the reactor (4) was stabilized.
After the reactor (4) was evacuated and fed with nitrogen gas until its pressure reached the ambient pressure, a product of fluorine gas treatment was taken out.
The product was weighed and the composition of each reaction product was calculated in accordance with an increase in weight and the results of analyses by ICP and ion chromatography.
The test results are shown in Table 2.
Table 2 also shows the results obtained by varying the temperature T and pressures P (P1 and P2) as the parameters. When in each example, a pressure check indicated a pressure P2 less than X MPa, the reactor (4) was supplied with fluorine gas until its pressure P1 rose to Y MPa, and it was closed, and its pressure range, Y-X, was 1 MPa.
The reactor having a ball mill was kept rotating all the time except when it was supplied with fluorine, and when its conditions (including pressure) were checked. As is obvious from the results shown in Table 2, a higher temperature and a higher pressure tended to bring about a higher degree of fluorination. It was also found that a higher degree of fluorination than giving a composition expressed as, say, MnF3.7 was gradually less likely to occur.
In a glove box having a controlled dew point, the reactor (4) ((1) in
The reactor (4) was evacuated and supplied with fluorine gas until it had a pressure P1 of 6.0 MPa, and it was closed. The reactor having a ball mill was rotated to carry out the reaction, while the manganese compound was crushed and ground therein, and a heater was started to hold the reactor (4) until it had a constant temperature T of 300° C.
When an occasional check of pressure indicated a pressure P2 less than 5.0 MPa, the reactor (4) was supplied with fluorine gas until its pressure P1 of 6.0 MPa was recovered, and it was closed.
The process was regarded as having been completed when the pressure P of the reactor (4) was stabilized.
After the reactor (4) was evacuated and fed with nitrogen gas until its pressure reached the ambient pressure, a product of fluorine gas treatment was taken out.
The product was weighed and the composition of each reaction product was calculated in accordance with an increase in weight and the results of analyses by ICP and ion chromatography.
Tests were also conducted by employing different starting materials and the results are all shown in Table 3. When in each example, a pressure check indicated a pressure P2 less than X MPa, the reactor (4) was supplied with fluorine gas until its pressure P1 rose to Y MPa, and it was closed, and its pressure range, Y-X, was 1 MPa.
In a glove box having a controlled dew point, the reactor (4) ((1) in
The reactor (4) was held until it had a constant temperature T of 300° C. The reactor (4) was evacuated and supplied with chlorine trifluoride ClF3 until it had a pressure P1 of 2.0 MPa, and it was closed. The reactor having a ball mill was rotated to carry out the reaction, while the manganese compound was crushed and ground therein.
When an occasional check of pressure indicated a pressure P2 less than 1.0 MPa, the reactor (4) was supplied with chlorine trifluoride until its pressure P1 of 2.0 MPa was recovered, and it was closed.
The process was regarded as having been completed when the pressure P of the reactor (4) was stabilized.
After the reactor (4) was evacuated and fed with nitrogen gas until its pressure reached the ambient pressure, a product of fluorine gas treatment was taken out.
The product was weighed and the composition of each reaction product was calculated in accordance with an increase in weight and the results of analyses by ICP and ion chromatography.
The test results are shown in Table 4.
Table 4 also shows the results obtained by varying the fluorinating agent to chlorine fluoride ClF. When in each example, a pressure check indicated a pressure P2 less than X MPa, the reactor (4) was supplied with the fluorinating agent until its pressure P1 rose to Y MPa, and it was closed, and its pressure range, Y-X, was 1 MPa.
The intermediate products including chlorine were considered to be replaced by fluorine and the products had a chlorine content which was about 1% or less of fluorine.
The starting material was pre-treated in an inert gas having a dew point of −40° C. or below at a temperature of 100-400° C. to have a lower content of water of crystallization before its fluorinating treatment, so that fluorine having a lower HF content might be obtained upon heating the final product (MnF4).
In a glove box having a controlled dew point, the reactor (4) ((1) in
The reactor (4) was evacuated and while it was supplied with an inert gas having a dew point of −40° C. or below, the reactor (4) had its internal temperature T held at 100-400° C., whereby the starting materials (MnF2·xH2O) having different water contents were obtained.
The reactor (4) was held until it had a constant temperature T of 300° C. The reactor (4) was evacuated and supplied with fluorine gas until it had a pressure P1 of 6.0 MPa, and it was closed. The reactor having a ball mill was rotated to carry out the reaction, while the manganese compound was crushed and ground therein.
When an occasional check of pressure indicated a pressure P2 less than 5.0 MPa, the reactor (4) was supplied with fluorine gas until its pressure P1 of 6.0 MPa was recovered, and it was closed.
The process was regarded as having been completed when the pressure P of the reactor (4) was stabilized.
After the reactor (4) was evacuated and fed with nitrogen gas until its pressure reached the ambient pressure, a product of fluorine gas treatment was taken out.
The product was weighed and the composition of each reaction product was calculated in accordance with an increase in weight and the results of analyses.
Then, 450±5 g of each of the substances to be tested, as obtained by the process described above and having the general formula MnF3.86 or having a higher fluorine content was decomposed under heat in a decomposition reactor (10) as shown in
Each substance to be tested was heated to a temperature T of 380° C. so as to achieve the highest degree of fluorine decomposition.
The fluorine gas generated by the decomposition of each substance to be tested was collected in a receptacle cooled by liquid nitrogen at an absolute pressure of 273 mmHg.
After the receptacle was heated to the ambient temperature, the fluorine gas obtained by the decomposition under heat had its HF content analyzed by FT-IR.
The results are shown in Table 5.
Table 5 confirms that a starting material having a lower water content gives a final product generating fluorine having a lower hydrogen fluoride (HF) content.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2004128382 | Sep 2004 | RU | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/JP05/18205 | 9/22/2005 | WO | 00 | 3/23/2007 |
