JP2006035217A - Method for accelerating reaction of chemical substance utilizing ultrasonic wave - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for accelerating a reaction of a chemical substance utilizing an ultrasonic wave without performing an advanced refining process and capable of performing a continuous process from introducing raw materials to recovering a residual gas. <P>SOLUTION: This method for accelerating the reaction of the chemical substance utilizing the ultrasonic wave uses the steps of irradiating a decomposed formation gas of the chemical substance with the ultrasonic wave to generate a compressional wave thereby to induce molecular motion repeating high-speed inversion and to increase intense collision of mutual molecules and the frequency thereof, and of utilizing a compressed part becoming adiabatic compression by the ultrasonic wave to thereby become a locally high-temperature and high-pressure condition to accelerating the reaction of the chemical substance. <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

  The present invention relates to a reaction promoting method such as cleavage of a double bond of a chemical substance using ultrasonic waves.

It has been pointed out that chlorofluorocarbon gas, which has been used as a refrigerant, and halon gas, which has been used as a digestive agent, are environmental pollutants. Various countermeasures have been proposed. For example, hydrothermal reaction methods, incineration methods, explosion reaction decomposition methods, microbial decomposition methods, ultrasonic decomposition methods, plasma reaction methods, and the like have been proposed for chlorofluorocarbon treatment methods. Further, a means for disposing of CFCs R22 (CHClF ₂ ), which is a depleting substance of the ozone layer, is generally disposed of after being decomposed, but recently, attempts have been made to recycle and reuse the fluororesin. For example, a means has been devised in which chlorofluorocarbon R22 recovered from a used air conditioner or the like is purified after recovery and then used as a polytetrafluoroethylene resin material.

In general, polytetrafluoroethylene production methods include dechlorination of fluorinated chloroethane, thermal decomposition of lower aliphatics including C, F, H, Cl, Br, etc., heat of alkali metal salt of trifluoroacetic acid A decomposition method, a thermal decomposition method of PTFT, and the like are known. Industrially, a reaction tube made of platinum, silver, carbon or the like is used, and polytetrafluoroethylene is obtained by thermal decomposition at 650 ° C. to 800 ° C. by an unfilled flow method. The main by-product is C ₃ F ₆ (see Non-Patent Documents 1 and 2).
Fluorine resin handbook (Takaomi Satokawa, 1990, published by Nikkan Kogyo Shimbun) Development of fluorine-based materials (Masaaki Yamabe, Hitoshi Matsuo, 1997, issued by CMC Publishing Co., Ltd.)

However, the conventional means for recycling Freon R22 to fluorocarbon resin requires that the purity of Freon R22 as a raw material is high, while Freon R22 recovered from a home air conditioner contains moisture, oil, air, and the like. Therefore, there is a problem that it cannot be used as a raw material unless it is sufficiently purified to increase its purity. Furthermore, since harmful gas is generated as a by-product when ethylene tetrafluoride gas (CF ₂ = CF ₂ gas) is produced by a thermal decomposition method, there is a problem that it is difficult to treat this toxic gas. In addition, there is a problem in that it is impossible to continuously produce from fluorocarbon R22 as a raw material to polytetrafluoroethylene.

Further, even if tetrafluoroethylene gas (CF ₂ = CF ₂ gas) is produced by thermal decomposition, polymerization does not start unless the purity of this CF ₂ = CF ₂ gas is high. Therefore, the CF ₂ = CF ₂ gas is purified. Thus, it is necessary to increase the purity until the polymerization is started. On the other hand, when the purity is high, the polymerization is so intense that the polymerization cannot be started and stopped even at room temperature and normal pressure, and at this time, a large reaction heat is generated, which causes an explosion or a dangerous reaction. Also, to save the high-purity CF 2 ₌ CF ₂ gas must be stored in the -20 ° C. or less put polymerization inhibitor, still gradually polymerization.

In addition, there is a substance called Freon R23 (CHF ₃ ) in which one chlorine (Cl) of Freon R22 (CHClF ₂ ) is replaced with fluorine (F). This chlorofluorocarbon R23 is chlorofluorocarbon that is always produced as a by-product in producing fluorocarbon R22 as a raw material for fluororesin, and has no particularly important use. However, Freon R23 has been overlooked because it is not an ozone-depleting substance like Freon R22, but the index of global warming, which has recently become a major environmental problem, is more than 10,000 times that of carbon dioxide (Freon R22 is It is clear that there are about 1000 times), and the decomposition process is a big problem. On the other hand, since chlorofluorocarbon R23 does not contain chlorine (Cl), if fluorocarbon resin can be produced from chlorofluorocarbon R23, there is no mixing of chlorine. An epoch-making effect that only ethylene can be produced can be obtained.

  Accordingly, in view of these circumstances, the present invention solves the problems of the above-mentioned means for recycling and reusing the conventional Freon R22 to fluororesin, and double bonds of various chemical substances using ultrasonic waves. The purpose of this invention is to provide various reaction promotion methods such as cleavage, polymerization and substitution.

  In order to achieve the above object, the present invention promotes the reaction of the chemical substance by irradiating the chemical decomposition product gas with ultrasonic waves, that is, the chemical substance decomposition product gas is irradiated with ultrasonic waves to reduce the density. By creating waves, it causes molecular motion that repeats high-speed reversal, and increases the frequency and frequency of intense collisions between molecules. The method of promoting the reaction of chemical substances using ultrasonic waves, which promotes the reaction of chemical substances by using, is basically provided.

  In addition, by irradiating ultrasonic waves to the decomposition product gas of a chemical substance having a double bond, a reaction promotion method for the chemical substance using ultrasonic waves that cleave the double bond, a chemical substance having a double bond By irradiating the decomposition product gas with ultrasonic waves to create a dense wave, molecular motion that repeats high-speed reversal occurs, increasing the frequency and frequency of intense collisions between molecules, and the compression part by ultrasonic waves becomes adiabatic compression Therefore, the present invention provides a method for promoting the reaction of a chemical substance using ultrasonic waves that cleave double bonds by utilizing a local high-temperature and high-pressure state.

  According to the chemical substance reaction promoting method using ultrasonic waves, the reaction of various chemical substances can be promoted by ultrasonic waves. In other words, by irradiating the chemical decomposition product gas with ultrasonic waves, the kinetic energy increases and the collision frequency increases, and furthermore, energy can be supplied in a high temperature and high pressure state by adiabatic compression, so that sufficient activation energy is given. The chemical reaction is promoted. For example, there can be a place where double bond breakage, polymerization (molecular bond reaction), substitution reaction, and the like are actively performed.

  BEST MODE FOR CARRYING OUT THE INVENTION The best embodiment of the method for promoting the reaction of chemical substances using ultrasonic waves according to the present invention will be described below by taking as an example the cleavage of Freon R22 and the production of a fluororesin such as polytetrafluoroethylene from Freon R22. The present invention is not limited to chlorofluorocarbon R22 (or chlorofluorocarbon R23), and can be widely applied to the promotion of reactions such as cleavage, polymerization, and substitution of various chemical substances.

  FIG. 1 is a flowchart showing an example of a process for producing a fluororesin such as polytetrafluoroethylene from Freon R22 by applying the present invention. First, main components will be described. 1 is a preheater, The preheater 1 is provided with a Freon R22 inlet 1a and a steam inlet 1b. 2 is a first reactor, 3 is a cooler, 4 is a gas scrubber, 5 is a second reactor, 6 is a filtration device, 7 is a compressor, and 8 is a residual gas recovery container. An ultrasonic transducer 5a is disposed in the second reactor 5, and an ultrasonic oscillator 5b and a control circuit 5c for operating the ultrasonic transducer 5a are provided outside.

  The gist of the present invention is that sufficient activation is achieved by irradiating ultrasonic waves to the decomposition product gas of chemical substances, increasing kinetic energy and collision frequency, and enabling energy supply at high temperature and high pressure by adiabatic compression. Energy is applied and chemical reaction is promoted, and for example, there is a place where a double bond breakage, polymerization (molecular bond reaction), substitution reaction and the like are actively performed. First, basic experimental data relating to these will be described with reference to FIGS.

  FIG. 3 shows a temperature rise curve due to sound pressure and adiabatic compression when ultrasonic waves are applied during operation in the second reactor 5, and the vertical axis represents pressure (Pa) and temperature (° C.), and the horizontal axis. Is taking the voltage. Since the pressure is about 1000 Pa and the temperature is about 450 ° C., it can be said that the energy level that can be supplied is high.

FIG. 4 is a graph showing the relationship between the yield (%) of CF ₂ = CF ₂ gas and the temperature (° C.) of the first reactor ₂ among the cracked gas produced in the first reactor 2. FIG. 5 is a graph showing the relationship of CF ₂ = CF ₂ gas amount ratio (%) depending on the temperature (° C.) of the second reactor 5. According to FIG. 4, the yield of CF ₂ = CF ₂ gas is about 40% at maximum. On the other hand, as shown in FIG. 5, the yield of CF ₂ = CF ₂ gas increases with the reaction temperature. This is because the total gas amount is reduced when the temperature is increased. % Is composed of CF ₂ = CF ₂ gas. This is apparent, and as is apparent from the yield at 850 ° C. in FIG. 4, the actual amount of CF ₂ = CF ₂ gas is Remarkably reduced. The yield is good between 550 ° C and 650 ° C. Figure 6 shows the relationship between the temperature amount and the first reactor second unique ion molecular weight 81 to 650 ° C. to 100% by CF 2 ₌ CF ₂ gas not included in the other gas produced at the time the It is a graph. If the amount of ions is large, the amount of CF ₂ = CF ₂ gas is considered to be large, and the ratio is high between 550 ° C. and 650 ° C. as shown in FIG.

FIG. 7 is a graph showing the relationship between the temperature of CF ₂ = CF ₂ gas and the decomposition rate, and it is necessary to examine the relationship with hydrolysis in order to supply water vapor to the first reactor 2, as shown in FIG. Thus, about 500 to 650 ° C. is effective. When the temperature exceeds 650 ° C., Freon R22 is almost decomposed by hydrolysis or thermal decomposition, and the amount thereof decreases as shown in FIG. 4 even if the composition ratio of CF ₂ = CF ₂ gas is high. On the other hand, if the temperature is lower than 500 ° C., thermal decomposition becomes insufficient. FIG. 8 is a graph showing the relationship between the temperature of the first reactor 2 and the amount of gas discharged, and it can be seen that the amount of exhaust gas due to temperature does not change much. This is presumably because the gas amount after washing with hydrochloric acid becomes the same molar amount from the following formulas (1) and (2).
CHClF ₂ + H ₂ O = CO + HCl + 2HF (hydrolysis) (1)
2CHClF ₂ = CF ₂ CF ₂ + 2HCl (expected conversion reaction formula) (2)

Therefore, the conversion rate to CF ₂ = CF ₂ gas in the first reactor 2 is about 40% at a temperature of 550 ° C. to 650 ° C., but the yield is good. When the temperature is from 650 ° C. to 850 ° C., the conversion rate increases, but the amount of CF ₂ = CF ₂ gas decreases. When the temperature is 850 ° C. or higher, the conversion rate is improved, but by-products are increased. When the temperature is higher than 900 ° C., the hydrolysis becomes remarkable and the conversion rate expressed by the above formulas (1) and (2) also decreases.

  Next, based on these experimental data, based on the schematic view of the specific example of an apparatus shown in FIG. 2, it demonstrates regarding the reaction conditions at the time of the fluororesin manufacture by this invention. First, a predetermined amount of Freon R22 is introduced into the preheater 1 from the Freon R22 inlet 1a, and at the same time, the same amount of steam as the Freon R22 is introduced from the steam inlet 1b to preheat to about 300 ° C to 500 ° C. In the preheater 1, Freon R22 and water vapor are not mixed but preheated separately and flow into the first reactor 2 in the next stage. In addition, Freon R22 as a raw material is transferred to the preheater 1 after removing oil and moisture to some extent by transfer filling. The preheater 1 is intended to immediately start pyrolysis of the decomposition product in the first reactor 2 in the next stage and is not necessarily an indispensable component, but by reducing the reaction time, It is preferable to preheat in order to obtain a cracked product gas with less contamination. In addition, separate preheaters can be used for Freon R22 and water vapor, respectively.

Heaters 2a and 2a are provided on the outer periphery of the first reactor 2, and preheated Freon R22 and water vapor are mixed in the first reactor 2, and the temperature is about 500 ° C. to 750 ° C., pressure −100 mH. _The reaction is carried out under conditions of ₂ O to normal pressure. The residence time of Freon R22 and water vapor in the first reactor 2 is about 1 second. In addition, since the decomposition reaction in the first reactor 2 is thermal decomposition, water vapor is not particularly necessary. However, the presence of water vapor reduces the generation of by-products and increases the yield of the target gas. Therefore, it is preferable to add water vapor.

The first reactor 2, thermal decomposition reaction occurs, Freon R22 is generated decomposed into hydrogen chloride and CF 2 ₌ CF ₂ gas by thermal decomposition, decomposition product gas of CF 2 ₌ CF ₂ gas with hydrogen chloride to obtain . The reaction formula is as follows.
2CHClF ₂ → CF ₂ = CF ₂ + 2HCl

The present invention can be directly applied to the cleavage of Freon R23 and polymerization to a fluororesin instead of Freon R22. When using Freon R23 as a raw material, Freon R23 is decomposed and generated into CF ₂ = CF ₂ gas and hydrogen fluoride by thermal decomposition in the first reactor 2, and from CF ₂ = CF ₂ gas and hydrogen fluoride. A cracked product gas is obtained. The reaction formula is as follows.
2CHF ₃ → CF ₂ = CF ₂ + 2HF
Therefore, this embodiment corresponds to the case where Freon R23 is used as a raw material by replacing Freon R22 with Freon R23 and hydrogen chloride with hydrogen fluoride.

Next, the decomposition product gas (CF ₂ = CF ₂ gas + hydrogen chloride) and water vapor generated by thermal decomposition enter the cooler 3 and are decomposed by the cooling water flowing in from the cooling water inlet 3a and flowing out to the cooling water outlet 3b. By cooling the product gas and water vapor, the temperature of the decomposition product gas is lowered and the water vapor is liquefied. The temperature in the cooler 3 should just be the temperature which can liquefy water vapor | steam, and about normal temperature is suitable. This cooling is for liquefying and removing water vapor, but at that time, many acids are also dissolved in water, and at the same time, the acid is also removed. By rapidly liquefying in this way, the generation of by-products is prevented, and the purity of CF ₂ = CF ₂ gas in the decomposition product gas is increased, so that the cracking and polymerization reaction in the second reactor 5 occurs. Can be performed efficiently.

The cracked product gas from which the water vapor has been removed is neutralized and washed with the acid contained in the cracked product gas by the gas scrubbers 4 and 4, and is introduced into the second reactor 5 after CF ₂ = CF ₂ gas. The temperature in the second reactor 5 is usually room temperature, but may be appropriately heated to increase the reactivity, and is equipped with a heater for that purpose. This second reactor 5 has a pressure of −100 mH ₂ O to normal pressure, an ultrasonic oscillator 5b controlled by the control circuit 5c has an ultrasonic frequency of 200 KHz and a drive voltage of 1 kV. The reaction is performed by irradiating sound waves. The residence time of the reactant in the second reactor 5 is about 0.5 to 3 seconds.

In the second reactor 5, the double bond of CF ₂ = CF ₂ gas is cleaved by ultrasonic irradiation, and polymerization reactions to various fluororesins represented by polytetrafluoroethylene are started and promoted. The mechanism by which CF ₂ = CF ₂ gas is cleaved and polymerized by ultrasonic irradiation in the second reactor 5 is as follows. That is, a local high-temperature and high-pressure state is obtained by a physical impact caused by repetition of high-pressure and vacuum of dense waves in ultrasonic irradiation and an adiabatic compression action of ultrasonic waves, and this energy causes a double CF ₂ = CF ₂ gas. The bond is broken. Since the molecules after cleavage are rich in reactivity, they are bonded and polymerized one after another by collision of similar molecules, and once polymerization is initiated, polymerization is accelerated by exothermic reaction, but the negative pressure part In this case, explosive polymerization does not occur because the temperature decreases, and when the ultrasonic irradiation is stopped, the double bond breakage stops and the polymerization also stops. That is, the start and stop of the polymerization reaction can be arbitrarily controlled by the presence or absence of ultrasonic irradiation. Similarly, for other chemical substances, chemical reactions such as cleavage, polymerization, and substitution can be promoted.

  9 is a product outlet from the second reactor 5. The residual gas is taken into the residual gas recovery container 8 from the filter 6 such as a filter through the compressor 7. The filtration device 6 has a function of supplementing this by using an appropriate filter because the fluororesin particles that have become solid by polymerization are small and scatter with the gas. The compressor 7 is used again as a raw material for the fluororesin by recovering the fluorocarbon R22, which has not been decomposed, into a cylinder without releasing it to the atmosphere.

A purification step is not required in the middle of the above process, and fluorocarbon resin such as polytetrafluoroethylene is obtained from Freon R22 by ultrasonic vibration emitted from the ultrasonic vibrator 5a driven by the ultrasonic oscillator 5b in the second reactor 5. Polymerization was possible. In addition, the used raw material Freon R22 could be polymerized without any problems even if it was transferred and filled and the oil and water were roughly removed. However, since it was not converted into CF ₂ = CF ₂ gas when there was air, it was taken out and supplied as a liquid. Further, it has been found from experiments that the polymerization is started simultaneously with the oscillation of the ultrasonic vibration, and that the polymerization is stopped when the ultrasonic vibration is stopped.

  It is also possible to supply a chemical substance that promotes reactions such as cleavage and polymerization directly to the reactor (second reactor 5).

Using the above reaction accelerator under the following conditions, CF ₂ ═CF ₂ gas is continuously decomposed and generated from Freon R22, the double bond of the CF ₂ ═CF ₂ gas is cleaved, and polymerization reaction is performed. Polytetrafluoroethylene was produced.
Conditions in the first reactor 2 Reactor temperature 650 ° C
2. Input amount of Freon R22 2kg / h
3. Amount of steam input Same amount as Freon R22 (weight)
4). Residence time About 1 second 5. Fluorocarbon R22, preheat temperature of steam about 500 ℃
6). Reactor pressure −100 mH ₂ O to atmospheric pressure in the second reactor 5 Reactor temperature Normal temperature 2. Reactor pressure −100 mH ₂ O to normal pressure Ultrasonic frequency 200KHz
4). Drive voltage 1kV (pp)
5. Residence time Approx. 3 seconds 6. CF ₂ = CF ₂ gas concentration 60%

As shown in the above data, Freon R22 and water vapor were respectively charged at 2 kg / h into the preheater 1 and preheated to 500 ° C., and then CFC R22 preheated in the first reactor 2 and water vapor were mixed at 650 ° C. The reaction is carried out for about 1 second under conditions of a pressure of −100 mH ₂ O to normal pressure, and after cooling with the cooler 3, the water vapor is condensed and removed and then the acid is neutralized and washed with the gas washers 4 and 4. Then, it was allowed to flow into the second reactor 5 and reacted at room temperature at a pressure of −100 mH ₂ O, an ultrasonic frequency of 200 KHz, and a drive voltage of 1 kV for 3 seconds. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG.

  Ultrasonic irradiation was performed 60 times at intervals of 0.1 seconds, and the others were reacted under the same conditions as in Example 1. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG.

Ultrasonic irradiation was performed 120 times at intervals of 0.1 seconds, and the others were reacted under the same conditions as in Example 1. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG. FIG. 12 is a diagram showing chemical formulas of the compositions of the peaks A to L in the chromatographs shown in FIGS. 9 to 11. FIG. 11 is a chromatograph by GC-MS. In this graph only, the column uses HP = PLOT / Q in order to increase the separation efficiency of CF ₂ = CF ₂ gas. When the number of times of irradiation with ultrasonic waves increases, CF ₂ = CF ₂ gas double bonds are broken and chained, and CF ₂ = CF ₂ gas is not detected and other gas peaks are conspicuous . In FIG. 11, there is no gas having a double bond. Therefore, when the CF ₂ = CF ₂ gas converted in the first reactor is cooled to room temperature and washed, and then irradiated with ultrasonic waves, only the flon R22 remains as shown in the peak G of FIG.

  The temperature of the first reactor 2 was set to 550 ° C., and the others were reacted under the same conditions as in Example 1. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG.

  The temperature of the first reactor 2 was set to 650 ° C., and the others were reacted under the same conditions as in Example 1. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG.

  The temperature of the first reactor 2 was 750 ° C., and the others were reacted under the same conditions as in Example 1. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG. FIG. 16 is a diagram showing chemical formulas of the compositions of the respective peaks A to E in the chromatographs shown in FIGS. 13 to 15. As the temperature increases, the conversion rate also increases, and almost no Freon R22 remains as shown in FIG.

  The reaction was performed under the same conditions as in Example 4 except that the ultrasonic wave was continuously irradiated. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG.

  The reaction was performed under the same conditions as in Example 5 except that the ultrasonic wave was continuously irradiated. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG.

  The reaction was performed under the same conditions as in Example 6 except that the ultrasonic wave was continuously irradiated. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG. In Example 7 to Example 9, by continuously irradiating ultrasonic waves, a place where the ultrasonic waves are in a steady state is generated in the second reactor 5 and the amplitude of the ultrasonic waves is increased. In some cases, the sound pressure level or temperature rises higher than the calculation, and polymerization is easily started.

  The amount of water vapor in the first reactor 2 was changed to 4 kg / h, and the others were reacted under the same conditions as in Example 1. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG.

  The amount of water vapor in the first reactor 2 was changed to 2 kg / h, and the others were reacted under the same conditions as in Example 1. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG.

The amount of water vapor in the first reactor 2 was changed to 1 kg / h, and the others were reacted under the same conditions as in Example 1. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG. FIG. 23 is a diagram showing a chemical formula of the composition of each peak A to F of the chromatographs shown in FIGS. 20 to 22. By mixing water vapor with Freon R22, the types of by-products are reduced and the conversion efficiency is increased. However, if the amount of water vapor is too large, undesired gas may be generated and the yield of CF ₂ = CF ₂ gas may be reduced. Therefore, it is preferable to introduce water vapor having the same weight as that of Freon R22.

  Next, the amount of water vapor was set to 0, and the others were reacted under the same conditions as in Example 4. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG.

  Next, the amount of water vapor was set to 0, and the others were reacted under the same conditions as in Example 5. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG.

Next, the amount of water vapor was set to 0, and the others were reacted under the same conditions as in Example 6. As a result, a chromatograph of the exhaust gas discharged from the second reactor 5 is shown in FIG. FIG. 27 is a diagram illustrating chemical formulas of the compositions of the peaks A to L of the chromatographs illustrated in FIGS. 24 to 26. 24 shows a case where the temperature is 550 ° C., FIG. 25 shows a case where the temperature is 650 ° C., and FIG. 26 shows a case where the temperature is 750 ° C. When the temperature is low, various gases are generated and double bonds are formed. Gas other than the gas it has is also generated. On the other hand, as the temperature increases, the type of gas produced decreases and the ratio of CF ₂ = CF ₂ gas increases, but the overall thermal decomposition increases and the amount of gas decreases, so CF ₂ = CF ₂ gas Yield deteriorates.

On the other hand, when the temperature is raised, hydrolysis and thermal decomposition increase, and the amount of CF ₂ = CF ₂ gas decreases especially when water vapor is not added. This is thought to be because a large amount of carbon is emitted and a large amount of gas having a large molecular weight is generated. When the temperature is increased by setting the steam to 2 kg / h, the composition ratio of CF ₂ = CF ₂ gas and undecomposed chlorofluorocarbon is higher in CF ₂ = CF ₂ gas and the amount of CO ₂ gas is increased, so that hydrolysis is increased. The amount of CFCs R22 to be increased increases and the total gas amount decreases. Therefore, the amount of gas can be increased by adding water vapor, but conversion conditions are required so that thermal decomposition and hydrolysis do not increase.

  As described above in detail, according to the present invention, even if the recovered chlorofluorocarbon R22 (or chlorofluorocarbon R23) contains a large amount of impurities, it is a continuous process from raw material input to residual gas recovery without performing an advanced purification process. Since it is possible to prevent generation of harmful gas as a by-product, it is possible to easily detoxify chlorofluorocarbon gas that has been conventionally used as a refrigerant, and chlorofluorocarbon R22 (or chlorofluorocarbon R23). ) Can be used as a raw material for fluororesins represented by polytetrafluoroethylene resin after simple purification after recovery. Moreover, the index of global warming is 10,000 times or more of carbon dioxide gas (Freon R22 is about 1000 times), and it can be effectively used as a raw material for fluororesin while decomposing Freon R23, which has a high impact on global warming.

The flowchart which shows the process example at the time of manufacturing a fluororesin by applying this invention. 1 is a schematic diagram showing an example of a reaction promoting device according to the present invention. The graph which shows the temperature rise curve by the sound pressure by an ultrasonic wave in a 2nd reactor, and adiabatic compression. Graph continuous polymerization by _CF 2 = CF ₂ gas yield and (%) shows the relationship between the temperature (° C.). Graph showing the relationship between the CF 2 ₌ CF ₂ gas amount ratio of According to a second reactor temperature (℃) (%). Graph showing the relationship between the amount and the temperature of the first reactor of unique ion molecular weight 81 to 650 ° C. to CF 2 ₌ CF ₂ gas not included in the other gases produced in is 100%. Graph showing the relationship between the CF ₂ = CF ₂ gas temperature and decomposition rate. The graph which shows the relationship between the temperature of a 1st reactor, and gas amount. 2 is an exhaust gas chromatograph of Example 1. FIG. 2 is a chromatograph of exhaust gas of Example 2. FIG. 4 is a chromatograph of exhaust gas of Example 3. FIG. The figure of the chemical formula of the composition of each peak A-L of FIGS. 6 is an exhaust gas chromatograph of Example 4. 6 is a chromatograph of exhaust gas of Example 5. FIG. 7 is an exhaust gas chromatograph of Example 6. FIG. The figure of the chemical formula of the composition of each peak AE of FIGS. 10 is a chromatograph of exhaust gas of Example 7. 10 is an exhaust gas chromatograph of Example 8. 10 is an exhaust gas chromatograph of Example 9. 10 is a chromatograph of exhaust gas of Example 10. FIG. 14 is an exhaust gas chromatograph of Example 11. FIG. 14 is an exhaust gas chromatograph of Example 12. The figure of the chemical formula of the composition of each peak AF of FIGS. 14 is an exhaust gas chromatograph of Example 13. FIG. 14 is an exhaust gas chromatograph of Example 14. FIG. FIG. 19 is an exhaust gas chromatograph of Example 15. FIG. The figure of the chemical formula of the composition of each peak A-L of FIGS.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 ... Preheater 1a ... Freon R22 inlet 1b ... Steam inlet 2 ... First reactor 3 ... Cooler 4 ... Gas scrubber 5 ... Second reactor 5a ... Ultrasonic vibrator 5b ... Ultrasonic oscillator 5c ... Control Circuit 6 ... Filtration device 7 ... Compressor 8 ... Residual gas recovery container 9 ... Product outlet

Claims (4)

  A method of promoting reaction of a chemical substance using ultrasonic waves, characterized by accelerating the reaction of the chemical substance by irradiating the decomposition product gas of the chemical substance with ultrasonic waves.   By irradiating ultrasonic waves to the decomposition gas of chemical substances to create a dense wave, molecular motion that repeats high-speed reversal occurs, increasing the frequency and frequency of intense collisions between molecules, and the compressed part by ultrasonic waves is insulated. A method of promoting reaction of a chemical substance using ultrasonic waves, characterized in that the reaction of the chemical substance is promoted by utilizing a local high temperature and high pressure state due to compression.   A method for promoting a reaction of a chemical substance using ultrasonic waves, wherein the double bond is cleaved by irradiating ultrasonic waves to a decomposition product gas of the chemical substance having a double bond.   By irradiating ultrasonic waves to the decomposition product gas of a chemical substance having a double bond to create a dense wave, it causes molecular motion that repeats high-speed reversal, increases the frequency and frequency of intense collisions between molecules, A method for promoting the reaction of a chemical substance using ultrasonic waves, wherein the double bond is cleaved by utilizing a local high temperature and high pressure state because the compression part by adiabatic becomes adiabatic compression.

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