WO2009139352A1 - 1,2,3,4-テトラクロロヘキサフルオロブタンの製造方法および精製方法 - Google Patents
1,2,3,4-テトラクロロヘキサフルオロブタンの製造方法および精製方法 Download PDFInfo
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- WO2009139352A1 WO2009139352A1 PCT/JP2009/058772 JP2009058772W WO2009139352A1 WO 2009139352 A1 WO2009139352 A1 WO 2009139352A1 JP 2009058772 W JP2009058772 W JP 2009058772W WO 2009139352 A1 WO2009139352 A1 WO 2009139352A1
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- tetrachlorohexafluorobutane
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- fluorine gas
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
- C07C17/10—Preparation of halogenated hydrocarbons by replacement by halogens of hydrogen atoms
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
- C07C17/383—Separation; Purification; Stabilisation; Use of additives by distillation
Definitions
- the present invention relates to a method for producing and purifying 1,2,3,4-tetrachlorohexafluorobutane. More specifically, the present invention relates to a process for producing 1,2,3,4-tetrachlorohexafluorobutane useful as a raw material for synthesis of hexafluoro-1,3-butadiene, which is attracting attention as an etching gas for semiconductors, and the like. The present invention relates to a method for purifying 1,2,3,4-tetrachlorohexafluorobutane.
- 1,2,3,4-Tetrachlorohexafluorobutane is an important compound as a raw material for synthesis of hexafluoro-1,3-butadiene, which is attracting attention as an etching gas used for fine processing of semiconductors.
- Conventionally, as a method for producing 1,2,3,4-tetrachlorohexafluorobutane methods described in the following patent documents are known.
- Patent Document 1 JP 2006-342059 A discloses a compound represented by CClX 1 X 2 —CClX 3 —CClX 4 —CClX 5 X 6 (X is a hydrogen atom or a fluorine atom) in a liquid phase. Describes a process for preparing 1,2,3,4-tetrachlorohexafluorobutane by reacting with. In this method, Patent Document 1 discloses that perfluoroalkanes, perfluoroethers, perfluoropolyethers, chlorinated hydrocarbons, and perfluoroalkylamines are used as a solvent.
- Patent Document 1 describes that when 1,2,3,4-tetrachlorohexafluorobutane is used as a solvent for the fluorination reaction, it is particularly preferable because separation of the solvent and the product is unnecessary. Yes.
- the reaction raw material is diluted with a solvent to carry out the fluorination reaction at a low concentration, and there remains a problem in that the target product is produced economically and efficiently industrially.
- Patent Document 1 the process for producing 1,2,3,4-tetrachlorohexafluorobutane described in Patent Document 1 also has a problem in that the target product is produced industrially inexpensively and efficiently. Has been.
- 1,2,3,4-tetrachlorobutane has isomers such as optical isomers.
- the reaction temperature is often set based on isomers having a high melting point among these isomers. Therefore, when carrying out a liquid phase reaction, it may be necessary to ensure the reaction temperature at a certain high temperature in order to carry out the reaction while maintaining the liquid state. In such a case, the production side reaction such as low boiling point proceeds due to CC cleavage in the fluorination reaction, and the yield of the target product is lowered, or the fluorination reaction proceeds excessively. happenss.
- An object of the present invention is to provide a method for efficiently producing 1,2,3,4-tetrachlorohexafluorobutane industrially at low cost by efficiently using expensive fluorine gas.
- the object is to provide a process by which 4-tetrachlorohexafluorobutane can be produced.
- Another object of the present invention is to provide a method for efficiently purifying the produced 1,2,3,4-tetrachlorohexafluorobutane.
- the present invention relates to the following [1] to [10].
- a part, or all of unreacted fluorine gas discharged from the downstream reactor is further introduced into the upstream reactor.
- a process for producing 4-tetrachlorohexafluorobutane is further introduced into the upstream reactor.
- a reaction product liquid containing 1,2,3,4-tetrachlorohexafluorobutane obtained by the reaction of 1,2,3,4-tetrachlorobutane and fluorine gas is introduced into a distillation column, The reaction product liquid is separated into a liquid containing 1,2,3,4-tetrachlorohexafluorobutane and a liquid containing the solvent, and the liquid containing the separated solvent is converted into 1,2,3,4-tetrachloro
- reaction product liquid containing 1,2,3,4-tetrachlorohexafluorobutane obtained by the method described in [1] above is introduced into a distillation column, and the reaction product liquid is converted into 1,2,
- the liquid containing 3,4-tetrachlorohexafluorobutane is separated into the liquid containing the solvent and the liquid containing the solvent, and at least a part of the separated liquid containing 1,2,3,4-tetrachlorohexafluorobutane is treated with an alkaline substance and / or
- a method for purifying 1,2,3,4-tetrachlorohexafluorobutane comprising contacting with water.
- fluorine gas can be used without waste by introducing a part or all of unreacted fluorine gas discharged from one reactor into a reactor other than the one reactor. 1,2,3,4-tetrachlorohexafluorobutane can be produced efficiently and economically.
- the reaction of 1,2,3,4-tetrachlorobutane and fluorine gas can be carried out in a low temperature region, the generation of low boiling components due to C—C cleavage can be suppressed, and the excess fluorination reaction Progress and the like can be suppressed. Therefore, according to the present invention, expensive fluorine gas can be used without waste, and 1,2,3,4-tetrachlorohexafluorobutane can be produced efficiently and economically.
- 1,2,3,4-tetrachlorohexafluorobutane is used as a starting material, and fluorine gas is supplied without catalyst in the presence of a solvent to produce 1,2,3,4-tetrachlorobutane. And fluorine gas are reacted to produce 1,2,3,4-tetrachlorohexafluorobutane.
- 1,2,3,4-Tetrachlorobutane used as a starting material in the present invention is produced as a by-product in the manufacturing stage of industrially produced chloroprene rubber, for example, as shown in the following chemical formula To do.
- the following formula (1) is a formula showing a main reaction when producing chloroprene rubber.
- Formula (2) is a formula showing an example of a side reaction that proceeds simultaneously when the reaction shown by Formula (1) proceeds.
- 1,2,3,4-tetrachlorobutane produced by the side reaction represented by the above formula (2) is made harmless by incineration with other by-products (chlorinated products). And discarded.
- 1,2,3,4-tetrachlorobutane produced and discarded as a by-product in the production process of chloroprene rubber can be separated and recovered and used as a starting material.
- 1,2,3,4-tetrachloro Butane can also be obtained (see the following formula (3)).
- the 1,2,3,4-tetrachlorobutane When 1,2,3,4-tetrachlorobutane obtained as described above is used as a starting material, the 1,2,3,4-tetrachlorobutane usually has a purity of 95 mol%. More preferably, it is 98 mol% or more.
- 1,2,3,4-tetrachlorobutane having a high purity as a starting material as described above there are few by-products and the separation is facilitated, and the resulting 1,2,3,4-tetrachlorobutane is obtained. Since the purity of hexafluorobutane is high and excessive equipment is not required in the purification process, it is advantageous in production.
- 1,2,3,4-tetrachlorobutane has meso form and dl form which is an optical isomer as isomers.
- the melting point (mp) of the dl form which is an optical isomer, is 0 ° C. or lower (boiling point (bp) is about 213 ° C.), and the dl form is liquid at room temperature.
- the melting point of the meso form is about 73 ° C. (boiling point is about 213 ° C.), and the meso form is a white solid at room temperature.
- the content of the dl form having a low melting point contained in 100% by mass of 1,2,3,4-tetrachlorobutane as a starting material is usually within the range of 40% by mass or more.
- the meso form content inevitably falls within the range of 60% by mass or less.
- the solvent (reaction solvent) used in the present invention is preferably a compound that does not easily react with fluorine gas and can maintain a liquid state under reaction conditions.
- examples of such compounds include chlorocarbons and chlorofluorocarbons.
- a compound in which all of the hydrogen atoms bonded to the carbon atom are substituted with a halogen atom such as a chlorine atom or a fluorine atom is unlikely to undergo a substitution reaction even when contacting with a fluorine gas.
- the target compound 1,2,3,4-tetrachlorohexafluorobutane can be efficiently produced.
- 1,2,3,4-tetrachlorohexafluorobutane itself produced by the production method of the present invention can also be used as a solvent. This is because the above-described condition that the reaction with the fluorine gas is difficult and the liquid state can be maintained under the reaction conditions is satisfied.
- the amount of hydrogen fluoride contained in the reaction solvent is usually 5% by mass or more with respect to 100% by mass of the reaction solvent.
- the amount of hydrogen fluoride in the reaction solvent is preferably in the range of 5 to 50% by mass.
- the reaction rate of the fluorination reaction may be slow.
- the amount of hydrogen fluoride is 50% by mass or more, the reaction tends to proceed, and low boiling components tend to increase due to C—C cleavage or the like.
- a fluorine gas is supplied to 1,2,3,4-tetrachlorobutane in the presence of a solvent in a non-catalyst using a plurality of reactors to obtain 1,2,3,4-tetrachlorobutane and
- 1, 2, 3, 4-tetrachlorohexafluorobutane is produced.
- the configuration and arrangement of the reactor for performing such a reaction are not particularly limited, but in the present invention, the plurality of reactors are arranged in series, and the solvent and 1,2,3,4-tetra are placed in the reactor. Fill with chlorobutane, supply fluorine gas to react 1,2,3,4-tetrachlorobutane with fluorine gas, and part or all of the unreacted fluorine gas discharged from the upstream reactor Is preferably introduced into the downstream reactor. By circulating fluorine gas in this way, expensive fluorine gas can be used efficiently without waste.
- 1,2,3,4-tetrachlorobutane and fluorine gas are brought into contact with each other using a plurality of reactors, and a part or all of unreacted fluorine gas discharged from one reactor is (2)
- 1,2,3,4-tetrachlorobutane and fluorine gas are brought into contact with each other, and from the upstream reactor
- the method (2) in which part or all of the unreacted fluorine gas discharged is introduced into the downstream reactor, is particularly preferred.
- a heating / cooling device As the reactor, a heating / cooling device, a stirring device, a gas blowing line having an introduction port for introducing gas into the liquid phase, and a gas discharge line for discharging a gas such as fluorine gas from the gas phase are generally arranged.
- a pressure vessel such as an autoclave can be used.
- the reaction solvent may contain highly corrosive hydrogen fluoride.
- the reaction liquid such as a stirrer and a gas blowing line, are formed of a corrosion resistant material against fluorine or hydrogen fluoride.
- a corrosion resistant material against fluorine or hydrogen fluoride.
- examples of such a material having corrosion resistance include Inconel (registered trademark) and Hastelloy (registered trademark), among them, for example, Hastelloy HC, SUS and their Teflon (registered trademark) lining.
- nickel that may be contained in the corrosion-resistant material may become a fluoride, and since this fluoride promotes the substitution reaction between Cl and F, the corrosion-resistant material has a nickel content. It is preferable to use a low material.
- the number of the plurality of reactors arranged in series is not particularly limited. However, if two reactors are arranged in series, in many cases, expensive fluorine gas can be efficiently and efficiently used. Can be used. However, if the fluorine in the fluorine gas is not fully utilized even in the downstream reactor, a part or all of the unreacted fluorine gas discharged from the downstream reactor is further removed from the upstream reactor. It is preferable to introduce into the reactor, to increase the number of reactors to 3 or more, and to introduce a part or all of the unreacted fluorine gas into the downstream reactor.
- the upstream reactor is referred to as a first reactor
- the downstream reactor is referred to as a second reactor.
- 1,2,3,4-tetrachlorobutane as a starting material is introduced into each reactor, and the above solvent (reaction solvent) is further introduced into the reactor.
- the 1,2,3,4-tetrachlorobutane concentration of the starting material in the reactor is usually in the range of 10 to 50% by mass, Introduce chlorobutane.
- the air in the reactor is reduced to nitrogen gas, helium gas, neon gas, argon gas, etc. in order to suppress the generation of oxygen-containing impurities. Replacement with an inert gas is preferred.
- fluorine gas is introduced from a gas blowing line having an inlet in the liquid phase to fluorinate 1,2,3,4-tetrachlorobutane.
- fluorine gas is introduced from a gas blowing line having an inlet in the liquid phase to fluorinate 1,2,3,4-tetrachlorobutane.
- Part or all of the unreacted fluorine gas after the reaction in the first reactor is changed from the gas discharge line installed in the gas phase part to the gas blowing line having an inlet in the liquid phase of the second reactor. be introduced.
- a new fluorine gas can be introduced into the second reactor.
- the fluorine gas introduced into the first reactor from the gas blowing line of the first reactor may be a fluorine gas alone, but is usually introduced as a diluted mixed gas diluted with the inert gas.
- a diluted mixed gas the concentration of the fluorine gas in the diluted mixed gas is usually 30% by volume or more, and it is preferable to use a diluted mixed gas in the range of 40 to 70% by volume. .
- the concentration of fluorine gas in the diluted mixed gas is 30 to 70% by volume. It is preferable to set within the range.
- the diluted mixed gas is preferably introduced into the liquid phase from a gas blowing line.
- the supply rate of the diluted mixed gas introduced into the first reactor depends on the concentration of the fluorine gas. For example, when the concentration of the fluorine gas is 40 to 50% by volume, the supply rate per minute is usually the first.
- the speed is 1/30 to 1/2, preferably 1/15 to 1/4 of the volume of the reactor.
- the fluorine gas introduced into the liquid phase of the first reactor as described above and set in the concentration range of 30 to 70% by volume is fluorinated with 1,2,3,4-tetrachlorobutane.
- a part or all of the exhaust gas after the reaction, which is consumed by the gas phase and exhausted from the gas phase part of the first reactor, is introduced into the second reactor.
- the exhaust gas contains fluorine gas that has not reacted in the first reactor, which is consumed in the second reactor.
- dilution gas is mainly discharged
- the concentration of fluorine gas contained in the exhaust gas of the second reactor is preferably 10% by volume or less, more preferably 2% by volume or less.
- the expensive fluorine gas can be used efficiently without loss. That is, the second reactor is intended to recover and effectively use the fluorine gas lost from the first reactor.
- the exhaust gas containing fluorine gas discharged from the first reactor is introduced into the liquid phase part of the second reactor as it is, and 1,2,3,4-tetra in the second reactor is introduced.
- 1,2,3,4-tetra in the second reactor Used in the fluorination reaction of chlorobutane.
- the reaction rate may be slow. Therefore, in some cases, it is possible to carry out a reaction by additionally introducing fluorine gas.
- the capacity of the second reactor is preferably less than or equal to the capacity of the first reactor, more preferably 2/3 or less of the capacity of the first reactor, and in order to increase the absorption efficiency of fluorine gas, A vertically elongated structure is preferable.
- the present invention uses a plurality of reactors in the presence of a solvent and supplies a fluorine gas to 1,2,3,4-tetrachlorobutane in a non-catalytic manner to produce 1,2,3,4-tetrachlorobutane. 1, 2 and 3, by introducing a part or all of the unreacted fluorine gas discharged from one reactor into a reactor different from the one reactor.
- This is a method for producing 4-tetrachlorohexafluorobutane.
- the plurality of reactors are arranged in series, and by introducing some or all of the unreacted fluorine gas discharged from the upstream reactor into the downstream reactor, the expensive fluorine gas can be efficiently used. Can be used. That is, the present invention is an economical method for producing 1,2,3,4-tetrachlorohexafluorobutane that makes effective use of expensive fluorine gas.
- the reaction temperature of the fluorination reaction is usually set in the range of ⁇ 20 to 70 ° C., preferably in the range of 0 to 50 ° C. By setting the reaction temperature as described above, CC cleavage, excessive fluorination and the like of 1,2,3,4-tetrachlorobutane are less likely to occur.
- the reaction pressure of the fluorination reaction is usually set within the range of 0.1 to 2.0 MPa.
- 1,2,3,4-tetrachlorohexafluorobutane By reacting as described above, 1,2,3,4-tetrachlorobutane is fluorinated, and at least a part thereof becomes 1,2,3,4-tetrachlorohexafluorobutane. Since most of the 1,2,3,4-tetrachlorohexafluorobutane exists in the reaction solvent, the reaction product after the reaction as described above contains a reaction solvent, hydrogen fluoride. 1,2,3,4-tetrachlorobutane as a raw material, 1,2,3,4-tetrachlorohexafluorobutane produced by this reaction, and by-products are contained.
- the target product of the production method of the present invention is 1,2,3,4-tetrachlorohexafluorobutane
- Tetrachlorohexafluorobutane needs to be separated.
- 1,2,3,4-tetrachlorohexafluorobutane For the separation and purification of 1,2,3,4-tetrachlorohexafluorobutane, a purification method by distillation using a distillation column is advantageous.
- 1,2,3,4-tetrachlorohexafluorobutane of the present invention preferably, 1,2,3,4-tetrachlorohexafluorobutane is purified by distillation using two or more distillation columns. Do. At this time, at least one of the distillation columns usually needs to have 15 or more theoretical plates, more preferably 25 or more. If it is less than 15 stages, the separation of impurities, particularly tetrachloropentafluorobutane (C 4 HCl 4 F 5 ), etc.
- a reaction product solution containing 1,2,3,4-tetrachlorohexafluorobutane is introduced into the first distillation column using an infusion pump or the like, and a low-boiling product and a high-boiling product are introduced.
- a product a solution containing a solvent used in the reaction and a solution containing 1,2,3,4-tetrachlorohexafluorobutane.
- the target 1,2,3,4-tetrachlorohexafluorobutane can also be obtained from the top of the first distillation column as a low boiling point product, but usually the bottom of the first distillation column as a high boiling point product. If necessary, it can be introduced into the second distillation column and obtained from the top of the second distillation column. Moreover, it is possible to carry out purification by operating in the same manner with the third and fourth distillation columns as required.
- the 1,2,3,4-tetrachlorohexafluorobutane thus obtained may contain hydrogen fluoride, a small amount of fluorine gas, etc., so this 1,2,3,4-tetrachloro Hexafluorobutane is brought into contact with an alkaline substance and / or water to remove hydrogen fluoride and the like.
- this step can be carried out before the introduction into the first distillation column, or in some cases between the first distillation column and the second distillation column.
- alkaline substance used in the present invention examples include alkali metal compounds such as sodium hydroxide, potassium hydroxide and lithium hydroxide, and alkaline earth metal compounds such as calcium hydroxide. These alkaline substances are usually used by dissolving or dispersing in water.
- 1,2,3,4-tetrachlorohexafluorobutane contacted with water as described above contains a trace amount of water, it can be contacted with a porous purification agent. It is preferable to remove water contained in 4-tetrachlorohexafluorobutane.
- porous refining agent used here examples include carbonaceous solid materials, alumina, zeolite, and the like, and molecular sieves 3A, 4A, 5A, etc. are particularly preferably used in the present invention.
- the temperature in the contact step with such a porous purification agent is preferably in the range of 0 to 60 ° C.
- the purity of 1,2,3,4-tetrachlorohexafluorobutane thus purified is usually 98% by mass or more, preferably 99% by mass or more.
- the yield of 1,2,3,4-tetrachlorohexafluorobutane as viewed from the starting material is usually 70 mol% or more, and is very efficient and highly pure 1,2,3,4-tetrachlorohexa Fluorobutane can be obtained.
- the low boiling point product (liquid containing the solvent used in the reaction) obtained by separating 1,2,3,4-tetrachlorohexafluorobutane in the distillation column as described above is 1,2,3,4-tetra It can be used as a reaction solvent when chlorobutane is fluorinated, and can be recycled after returning to the reactor in which the fluorination reaction is performed. When at least a part of the reaction solvent is recycled, the low boiling point product can be purified and reused if necessary.
- reaction solvent is not fluorinated by the fluorination reaction as described above, that is, does not consume fluorine, it is industrially advantageous to use at least a part of the reaction solvent in a circulating manner.
- This 3,4-dichlorobutene-1 was chlorinated with chlorine gas in the absence of a solvent, and the resulting mixture was separated and purified by distillation to obtain 1,2,3,4-tetrachlorobutane.
- the purity was 99.1 mol% and the ratio of dl form / meso form was about 49/51.
- Example 1 A SUS304 (Teflon (registered trademark) lining) reactor having an internal volume of 1000 ml was used as the first reactor.
- nitrogen gas was purged, and the temperature was maintained at 35 ° C. with stirring.
- an outlet gas (discharge line) line provided in the gas phase portion of the first reactor was connected to the inlet of the second reactor.
- an SUS304 (Teflon (registered trademark) lining) reactor having an internal volume of 1000 ml was used.
- nitrogen gas was purged, and the temperature was maintained at 30 ° C. while stirring.
- the outlet gas (gas discharge line) of this first reactor was continuously introduced into the liquid phase part of the second reactor.
- the reaction temperature was kept at 30 ° C. and the gas introduced from the outlet of the first reactor was reacted while stirring. As a result, no fluorine gas was present in the outlet (gas discharge line) gas of the second reactor. Not detected.
- the fluorine gas concentration in the first reactor outlet (gas discharge line) gas was 30% by volume (the remainder was mainly nitrogen gas).
- the outlet gas of the second reactor was analyzed, no fluorine gas was detected in the outlet gas of the second reactor.
- the reaction was restarted while supplying the supply gas (50% by volume fluorine gas) as described above.
- the fluorine gas concentration in the outlet gas of the first reactor was about 50% by volume, and the reaction in the first reactor was completed.
- the fluorine gas concentration in the outlet gas of the second reactor was 0.1% by volume or less.
- the supply gas (50 vol% fluorine gas) was stopped and the product of the first reactor was analyzed.
- the target 1,2,3,4-tetrachlorohexafluorobutane The yield was 78 mol%.
- Example 2 A solution containing crude 1,2,3,4-tetrachlorohexafluorobutane obtained by repeating the reaction under the conditions of [Example 1] was charged into a distillation column (15 theoretical plates) and distilled. The resulting high boiling point product was brought into contact with an aqueous potassium hydroxide solution and dehydrated at 18 ° C. using zeolite (Molecular Sieves 4A). The high-boiling product that had undergone the treatment was charged into a distillation column (theoretical plate number: 25) and subjected to separation and purification to obtain 1,2,3,4-tetrachlorohexafluorobutane and mainly tetrachloromethane, which were the target products. When this was analyzed by gas chromatography, the purity of 1,2,3,4-tetrachlorohexafluorobutane was about 99.8% by mass.
- Example 3 A SUS reactor having an internal volume of 1000 ml was used as the first reactor.
- 20 g of hydrogen fluoride was dissolved in 380 g of 1,2,3,4-tetrachlorohexafluorobutane obtained in [Example 2] as a solvent, and 1 obtained in ⁇ Raw material example>.
- 2,3,4-Tetrachlorobutane was charged in an amount of 100 g, nitrogen gas was introduced at a pressure of 1.0 MPa, and a leak test was performed. Then, the nitrogen gas was purged and the temperature was maintained at 40 ° C. with stirring.
- an outlet gas (discharge line) line provided in the gas phase portion of the first reactor was connected to the inlet of the second reactor.
- a reactor made of SUS304 having an internal volume of 1000 ml was used as the second reactor.
- 20 g of hydrogen fluoride dissolved in 300 g of 1,2,3,4-tetrachlorohexafluorobutane obtained in [Example 2] as a solvent and 1 obtained in ⁇ Raw material example> 2,3,4-Tetrachlorobutane was charged in an amount of 80 g, and a leak test was conducted in the same manner as in the first reactor, and the mixture was kept at 35 ° C. with stirring.
- the fluorine gas concentration in the first reactor outlet (gas discharge line) gas was 3% by volume (the remainder was mainly nitrogen gas).
- the exhaust gas exiting from the outlet (gas exhaust line) of the first reactor was continuously introduced into the liquid phase part of the second reactor and reacted while stirring at a reaction temperature of 35 ° C. At this time, no fluorine gas was detected in the gas at the outlet (gas discharge line) of the second reactor.
- the fluorine gas concentration in the first reactor outlet (gas discharge line) gas was about 22% by volume (the remainder was mainly nitrogen gas).
- the outlet gas of the second reactor was analyzed, no fluorine gas was detected in the outlet gas of the second reactor.
- the reaction was restarted while supplying the supply gas (40% by volume fluorine gas) as described above.
- the fluorine gas concentration in the first reactor outlet gas was about 40% by volume, and the reaction in the first reactor was completed.
- the fluorine gas concentration in the outlet gas of the second reactor was 0.1% by volume or less.
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Abstract
Description
本発明は、出発原料として1,2,3,4-テトラクロロブタンを用いて、これに溶媒の存在下、無触媒でフッ素ガスを供給して、1,2,3,4-テトラクロロブタンとフッ素ガスとを反応させて1,2,3,4-テトラクロロヘキサフルオロブタンを製造する方法である。
本発明で出発原料として使用される1,2,3,4-テトラクロロブタンは、例えば、下記の化学式に示すように、工業的に生産されているクロロプレンゴムの製造段階で副生成物として生成する。下記の式(1)はクロロプレンゴムを製造する際の主反応を示す式である。式(2)は式(1)で示す反応が進行する際に同時に進行する副反応の例を示す式である。
本発明で使用する溶媒(反応溶媒)はフッ素ガスと反応しにくく、反応条件で液体状態を維持することができる化合物であることが望ましい。このような化合物としては、クロロカーボン類やクロロフルオロカーボン類を挙げることができる。
本発明では溶媒の存在下、複数の反応器を用いて、無触媒で、1,2,3,4-テトラクロロブタンにフッ素ガスを供給して1,2,3,4-テトラクロロブタンとフッ素ガスとを反応させるに際して、一の反応器から排出される未反応のフッ素ガスの一部または全部を該一の反応器とは別の反応器に導入することにより、1,2,3,4-テトラクロロヘキサフルオロブタンを製造する。
(1)複数の反応器を用いて1,2,3,4-テトラクロロブタンとフッ素ガスとを接触させ、一の反応器から排出される未反応のフッ素ガスの一部または全部を該一の反応器とは別の反応器に導入する方法
(2)直列に配置された複数の反応器で1,2,3,4-テトラクロロブタンとフッ素ガスを接触させ、上流側の反応器から排出される未反応のフッ素ガスの一部または全部を下流側の反応器に導入する方法
(2)の方法が特に好ましい。
(1)反応効率がよい。
(2)1,2,3,4-テトラクロロブタン中のメソ体含有量が比較的高い場合であっても、メソ体を溶解するための加熱を行う必要がないかあるいは加熱したとしても加熱温度を低く抑えることができる。
(3)1,2,3,4-テトラクロロブタンのC-C開裂などが生じにくい。
上記のようにして反応させることにより1,2,3,4-テトラクロロブタンはフッ素化され、少なくともその一部は1,2,3,4-テトラクロロヘキサフルオロブタンになる。この1,2,3,4-テトラクロロヘキサフルオロブタンの大部分は反応溶媒中に溶解して存在するので、上記のように反応させた後の反応生成液には、反応溶媒、フッ化水素、原料としての1,2,3,4-テトラクロロブタン、この反応により生成した1,2,3,4-テトラクロロヘキサフルオロブタン、さらには副反応物などが含有されている。
工業的に生産されている1,3-ブタジエンの塩素化反応を行い、主として3,4-ジクロロブテン-1および1,4-ジクロロブテン-2を生成させた。1,4-ジクロロブテン-2を異性化反応により3,4-ジクロロブテン-1とし、副生物を蒸留により分離して3,4-ジクロロブテン-1を得た。これをガスクロマトグラフィ-にて分析したところ、3,4-ジクロロブテン-1の純度は99.3モル%であった。この3,4-ジクロロブテン-1を無溶媒下で塩素ガスにより塩素化し、得られた混合物を蒸留により分離精製して、1,2,3,4-テトラクロロブタンを得た。これをガスクロマトグラフィ-で分析したところ、純度は99.1モル%であり、dl体/メソ体の割合は約49/51であった。
第一反応器として内容積1000mlのSUS304製(テフロン(登録商標)ライニング)反応器を用いた。この反応器中に、溶媒としてテトラクロロメタン380gにフッ化水素20gを溶解させたものと、上記<原料例>で得られた1,2,3,4-テトラクロロブタンを100g仕込み、窒素ガスを圧力1.0MPaで導入し、漏れテストを行った後、窒素ガスをパージし、攪拌しながら温度を35℃に保った。
[実施例1]の条件で反応を繰り返して得られた粗1,2,3,4-テトラクロロヘキサフルオロブタンを含む溶液を蒸留塔(理論段数15段)に仕込んで蒸留した。得られた高沸点物を水酸化カリウム水溶液と接触させ、ゼオライト(モレキュラ-シ-ブス4A)を用いて18℃で脱水処理した。該処理を経た高沸点物を蒸留塔(理論段数25段)に仕込み、分離精製を行い目的物である1,2,3,4-テトラクロロヘキサフルオロブタンと主としてテトラクロロメタンを得た。これをガスクロマトグラフィ-で分析したところ、1,2,3,4-テトラクロロヘキサフルオロブタンの純度は約99.8質量%であった。
第一反応器として内容積1000mlのSUS製反応器を用いた。この中に、溶媒として[実施例2]で得られた1,2,3,4-テトラクロロヘキサフルオロブタン380gにフッ化水素20gを溶解させたものと、<原料例>で得られた1,2,3,4-テトラクロロブタンを100g仕込み、窒素ガスを圧力1.0MPaで導入して漏れテストを行った後、窒素ガスをパージし、撹拌しながら温度を40℃に保った。
Claims (10)
- 溶媒の存在下、複数の反応器を用いて、無触媒で、1,2,3,4-テトラクロロブタンにフッ素ガスを供給して1,2,3,4-テトラクロロブタンとフッ素ガスとを反応させるに際して、
一の反応器から排出される未反応のフッ素ガスの一部または全部を該一の反応器とは別の反応器に導入することを特徴とする1,2,3,4-テトラクロロヘキサフルオロブタンの製造方法。 - 前記複数の反応器が直列に配置され、上流側の反応器から排出される未反応のフッ素ガスの一部または全部を下流側の反応器に導入することを特徴とする請求項1に記載の1,2,3,4-テトラクロロヘキサフルオロブタンの製造方法。
- さらに下流側の反応器から排出される未反応のフッ素ガスの一部または全部を上流側の反応器に導入することを特徴とする請求項2に記載の1,2,3,4-テトラクロロヘキサフルオロブタンの製造方法。
- 前記複数の反応器が、直列に配置された2つの反応器であることを特徴とする請求項2または3に記載の1,2,3,4-テトラクロロヘキサフルオロブタンの製造方法。
- 前記溶媒がフッ化水素を含むことを特徴とする請求項1に記載の1,2,3,4-テトラクロロヘキサフルオロブタンの製造方法。
- 前記1,2,3,4-テトラクロロブタン100質量%中に、その光学異性体であるdl体が40質量%以上含有されることを特徴とする請求項1に記載の1,2,3,4-テトラクロロヘキサフルオロブタンの製造方法。
- 前記1,2,3,4-テトラクロロブタンとフッ素ガスとの反応により得られる1,2,3,4-テトラクロロヘキサフルオロブタンを含む反応生成液を蒸留塔に導入して、
該反応生成液を1,2,3,4-テトラクロロヘキサフルオロブタンを含む液と前記溶媒を含む液とに分離し、
分離した溶媒を含む液を、1,2,3,4-テトラクロロブタンとフッ素ガスとの反応を行う反応器に戻して循環使用することを特徴とする請求項1に記載の1,2,3,4-テトラクロロヘキサフルオロブタンの製造方法。 - 請求項1に記載の方法で得られた1,2,3,4-テトラクロロヘキサフルオロブタンを含む反応生成液を蒸留塔に導入して、
該反応生成液を1,2,3,4-テトラクロロヘキサフルオロブタンを含む液と前記溶媒を含む液とに分離し、
分離した1,2,3,4-テトラクロロヘキサフルオロブタンを含む液の少なくとも一部をアルカリ物質および/または水と接触させることを特徴とする1,2,3,4-テトラクロロヘキサフルオロブタンの精製方法。 - 前記アルカリ物質および/または水と接触した1,2,3,4-テトラクロロヘキサフルオロブタンを含む液を、さらに多孔質精製剤と接触させることを特徴とする請求項8に記載の1,2,3,4-テトラクロロヘキサフルオロブタンの精製方法。
- 前記多孔質精製剤が、ゼオライトであることを特徴とする請求項9に記載の1,2,3,4-テトラクロロヘキサフルオロブタンの精製方法。
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