Method for producing fluoroethane

Abstract

To provide a method for producing hydrofluoroethane in high selectivity by using hydrochlorofluoroethane as a raw material.SOLUTION: A method for producing a fluoroethane represented by the following general formula (1): CH2X1CHX2X3 (1), (Wherein X1, X2, and X3 each independently represent a hydrogen atom or a fluorine atom, and at least one of X1, X2, and X3 represents a fluorine atom.) and comprising a step A of obtaining the fluoroethane from a chlorofluoroethane represented by the following general formula (2): CX4ClFCX5X6X7 (2), (Wherein X4, X5, X6 and X7 each independently represent a hydrogen atom, a fluorine atom or a chlorine atom, and at least one of X5, X6 and X7 represents a hydrogen atom) in the presence of a catalyst.SELECTED DRAWING: None

Description

Technical Field

[0001] The present disclosure relates to a method for producing fluoroethane.

Background Art

[0002] Fluoroethane represented by 1,1,2-trifluoroethane (hereinafter, also simply referred to as "HFC-143" in this specification) is known as a raw material for producing various refrigerants. Various methods have been proposed as methods for producing fluoroethane such as HFC-143.

[0003]

[0004] For example, in Patent Document 1, a technique for producing chlorotrifluoroethylene or trifluoroethylene by a hydrogenation reaction such as 1,1,2-trichloro-1,2,2-trifluoroethylene (hereinafter, also simply referred to as "CFC-113" in this specification) in the presence of a hydrogenation catalyst has been proposed. However, when producing fluoroethane such as HFC-143 by the method disclosed in Patent Document 1, there is a problem that the selectivity of the target product is low. In addition, a method for obtaining hydrofluoroethane from hydrochlorofluorocarbon (hereinafter, also simply referred to as "HCFC" in this specification) is not disclosed.

Prior Art Documents

Patent Documents

[0005]

Patent Document 1

Summary of the Invention

Problems to be Solved by the Invention

[0006] In view of the above circumstances, an object of the present disclosure is to provide a method for obtaining hydrofluoroethane with a high selectivity using hydrochlorofluoromethane as a raw material.

Means for Solving the Problems

[0007] As a result of intensive studies to solve the above problems, the present inventors have found that fluoroethane can be obtained in a high yield by using a catalyst. Based on such findings, the present inventors have further conducted studies and completed the present disclosure.

[0008] That is, the present disclosure provides a method for producing fluoroethane as follows. Item 1. The following general formula (1) CH2X 1 CHX 2 X 3 (1) 〔In formula (1), X 1 , X 2 , and X 3 each independently represents a hydrogen atom or a fluorine atom, and at least one of X 1 , X 2 , and X 3 represents a fluorine atom.〕 A method for producing fluoroethane represented by obtaining the fluoroethane from a chlorofluoroethane represented by the following general formula (2) in the presence of a catalyst CX 4 ClFCX 5 X 6 X 7 (2) 〔In formula (2), X 4 , X 5 , X 6 and X 7 each independently represents a hydrogen atom, a fluorine atom or a chlorine atom, and at least one of X 5 , X 6 and X 7 represents a hydrogen atom.〕, the method for producing fluoroethane including step A. Item 2. The method according to item 1, wherein the catalyst is at least one selected from the group consisting of Ni, Pd, Pt, Rh and Ru. Item 3. The method according to item 1 or 2, wherein the catalyst is supported on a carrier, and the carrier is a carbon-based carrier. Section 4. The method according to any one of items 1 to 3, wherein the fluoroethane is 1,1,2-trifluoroethane (HFC-143), 1,1-difluoroethane (HFC-152a), 1,2-difluoroethane (HFC-152), or fluoroethane (HFC-161). Section 5. The method according to any one of items 1 to 4, wherein the chlorofluoroethane is 1,2-dichloro-1,1,2-trifluoroethane (HCFC-123a) or 1,1-dichloro-1,2,2-trifluoroethane (HCFC-123b). Section 6. The method according to any one of items 1 to 5, wherein a hydrogenation reaction is carried out in step A. Section 7. The method according to item 6, wherein the hydrogenation reaction is carried out under temperature conditions of 150°C to 350°C. Section 8. The method according to item 6 or 7, wherein the hydrogenation reaction is carried out by adding hydrogen to the chlorofluoroethane in a molar ratio of H2 / chlorofluoroethane of 1 to 20. Section 9. The hydrogenation reaction is carried out under gas phase conditions, as described in any of items 6 to 8. Section 10. A method for producing a fluoroolefin, further comprising step B, of carrying out a dehydrofluoride reaction on fluoroethane obtained by a manufacturing method described in any of items 1 to 9 to obtain a fluoroolefin. [Effects of the Invention]

[0009] According to the method for producing fluoroethane according to the present disclosure as described above, fluoroethane can be obtained in high yield. [Modes for carrying out the invention]

[0010] In this specification, "contains" is a concept that encompasses all of the following: "contains," "consist essentially of," and "consist of."

[0011] (1. Method for producing fluoroethane) The method for producing fluoroethane in this disclosure is based on the following general formula (1) CH2X 1 CHX 2 X 3 (1) [In formula (1), X 1 , X 2 , and X 3 Each of these independently represents a hydrogen atom or a fluorine atom, and X 1 , X 2 , and X 3 At least one of them represents a fluorine atom. This is a method for producing fluoroethane represented by [the formula shown].

[0012] The method for producing fluoroethane in the presence of a catalyst is as follows: CX 4 ClFCX 5 X 6 X 7 (2) [In formula (2), X 4 , X 5 , X 6 and X 7 Each of these independently represents a hydrogen atom, a fluorine atom, or a chlorine atom, and X 5 , X 6 and X 7 The process includes step A, which involves obtaining the fluoroethane from a chlorofluoroethane represented by [ ], where at least one of the is a hydrogen atom.

[0013] Step A described above is carried out as a hydrogenation reaction, preferably in a reactor in the presence of a catalyst. Common raw materials are used as the hydrogenating agent. In addition to hydrogen gas, hydrogenating agents such as hydrazine can be used, but hydrogen gas is preferably used.

[0014] As the catalyst, a metal catalyst is preferred, more preferably Ni, Pd, Pt, Rh, or Ru, and particularly preferably Pd.

[0015] Furthermore, it is more preferable to use the above catalyst supported on a carrier. A wide range of known carriers can be used, and there are no particular limitations. Examples of constituent materials include activated carbon, amorphous carbon, graphite, and other carbon-based materials such as diamond; porous aluminosilicates represented by zeolites; aluminophosphates; aluminum oxide; silicon oxide; titanium oxide; zirconia oxide; zinc oxide; and aluminum fluoride. Only one of these may be used, or multiple may be used in combination. Among these, it is preferable to use the above-mentioned carbon-based materials to create a carbon-based carrier.

[0016] Regarding the amount of metal supported in the catalyst, it is preferable that the amount of metal supported be 0.2% by mass or more, more preferably 0.5% by mass or more, and even more preferably 1.0% by mass or more, with the total mass of the carrier and metal being 100% by mass. Furthermore, it is preferable that the mass of the catalyst be 5% by mass or less, with the total mass of the carrier and catalyst being 100% by mass, and more preferably 4% by mass or less.

[0017] The method for preparing the catalyst is not particularly limited, and a wide range of known preparation methods can be used. For example, a catalyst on which a noble metal is supported on a support can be obtained by immersing the support in a solution containing the noble metal, thereby impregnating the support with the solution, and then, if necessary, performing neutralization, drying, and calcination. In this case, the amount of noble metal supported on the support can be controlled by adjusting the concentration of the solution, the impregnation time, etc.

[0018] The fluoroethane represented by formula (1) above is preferably 1,1,2-trifluoroethane (HFC-143), 1,1-difluoroethane (HFC-152a), 1,2-difluoroethane (HFC-152), or fluoroethane (HFC-161). The manufacturing method disclosed herein allows for the production of only one type of fluoroethane or multiple types simultaneously. When producing multiple types of fluoroethane simultaneously, it is also preferable to separate them into individual fluoroethane components using a rectification column or the like.

[0019] Furthermore, the chlorofluoroethane represented by formula (2) above is not particularly limited, and examples include 1,2-dichloro-1,1,2-trifluoroethane (HCFC-123a), 1,1-dichloro-1,2,2-trifluoroethane (HCFC-123b), and 1,1,2-trichloro-1,2,2-trifluoroethane (CFC-113). These may be used individually or in combination by mixing multiple types. For example, using HCFC-123a or HCFC-123b individually, or using a mixture of HCFC-123a and HCFC-123b, are also preferred embodiments.

[0020] The reaction carried out in step A is not particularly limited as long as it is a reaction that can replace the fluorine or chlorine atoms bonded to the carbon atoms in fluoroethane with hydrogen atoms. Specifically, it is preferable to carry out a hydrogenation reaction.

[0021] When the hydrogenation reaction is carried out in step A, the amount of hydrogen added to the chlorofluoroethane represented by formula (2) is preferably 1 or more in terms of the molar ratio of H2 / chlorofluoroethane, more preferably 2 or more, even more preferably 3 or more, and particularly preferably 5 or more. Furthermore, it is preferable that the molar ratio be 20 or less, more preferably 18 or less, even more preferably 15 or less, and particularly preferably 13 or less. By setting the H2 / chlorofluoroethane ratio to or above this lower limit, it is possible to suppress the decrease in catalyst activity and improve the selectivity of the target product. On the other hand, by setting it to or below this upper limit, it is possible to suppress the generation of excess hydrogen and improve the reaction efficiency and yield.

[0022] In this case, the temperature conditions for carrying out the hydrogenation reaction are preferably 150°C or higher, and more preferably 180°C or higher. Furthermore, the temperature conditions are preferably 350°C or lower, and more preferably 320°C or lower. By setting the temperature above this lower limit, a suitable raw material conversion rate and selectivity for the target product can be obtained. On the other hand, by setting the temperature below this upper limit, the progress of side reactions can be suppressed, catalyst degradation can be suppressed, and the yield can be improved.

[0023] When carrying out a hydrogenation reaction, if the amount (mass) of catalyst packed into the reaction system is W (g), and the total flow rate of chlorofluoroethane and hydrogen gas represented by formula (2) into the reaction system is F0 (cc / sec), then the contact time expressed as W / F0 is preferably 0.1 (g·sec / cc) or more, more preferably 0.5 (g·sec / cc) or more, and even more preferably 1.0 (g·sec / cc) or more. Furthermore, the contact time is preferably 20 (g·sec / cc) or less, more preferably 15 (g·sec / cc) or less, and even more preferably 10 (g·sec / cc) or less. By setting the contact time within this numerical range, a high conversion rate and selectivity can be obtained, resulting in an efficient process.

[0024] In the reaction of step A, the reaction system may contain compounds other than chlorofluoroethane represented by formula (2). For example, it may contain chlorotrifluoroethylene (CTFE) and / or 1,1,2-trifluoroethylene (HFO-1123).

[0025] The reaction in step A described above proceeds, for example, according to reaction equation 1 below.

[0026] [ka]

[0027] In the above reaction equation, both HCFC-133 and HCFC-133b can be converted to HFC-143, and the generation of either of these useful products that can be converted to the target product can contribute to improving selectivity.

[0028] (2. Method for producing fluoroolefins) The method for producing fluoroolefins according to this disclosure includes a step of obtaining a fluoroolefin by a dehydrofluorination reaction of fluoroethane obtained by the above-described method for producing fluoroethane. Hereinafter, this step will be defined as step B.

[0029] The method for producing fluoroolefins described herein uses the following general formula (1) CH2X 1 CHX 2 X 3 (1) [In formula (1), X 1 , X 2 , and X 3 Each of these independently represents a hydrogen atom or a fluorine atom, and X 1 , X 2 , and X 3 At least one of them represents a fluorine atom. By carrying out a dehydrofluoridation reaction on fluoroethane represented by the following general formula (3), preferably the following CX 8 X 9 =CX 10 X 11 (3) [In formula (3), X 8 , X 9 , X 10 and X 11 X represents a hydrogen atom, a fluorine atom, or a chlorine atom, and is either the same or different. 8 , X 9 , X 10 and X 11 At least one of them represents a hydrogen atom, X 8 , X 9 , X 10 and X 11 [At least one of them represents a fluorine atom.] A fluoroolefin represented by the above can be obtained.

[0030] In step B, the method of the dehydrofluoride reaction is not particularly limited and can be carried out under conditions similar to those of known dehydrofluoride reactions. For example, the dehydrofluoride reaction can be carried out in the gas phase in the presence of a dehydrofluoride catalyst.

[0031] In the method for producing fluoroolefins according to this disclosure, when 1,1,2-trifluoroethane (HFC-143) is used as the fluoroethane, the defluoridation reaction follows the following reaction equation. CF2HCFH2 → CHF = CHF + HF

[0032] The catalyst for hydrogen fluoride removal is not particularly limited, and a wide range of known catalysts can be used. Examples include chromium oxide, chromium fluoride oxide, aluminum oxide, aluminum fluoride oxide, and the like.

[0033] The catalyst for hydrogen fluoride removal is preferably supported on a carrier. Examples of carriers include carbon, alumina (Al2O3), zirconia (ZrO2), silica (SiO2), and titania (TiO2). As for carbon, activated carbon, amorphous carbon, graphite, diamond, etc., can be used.

[0034] The dehydrofluoride reaction in step B can also be carried out in the presence of an oxidizing agent. Examples of oxidizing agents include oxygen, chlorine, bromine, or iodine, with oxygen being particularly preferred. The concentration of the oxidizing agent is not particularly limited and can be the same as that of known dehydrofluoride reactions.

[0035] The reaction temperature for the dehydrofluoride reaction is not particularly limited and can be the same as that of known dehydrofluoride reactions. For example, it can be 300°C or higher, preferably 320°C or higher, more preferably 340°C or higher, and particularly preferably 350°C or higher. Alternatively, the reaction temperature for the dehydrofluoride reaction can be 600°C or lower, preferably 550°C or lower, more preferably 500°C or lower, and particularly preferably 450°C or lower.

[0036] The reaction time and pressure during the dehydrofluoride reaction are not particularly limited, and a wide range of known conditions can be used. The dehydrofluoride reaction can be carried out in the presence of either an inert gas or air. As inert gases, helium, nitrogen, argon, etc., as well as fluorocarbons and hydrofluorocarbons such as HFC-23, FC-14, FC-116, HFC-152a, and HFC-161, which do not participate in the reaction, can also be used. The dehydrofluoride reaction may be carried out in either a continuous or batch manner.

[0037] The method for producing fluoroolefins according to this disclosure may include other steps as needed, in addition to step B. Furthermore, in the method for producing fluoroolefins according to this disclosure, the raw materials can be separated and recycled from the crude product obtained by this method.

[0038] By carrying out step B, the target fluoroolefin, for example, a compound represented by general formula (4), is obtained. The fluoroolefin obtained by the dehydrofluoridation step is one or more types.

[0039] The resulting fluoroolefin can be determined by the fluoroethane used in the dehydrofluoridation step. Examples of fluoroolefins include 1,2-difluoroethylene (HFO-1132), 1,1-difluoroethylene (HFO-1132a), and trifluoroethylene (HFO-1123).

[0040] In the method for producing fluoroolefins according to this disclosure, when HFC-143 is used as fluoroethane, the resulting fluoroolefin is HFO-1132. In method 2 of this disclosure, when HFC-143a is used as fluoroethane, the resulting fluoroolefin is HFO-1132a. In the method for producing fluoroolefins according to this disclosure, when HFC-134 is used as fluoroethane, the resulting fluoroolefin is HFO-1123. HFO-1132 may include trans-1,2-difluoroethylene [(E)-HFO-1132] and cis-1,2-difluoroethylene [(Z)-HFO-1132].

[0041] When obtaining a fluoroolefin by the method for producing a fluoroolefin according to the present disclosure described above, the method for producing fluoroethane according to the present disclosure and the method for producing a fluoroolefin according to the present disclosure may be carried out sequentially, or they may be carried out independently.

[0042] While embodiments of this disclosure have been described above, this disclosure is by no means limited to these examples, and can be implemented in various forms without departing from the gist of this disclosure. [Examples]

[0043] The embodiments of this disclosure will be described in more detail below based on the examples, but this disclosure is not limited to these examples.

[0044] (Example 1) A 0.2 kg activated carbon catalyst supported with 2% by mass of Pd was packed into a Hastelloy C reaction tube with an inner diameter of 50 mm and dried by nitrogen purging at 250°C for 3 hours. The reactor temperature was then set to 200°C, and the reduction reaction was carried out by supplying 2.7 g / min of HCFC-123a and 3600 N ml / min of hydrogen. The W / F0 ratio at this time was 3, and the H2 / HCFC-123a molar ratio was 9. After washing the outlet gas with water and drying it with calcium chloride, analysis by GC (Shimadzu GC-2030) revealed that HFC-143 was obtained in high yield (HCFC-123a conversion rate: 28.8%, selectivity for HFC-143 and useful substances convertible to HFC-143: 95.6%).

[0045] (Example 2) A 0.2 kg activated carbon catalyst supported with 2% by mass of Pd was packed into a Hastelloy C reaction tube with an inner diameter of 50 mm and dried by nitrogen purging at 250°C for 3 hours. The reactor temperature was then set to 250°C, and the reduction reaction was carried out by supplying 2.7 g / min of HCFC-123a and 3600 N ml / min of hydrogen. The W / F0 ratio at this time was 3, and the H2 / HCFC-123a molar ratio was 9. After washing the outlet gas with water and drying it with calcium chloride, analysis by GC (Shimadzu GC-2030) revealed that HFC-143 was obtained in high yield (HCFC-123a conversion rate: 70.4%, selectivity for HFC-143 and useful substances convertible to HFC-143: 97.6%).

[0046] (Example 3) A 0.2 kg activated carbon catalyst supported with 2% by mass of Pd was packed into a Hastelloy C reaction tube with an inner diameter of 50 mm and dried by nitrogen purging at 250°C for 3 hours. The reactor temperature was then set to 300°C, and the reduction reaction was carried out by supplying 2.7 g / min of HCFC-123a and 3600 N ml / min of hydrogen. The W / F0 ratio at this time was 3, and the H2 / HCFC-123a molar ratio was 9. After washing the outlet gas with water and drying it with calcium chloride, analysis by GC (Shimadzu GC-2030) revealed that HFC-143 was obtained in high yield (HCFC-123a conversion rate: 98.7%, selectivity for HFC-143 and useful substances convertible to HFC-143: 98.3%).

[0047] The results of Examples 1 to 3 described above are summarized in Table 1 below.

[0048] [Table 1]

Claims

1. The following general formula (1) CH ２ X １ CHX ２ X ３ (1) [In formula (1), X １ , X ２ , and X ３ each independently represent a hydrogen atom or a fluorine atom, and at least one of X １ , X ２ , and X ３ represents a fluorine atom.] A method for producing fluoroethane represented by the following: A method for producing fluoroethane, comprising step A, which involves obtaining the fluoroethane from 1,2-dichloro-1,1,2-trifluoroethane (HCFC-123a) or 1,1-dichloro-1,2,2-trifluoroethane (HCFC-123b) in the presence of a catalyst.

2. The method according to claim 1, wherein the catalyst is at least one selected from the group consisting of Ni, Pd, Pt, Rh, and Ru.

3. The method according to claim 1 or 2, wherein the catalyst is supported on a carrier, and the carrier is a carbon-based carrier.

4. The method according to claim 1 or 2, wherein the fluoroethane is 1,1,2-trifluoroethane (HFC-143), 1,1-difluoroethane (HFC-152a), 1,2-difluoroethane (HFC-152), or fluoroethane (HFC-161).

5. The method according to claim 1 or 2, wherein a hydrogenation reaction is carried out in step A.

6. The method according to claim 5, wherein the hydrogenation reaction is carried out under temperature conditions of 150°C to 350°C.

7. The hydrogenation reaction involves adding hydrogen to the chlorofluoroethane, H ２ The method according to claim 5, which is carried out by adding chlorofluoroethane in a molar ratio of 1 to 20.

8. The method according to claim 5, wherein the hydrogenation reaction is carried out under gas phase conditions.

9. A method for producing a fluoroolefin, further comprising step B, of carrying out a dehydrofluoride reaction on fluoroethane obtained by the production method described in claim 1 or 2 to obtain a fluoroolefin.

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