JP2022139965A - Method for producing fluorine-containing vinyl sulfonic acid fluoride or fluorine-containing vinyl sulfonate, and method for separating the same - Google Patents

Abstract

To provide a method for producing fluorine-containing vinyl sulfonic acid fluoride and/or fluorine-containing vinyl sulfonate in high yield.SOLUTION: A method for producing fluorine-containing vinyl sulfonic acid fluoride and/or fluorine-containing vinyl sulfonate is provided. In a reaction between a fluorine-containing vinyl sulfonic acid anhydride (1) represented by general formula (1) and an alkali metal fluoride, the alkali metal fluoride is added to the fluorine-containing vinyl sulfonic acid anhydride (1) under heating. (In general formula (1), m is an integer of 0-3 and n is an integer of 1-6.)SELECTED DRAWING: None

Description

TECHNICAL FIELD The present invention relates to a method for producing a fluorine-containing vinylsulfonic acid fluoride or a fluorine-containing vinylsulfonate, and a method for separating the same. The present invention also relates to a method for reusing compounds used in the separation method.

（ｐは０～６の整数、ｑは１～６の整数）
一般式（５）で表されるフッ素系高分子電解質は、下記一般式（６）で表される含フッ素ビニルスルホン酸フルオリド（６）とテトラフルオロエチレン（ＴＦＥ）との共重合体をケン化反応及び酸処理を施すことによって製造できることが知られている。

（ｐは０～６の整数、ｑは１～６の整数）
上記一般式（６）で表される含フッ素ビニルスルホン酸フルオリド（６）の製造方法として、下記一般式（１）：

（式中、ｍは０～３の整数、ｎは１～６の整数）
で表される含フッ素ビニルスルホン酸無水物（１）と、
フッ化水素、金属フッ化物、４級アンモニウムフルオリド、及び４級ホスホニウムフルオリドからなる群より選択される１種以上であるフッ素化剤とを、
接触・混合させることにより、下記一般式（３）：

（式中、ｍは０～３の整数、ｎは１～６の整数）
で表される含フッ素ビニルスルホン酸フルオリド（３）を製造方法が開示されている（特許文献１）。また、該特許文献では、上記含フッ素ビニルスルホン酸フルオリド（３）を製造する際、同時に下記一般式（４）：

（式中、ｍは０～３の整数、ｎは１～６の整数、Ｍ^２はＬｉ、Ｎａ、Ｋ、Ｒｂ、又はＣｓである。）
で表される含フッ素ビニルスルホン酸塩（４）を製造できることが開示されている。さらに、上記含フッ素ビニルスルホン酸塩（４）を再利用し、上記含フッ素ビニルスルホン酸フルオリド（３）を製造する方法も開示されている。また、含フッ素ビニルスルホン酸塩（４）は、別法によっても含フッ素ビニルスルホン酸フルオリド（３）に変換できることが開示されており、有用な化合物であることが知られている（特許文献２）。 Conventionally, a fluorine-based polymer electrolyte (5) represented by the following general formula (5) has been mainly employed as a main component of membranes for fuel cells, catalyst binder polymers for fuel cells, membranes for salt electrolysis, and the like.

(p is an integer from 0 to 6, q is an integer from 1 to 6)
The fluorine-based polymer electrolyte represented by the general formula (5) is obtained by saponifying a copolymer of a fluorine-containing vinyl sulfonic acid fluoride (6) represented by the following general formula (6) and tetrafluoroethylene (TFE). It is known that it can be produced by reaction and acid treatment.

(p is an integer from 0 to 6, q is an integer from 1 to 6)
As a method for producing the fluorine-containing vinyl sulfonic acid fluoride (6) represented by the general formula (6), the following general formula (1):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6)
A fluorine-containing vinyl sulfonic anhydride (1) represented by
a fluorinating agent that is one or more selected from the group consisting of hydrogen fluoride, metal fluorides, quaternary ammonium fluorides, and quaternary phosphonium fluorides;
By contacting and mixing, the following general formula (3):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6)
A method for producing a fluorine-containing vinylsulfonic acid fluoride (3) represented by is disclosed (Patent Document 1). Further, in this patent document, when producing the fluorine-containing vinyl sulfonic acid fluoride (3), the following general formula (4) is used at the same time:

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6, and ^M2 is Li, Na, K, Rb, or Cs.)
It is disclosed that a fluorine-containing vinyl sulfonate (4) represented by can be produced. Furthermore, a method of reusing the fluorine-containing vinylsulfonate (4) to produce the fluorine-containing vinylsulfonic acid fluoride (3) is also disclosed. It is also disclosed that the fluorine-containing vinylsulfonate (4) can be converted to the fluorine-containing vinylsulfonic acid fluoride (3) by another method, and is known to be a useful compound (Patent Document 2). ).

WO2020/012913 U.S. Pat. No. 3,560,568

In Patent Document 1, by reacting a fluorine-containing vinylsulfonic anhydride (1) where m = 0 and n = 2 with sodium fluoride or potassium fluoride, m = 0 and n = 2 Although a method for producing the fluorine-containing vinylsulfonic acid fluoride (3) and the fluorine-containing vinylsulfonic acid salt (4) is disclosed, the fluorine-containing vinylsulfonic acid fluoride, which is the raw material of the fluorine-containing polymer electrolyte (5), is disclosed. There is a demand for a production method that can obtain (3) in a higher yield. There is also a demand for a method for separating the fluorine-containing vinylsulfonic acid fluoride (3) and the fluorine-containing vinylsulfonate (4).

The present inventors have made intensive studies to solve the above problems, and as a result, in the reaction between the fluorine-containing vinylsulfonic anhydride (1) and the alkali metal fluoride (2), under heating, the fluorine-containing The inventors have found that the above object can be achieved by adding the alkali metal fluoride (2) to the vinylsulfonic anhydride (1), and have completed the present invention. In addition, a method capable of separating the fluorine-containing vinyl sulfonic acid fluoride (3) and the fluorine-containing vinyl sulfonate (4) and a method of reusing the compounds used for the separation were also found.

（式中、ｍは０～３の整数、ｎは１～６の整数）
で表される含フッ素ビニルスルホン酸フルオリド（３）、及び／又は
下記一般式（４）：

式中、ｍは０～３の整数、ｎは１～６の整数、ＭはＫ、Ｒｂ、又はＣｓである。）
で表される含フッ素ビニルスルホン酸塩（４）の製造方法であり、
下記一般式（１）：

（式中、ｍは０～３の整数、ｎは１～６の整数）
で表される含フッ素ビニルスルホン酸無水物（１）と、
下記一般式（２）：
ＭＦ （２）
（式中、Ｍは、Ｋ、Ｒｂ、又はＣｓである。）
で表されるアルカリ金属フッ化物（２）との反応において、
加熱下で、含フッ素ビニルスルホン酸無水物（１）に、アルカリ金属フッ化物（２）を添加する、
ことを特徴とする、製造方法。
［２］
反応温度が、６０～２５０℃である、［１］に記載の製造方法。
［３］
前記含フッ素ビニルスルホン酸無水物（１）の物質量（α）に対する前記アルカリ金属フッ化物（２）の物質量（β）の比率（β／α）が、１～１００である、［１］又は［２］に記載の製造方法。
［４］
下記一般式（３）：

（式中、ｍは０～３の整数、ｎは１～６の整数）
で表される含フッ素ビニルスルホン酸フルオリド（３）の製造方法である、［１］に記載の製造方法。
［５］
下記一般式（４）：

（式中、ｍは０～３の整数、ｎは１～６の整数、ＭはＫ、Ｒｂ、又はＣｓである。）
で表される含フッ素ビニルスルホン酸塩（４）の製造方法である、［１］に記載の製造方法。
［６］
前記含フッ素ビニルスルホン酸フルオリド（３）を分離する工程を含む、［１］に記載の製造方法。
［７］
前記含フッ素スルホン酸フルオリド（３）を蒸留する工程を含む、［６］に記載の製造方法。
［８］
前記含フッ素スルホン酸フルオリド（３）と、抽出化合物とを混合する工程を含む、［６］に記載の製造方法。
［９］
前記抽出化合物が、水、無機塩含有水溶液、アルコール化合物、アミド化合物、及びスルホ化合物からなる群より選ばれる少なくとも１種の化合物である、［８］に記載の製造方法。
［１０］
前記無機塩含有水溶液が、炭酸塩類、硫酸塩類、チオ硫酸塩類、酢酸塩類、リン酸塩類、クエン酸塩類、酒石酸塩類、及び四ホウ酸塩類からなる群より選ばれる少なくとも１種の無機塩化合物を含む水溶液である、［９］に記載の製造方法。
［１１］
前記含フッ素スルホン酸フルオリド（３）の質量（ε）に対する前記抽出化合物の質量（ζ）の比率（ζ／ε）が、０．１～１００である、［８］に記載の製造方法。
［１２］
含フッ素スルホン酸フルオリド（３）と、抽出化合物とを混合する前記工程により得られた混合溶液を、静置し、前記含フッ素スルホン酸フルオリド（３）を含む相と、前記抽出化合物を含む相とに分離する工程を含む、［８］に記載の製造方法。
［１３］
抽出化合物を含む前記相を、含フッ素スルホン酸フルオリド（３）と、抽出化合物とを混合する前記工程に再利用する、［１２］に記載の製造方法。
［１４］
含フッ素スルホン酸フルオリド（３）を含む前記相から、含フッ素スルホン酸フルオリド（３）を、蒸留により分離する工程を含む、［１２］に記載の製造方法。
［１５］
反応残渣を分離する工程を含む、［１］に記載の製造方法。
［１６］
前記反応残渣と、溶解化合物とを混合し、含フッ素スルホン酸塩溶解液を調製する工程を含む、［１５］に記載の製造方法。
［１７］
前記溶解化合物が、エーテル化合物、ケトン化合物、エステル化合物、カーボネート化合物、及びニトリル化合物からなる群より選ばれる少なくとも１種の化合物である、［１６］に記載の製造方法。
［１８］
前記反応残渣の質量（γ）に対する前記溶解化合物の質量（δ）の比率（δ／γ）が、０．０１～１００である、［１６］に記載の製造方法。
［１９］
前記含フッ素スルホン酸塩溶解液をろ過し、含フッ素スルホン酸塩含有ろ液を得る工程を含む、［１６］に記載の製造方法。
［２０］
前記含フッ素スルホン酸塩溶解液をろ過し、アルカリ金属フッ化物（２）を含むろ物を得る工程を含む、［１６］に記載の製造方法。
［２１］
アルカリ金属フッ化物（２）を含む前記ろ物を、前記含フッ素ビニルスルホン酸無水物（１）と前記アルカリ金属フッ化物（２）との前記反応に再利用する、［２０］に記載の製造方法。
［２２］
前記含フッ素スルホン酸塩含有ろ液から、前記溶解化合物を含む揮発成分を分離し、前記含フッ素ビニルスルホン酸塩（４）を得る工程を含む、［１９］に記載の製造方法。
［２３］
溶解化合物を含む前記揮発成分を、反応残渣と、溶解化合物とを混合し、含フッ素スルホン酸塩溶解液を調製する前記工程に再利用する、［２２］に記載の製造方法。
［２４］
前記含フッ素スルホン酸塩含有ろ液に、水を添加し、混合する工程を含む、［１９］に記載の製造方法。
［２５］
前記含フッ素スルホン酸塩含有ろ液の質量（ι）と前記水の総質量（κ）の比率（κ／ι）が、０．１～１００である、［２４］に記載の製造方法。
［２６］
前記含フッ素スルホン酸塩含有ろ液に、水を添加し、混合する工程により得られた溶液から、前記溶解化合物を含む揮発成分を分離し、含フッ素スルホン酸塩含有水溶液を調製する工程を含む、［２４］に記載の製造方法。
［２７］
前記含フッ素スルホン酸塩含有ろ液に、水を添加し、混合する工程により得られた溶液から、前記溶解化合物を含む揮発成分を分離し、含フッ素スルホン酸塩含有水溶液を調製する工程において分離した溶解化合物を含む前記揮発成分から、水を分離する工程を含む、［２６］に記載の製造方法。
［２８］
溶解化合物を含む前記揮発成分を、反応残渣と、溶解化合物とを混合し、含フッ素スルホン酸塩溶解液を調製する前記工程に再利用する、［２６］又は［２７］に記載の製造方法。
［２９］
前記含フッ素スルホン酸塩含有ろ液に、水を添加し、混合する工程により得られた溶液から、前記溶解化合物を含む揮発成分を分離し、含フッ素スルホン酸塩含有水溶液を調製する工程において分離した前記溶解化合物を含む揮発成分から、水を分離する工程において分離した水を、前記含フッ素スルホン酸塩含有ろ液に、水を添加し、混合する前記工程に再利用する、［２４］に記載の製造方法。 That is, the present invention is as follows.
[1]
The following general formula (3):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6)
Fluorinated vinyl sulfonic acid fluoride (3) represented by and/or the following general formula (4):

In the formula, m is an integer of 0-3, n is an integer of 1-6, and M is K, Rb, or Cs. )
A method for producing a fluorine-containing vinyl sulfonate (4) represented by
The following general formula (1):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6)
A fluorine-containing vinyl sulfonic anhydride (1) represented by
The following general formula (2):
MF (2)
(In the formula, M is K, Rb, or Cs.)
In the reaction with an alkali metal fluoride (2) represented by
adding an alkali metal fluoride (2) to a fluorine-containing vinylsulfonic anhydride (1) under heating;
A manufacturing method characterized by:
[2]
The production method according to [1], wherein the reaction temperature is 60 to 250°C.
[3]
The ratio (β/α) of the substance amount (β) of the alkali metal fluoride (2) to the substance amount (α) of the fluorine-containing vinylsulfonic anhydride (1) is 1 to 100 [1] Or the production method according to [2].
[4]
The following general formula (3):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6)
The production method according to [1], which is a production method of the fluorine-containing vinyl sulfonic acid fluoride (3) represented by
[5]
The following general formula (4):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6, and M is K, Rb, or Cs.)
The production method according to [1], which is a production method for the fluorine-containing vinyl sulfonate (4) represented by
[6]
The production method according to [1], comprising the step of separating the fluorine-containing vinyl sulfonic acid fluoride (3).
[7]
The production method according to [6], comprising the step of distilling the fluorine-containing sulfonic acid fluoride (3).
[8]
The production method according to [6], comprising the step of mixing the fluorine-containing sulfonic acid fluoride (3) and an extraction compound.
[9]
The production method according to [8], wherein the extraction compound is at least one compound selected from the group consisting of water, an inorganic salt-containing aqueous solution, an alcohol compound, an amide compound, and a sulfo compound.
[10]
The inorganic salt-containing aqueous solution contains at least one inorganic salt compound selected from the group consisting of carbonates, sulfates, thiosulfates, acetates, phosphates, citrates, tartrates, and tetraborates. The production method according to [9], which is an aqueous solution containing
[11]
The production method according to [8], wherein the ratio (ζ/ε) of the mass (ζ) of the extracted compound to the mass (ε) of the fluorine-containing sulfonic acid fluoride (3) is 0.1-100.
[12]
The mixed solution obtained by the above step of mixing the fluorine-containing sulfonic acid fluoride (3) and the extraction compound is allowed to stand, and a phase containing the fluorine-containing sulfonic acid fluoride (3) and a phase containing the extraction compound are formed. The production method according to [8], including the step of separating into.
[13]
The production method according to [12], wherein the phase containing the extraction compound is reused in the step of mixing the fluorine-containing sulfonic acid fluoride (3) and the extraction compound.
[14]
The production method according to [12], comprising a step of separating the fluorine-containing sulfonic acid fluoride (3) from the phase containing the fluorine-containing sulfonic acid fluoride (3) by distillation.
[15]
The production method according to [1], including the step of separating reaction residues.
[16]
The production method according to [15], comprising the step of mixing the reaction residue and a dissolved compound to prepare a fluorine-containing sulfonate solution.
[17]
The production method according to [16], wherein the dissolved compound is at least one compound selected from the group consisting of ether compounds, ketone compounds, ester compounds, carbonate compounds, and nitrile compounds.
[18]
The production method according to [16], wherein the ratio (δ/γ) of the mass (δ) of the dissolved compound to the mass (γ) of the reaction residue is 0.01-100.
[19]
The production method according to [16], comprising filtering the fluorine-containing sulfonate solution to obtain a fluorine-containing sulfonate-containing filtrate.
[20]
The production method according to [16], comprising the step of filtering the fluorine-containing sulfonate solution to obtain a filtrate containing the alkali metal fluoride (2).
[21]
The production according to [20], wherein the filter cake containing the alkali metal fluoride (2) is reused for the reaction between the fluorine-containing vinylsulfonic anhydride (1) and the alkali metal fluoride (2). Method.
[22]
The production method according to [19], comprising a step of separating volatile components including the dissolved compound from the fluorine-containing sulfonate-containing filtrate to obtain the fluorine-containing vinyl sulfonate (4).
[23]
The production method according to [22], wherein the volatile component containing the dissolved compound is mixed with the reaction residue and the dissolved compound and reused in the step of preparing the fluorine-containing sulfonate solution.
[24]
The production method according to [19], comprising the step of adding water to the fluorine-containing sulfonate-containing filtrate and mixing.
[25]
The production method according to [24], wherein the ratio (κ/ι) between the mass (ι) of the fluorine-containing sulfonate-containing filtrate and the total mass (κ) of the water is 0.1-100.
[26]
a step of separating volatile components including the dissolved compound from the solution obtained by the step of adding water to the fluorine-containing sulfonate-containing filtrate and mixing to prepare a fluorine-containing sulfonate-containing aqueous solution; , the manufacturing method according to [24].
[27]
A volatile component containing the dissolved compound is separated from the solution obtained by adding water to the fluorine-containing sulfonate-containing filtrate and mixing, and separated in a step of preparing a fluorine-containing sulfonate-containing aqueous solution. The production method according to [26], comprising the step of separating water from the volatile components containing the dissolved compounds.
[28]
The production method according to [26] or [27], wherein the volatile component containing the dissolved compound is mixed with the reaction residue and the dissolved compound and reused in the step of preparing the fluorine-containing sulfonate solution.
[29]
A volatile component containing the dissolved compound is separated from the solution obtained by adding water to the fluorine-containing sulfonate-containing filtrate and mixing, and separated in a step of preparing a fluorine-containing sulfonate-containing aqueous solution. The water separated in the step of separating water from the volatile components containing the dissolved compound is reused in the step of adding water to the fluorine-containing sulfonate-containing filtrate and mixing, [24] Method of manufacture as described.

According to the present invention, fluorine-containing vinylsulfonic acid fluoride (3) can be produced in high yield. In addition, fluorine-containing vinyl sulfonate (4) can be produced. Furthermore, the fluorine-containing vinylsulfonic acid fluoride (3) and the fluorine-containing vinylsulfonate (4) can be separated, and the compounds obtained by the separation can be reused.

EMBODIMENT OF THE INVENTION Hereinafter, the form (henceforth "this embodiment") for implementing this invention is demonstrated in detail. However, the present invention is not limited to the following embodiments, and various modifications can be made within the scope of the gist of the present invention.

（式中、ｍは０～３の整数、ｎは１～６の整数）
で表される含フッ素ビニルスルホン酸フルオリド（３）、及び／又は
下記一般式（４）：

式中、ｍは０～３の整数、ｎは１～６の整数、ＭはＫ、Ｒｂ、又はＣｓである。）
で表される含フッ素ビニルスルホン酸塩（４）の製造方法であり、
下記一般式（１）：

式中、ｍは０～３の整数、ｎは１～６の整数）
で表される含フッ素ビニルスルホン酸無水物（１）と、
下記一般式（２）：
ＭＦ （２）
（式中、Ｍは、Ｋ、Ｒｂ、又はＣｓである。）
で表されるアルカリ金属フッ化物（２）との反応において、
加熱下で、含フッ素ビニルスルホン酸無水物（１）に、アルカリ金属フッ化物（２）を添加する、方法である。 The production method of the present embodiment uses the following general formula (3):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6)
Fluorinated vinyl sulfonic acid fluoride (3) represented by and/or the following general formula (4):

In the formula, m is an integer of 0-3, n is an integer of 1-6, and M is K, Rb, or Cs. )
A method for producing a fluorine-containing vinyl sulfonate (4) represented by
The following general formula (1):

In the formula, m is an integer of 0 to 3, n is an integer of 1 to 6)
A fluorine-containing vinyl sulfonic anhydride (1) represented by
The following general formula (2):
MF (2)
(In the formula, M is K, Rb, or Cs.)
In the reaction with an alkali metal fluoride (2) represented by
In this method, an alkali metal fluoride (2) is added to a fluorine-containing vinylsulfonic anhydride (1) under heating.

In the present specification, the fluorine-containing vinylsulfonic anhydride (1) is referred to as "compound (1)," the alkali metal fluoride (2) is referred to as "compound (2)," and the fluorine-containing vinylsulfonic acid fluoride (3). may be referred to as "compound (3)", and the fluorine-containing vinyl sulfonate (4) may be referred to as "compound (4)".
Details of reaction conditions and the like for producing compound (1), compound (2), and compound (3) and/or compound (4) are described below.

（式中、ｍは０～３の整数、ｎは１～６の整数）
で表される。
含フッ素ビニルスルホン酸無水物（１）は、１種単独であっても、複数種を組み合わせて用いてもよい。 <Fluorine-Containing Vinyl Sulfonic Anhydride (1) (Compound (1))>
The fluorine-containing vinylsulfonic anhydride (1) has the following general formula (1):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6)
is represented by
The fluorine-containing vinylsulfonic anhydride (1) may be used singly or in combination.

m is preferably 0 to 1, more preferably 0, because it is easily available or manufactured and tends to be economically efficient.
n is preferably 1 to 4, more preferably 2 to 4, and even more preferably 2, because it is easy to obtain or manufacture and tends to be economically efficient.
As a combination of m and n, it is particularly preferable that m=0 and n=2.

The method for producing the fluorine-containing vinylsulfonic anhydride (1) is not particularly limited, and it can be produced by a conventionally known method. For example, it can be produced by the method described in International Publication No. 2020/012913.

<Alkali metal fluoride (2) (compound 2)>
The alkali metal fluoride (2) has the following general formula (2):
MF (2)
(In the formula, M is K, Rb, or Cs.)
is represented by
Alkali metal fluoride (2) may be used singly or in combination.

M is more preferably K or Cs because it is easily available and tends to be economical, and K is more preferable from the same point of view.

As for compound (2), one having a reduced water content can also be used, if necessary.
The method for reducing the water content of compound (2) is not particularly limited as long as it is a generally available method, and examples thereof include a method of heating, a method of heating under vacuum, and a method of heating under circulation of dry gas. be done.
The heating temperature is not particularly limited as long as it can reduce the water content of compound (2), but is preferably 600° C. or less because decomposition of compound (2) tends to be suppressed. It is more preferably 300 ° C. or less because it suppresses excessive heating and tends to be more economical, and from the same viewpoint, it is more preferably 250 ° C. or less, and particularly 200 ° C. or less. preferable. In addition, since the water content tends to be reduced, the temperature is preferably 100°C or higher, more preferably 120°C or higher, and even more preferably 150°C or higher.
The dry gas is not particularly limited as long as it is a commonly used dry gas, and examples thereof include dry air and dry nitrogen.

When reacting the fluorine-containing vinylsulfonic anhydride (1) with the alkali metal fluoride (2), if necessary, for example, ether compounds, nitrile compounds, amide compounds, sulfo compounds, saturated hydrocarbon compounds, aromatic Group hydrocarbon compounds, halogenated hydrocarbon compounds, alcohol compounds, ketone compounds, ester compounds, water and the like can be used as additives.
The above additives may be used singly or in combination.
The above additives can be used by mixing with compound (1) and compound (2), or either one, or by mixing an additive with a mixture of compound (1) and compound (2). can also be used.

The additive is not particularly limited as long as it is a commonly used compound, but specific examples include tetrahydrofuran, 2-methyltetrahydrofuran, tetrahydropyran, 4-methyltetrahydropyran, cyclopentylmethyl ether, diethyl ether, Dipropyl ether, dibutyl ether, dipentyl ether, dihexyl ether, diheptyl ether, dioctyl ether, methyl tert-butyl ether, 1,4-dioxane, 1,2-dimethoxyethane, 1,2-diethoxyethane, ethylene glycol dibutyl ether , 1,2-dimethoxypropane, diethylene glycol dimethyl ether, diethylene glycol diethyl ether, diethylene glycol isopropyl methyl ether, diethylene glycol butyl methyl ether, triethylene glycol dimethyl ether, triethylene glycol butyl methyl ether, tetraethylene glycol dimethyl ether, and dipropylene glycol dimethyl ether. compound, acetonitrile, propionitrile, butyronitrile, isobutyronitrile, 2-methylbutyronitrile, cyclohexanecarbonitrile, benzonitrile, adiponitrile, m-fluorobenzonitrile, 2,3-difluorobenzonitrile, 2,3,4 -trifluorobenzonitrile, 2,3,6-trifluorobenzonitrile, 2-fluoro-3-(trifluoromethyl)benzonitrile, 2-fluoro-4-(trifluoromethyl)benzonitrile, 2-fluoro-5 -(trifluoromethyl)benzonitrile, 3-fluoro-5-(trifluoromethyl)benzonitrile, 2,3,4,5-tetrafluorobenzonitrile, fluoroacetonitrile, difluoroacetonitrile, 2-fluorobenzonitrile, 2, Nitrile compounds such as 4,5-trifluorobenzonitrile, o-(trifluoromethyl)benzonitrile, and pentafluorobenzonitrile, N,N-dimethylformamide, N,N-diethylformamide, N,N-dimethylacetamide, Amide compounds such as N,N-diethylacetamide, N-methylpyrrolidone, tetramethylurea, and 1,3-dimethyl-2-imidazolidinone, dimethylsulfoxide, dibutylsulfoxide, ethylmethylsulfone, ethylisopropylsulfone, sulfolane, and 3-methy Sulfo compounds such as Rusulfolane, saturated hydrocarbons such as n-pentane, n-hexane, isohexane, n-heptane, n-octane, isooctane, n-nonane, n-decane, cyclopentane, cyclohexane, cycloheptane, and cyclooctane aromatic hydrocarbon compounds such as benzene, toluene, xylene, ethylbenzene, diethylbenzene, isopropylbenzene, naphthalene, tetralin, and biphenyl, methylene chloride, chloroform, carbon tetrachloride, ethylene chloride, trichloroethane, tetrachloroethane, pentachloroethane, hexachloroethane Halogenated hydrocarbon compounds such as chloroethane, dichloroethylene, trichlorethylene, tetrachlorethylene, dichloropropane, trichloropropane, isopropyl chloride, butyl chloride, hexyl chloride, chlorobenzene, dichlorobenzene, trichlorobenzene, chlorotoluene, and chloronaphthalene, methanol, ethanol, propanol , isopropanol, butanol, isobutanol, pentanol, hexanol, heptanol, octanol, nonanol, decanol, undecanol, dodecanol, cyclohexanol, and alcohol compounds such as benzyl alcohol, acetone, methylacetone, ethyl methyl ketone, methyl propyl ketone, methyl Ketone compounds such as butyl ketone, methyl isobutyl ketone, methylhexyl ketone, diethyl ketone, ethyl butyl ketone, dipropyl ketone, diisobutyl ketone, and cyclohexanone, and ethyl acetate, propyl acetate, butyl acetate, isobutyl acetate, pentyl acetate, hexyl acetate , octyl acetate, cyclohexyl acetate, methyl propionate, ethyl propionate, butyl propionate, methyl benzoate, ethyl benzoate, propyl benzoate, butyl benzoate, and ester compounds such as benzyl benzoate.

If necessary, the above additives may be used with a reduced water content.
Low water content additives can be purchased or methods of reducing the water content of additives can be used. The method for reducing the water content of the additive is not particularly limited as long as it is a generally available method, and examples thereof include a method using a dehydrating agent and a method of distillation.
The dehydrating agent is not particularly limited as long as it is a commonly used dehydrating agent, and sodium hydride, magnesium sulfate, sodium sulfate, calcium sulfate, calcium chloride, zinc chloride, calcium oxide, magnesium oxide, diphosphorus pentoxide, Examples include activated alumina, silica gel, and molecular sieves. When a dehydrating agent is used, an additive containing the dehydrating agent may be used as long as it does not affect the reaction between compound (1) and compound (2). may be used.

<Ratio (β/α) of substance amount (β) of compound (2) to substance amount (α) of compound (1)>
The ratio (β/α) of the amount (β) of compound (2) to the amount (α) of compound (1) tends to increase the yield of compound (3), and the method for producing compound (3) is preferably 0.5 or more, more preferably 0.8 or more, because the economy tends to be excellent. It is more preferably 1 or more, particularly preferably 1.5 or more, because it tends to be possible to suppress the remaining unreacted compound (1).

The upper limit of the ratio (β/α) of the amount (β) of compound (2) to the amount (α) of compound (1) is not particularly limited. 3) tends to be more economical, it is preferably 100 or less, and from the same viewpoint, β/α is more preferably 50 or less, and β/α is 20 or less. It is more preferably 10, and particularly preferably 10 or less.

<Reaction between compound (1) and compound (2)>
In the present embodiment, the reaction temperature is the temperature at which the container containing compound (1) or the container in which compound (1) and compound (2) are reacted is heated from the outside. Although the reaction temperature is not particularly limited as long as it is within the range generally used, it is preferably 60 to 250°C.
Depending on the type of compound (2), the reactivity with compound (1) tends to increase, so the temperature is more preferably 70° C. or higher, further preferably 80° C. or higher, and 90° C. or higher. is particularly preferred.
Depending on the type of compound (1) and/or compound (3), deterioration due to heat tends to be suppressed, and the method for producing compound (3) tends to be more economical. Since volatilization is suppressed and the purity of compound (3) tends to increase, the reaction temperature is more preferably 200° C. or lower, still more preferably 170° C. or lower, even more preferably 160° C. or lower. Especially preferred.
The reaction temperature of compound (1) and compound (2) may be constant, or may be changed during the reaction within the above range.
In the production method of the present embodiment, compound (2) is added to compound (1) under heating. Heating compound (1) and/or compound (2) before mixing tends to improve the yield of compound (3) and compound (4). Here, heating means that compound (1) and/or compound (2) are heated before being mixed. One of compound (1) and compound (2) may be heated, or both may be heated. It is preferable to add compound (2) below the later temperature at the addition rate described below, and more preferably to heat only compound (1). The temperature after heating compound (1) and the temperature after heating compound (2) may be the same or different, but from the viewpoint of yield, they are preferably different. It is more preferable that the temperature after heating is higher than the temperature at the time of addition of compound (2).
The temperature after heating (preferably the temperature after heating of compound (1)) is preferably 60° C. or higher, more preferably 70° C. or higher, still more preferably 80° C. or higher, and particularly preferably 90° C. or higher. is. In addition, from the viewpoint of improving the yield of compound (3) and compound (4) and further increasing the purity of the resulting compound, the temperature is preferably 250° C. or lower, more preferably 200° C. or lower, and still more preferably 170° C. °C or less, particularly preferably 160°C or less.
From the viewpoint of yield, the difference between the temperature of compound (1) after heating and the temperature of compound (2) at the time of addition is preferably 0 to 200° C., more preferably 10 to 150° C., and further It is preferably 20 to 130°C.
Further, the temperature after heating (preferably the temperature after heating compound (1)) is within the range of the reaction temperature ±30° C. from the viewpoint of further improving the yield of compound (3) and compound (4). more preferably within the above reaction temperature range of ±20°C, more preferably within the above reaction temperature range of ±10°C, and particularly preferably within the above reaction temperature range of ±5°C.

The time from the start of adding compound (2) to compound (1) to the end of the addition of the entire amount (hereinafter sometimes referred to as "addition time") is not particularly limited as long as it is within a generally used range. The reaction time is preferably 1 minute or more, more preferably 3 minutes or more, and even more preferably 5 minutes or more, because side reactions due to a rapid reaction between compound (1) and compound (2) tend to be suppressed. In addition, by avoiding an excessive addition time such that the reaction of compound (1) is completed and compound (1) does not exist and the state where compound (1) and compound (2) do not react continues for a long time. , Since the production method tends to be more economical, the time is preferably 100 hours or less, more preferably 10 hours or less, even more preferably 5 hours or less, and 3 hours or less. is particularly preferred. The addition of compound (2) may be continuous or intermittent.

The rate at which compound (2) is added to compound (1) (meaning the value obtained by dividing the mass of added compound (2) by the addition time) is not particularly limited as long as it is within a generally used range. By avoiding excessive addition time such that the reaction of compound (1) is completed and compound (1) does not exist and the state where compound (1) and compound (2) do not react continues for a long time, it is economical It is preferably 0.01 g/min or more, more preferably 0.1 g/min or more, and even more preferably 0.3 g/min or more, because it tends to be a production method with excellent performance. , 0.5 g/min or more. From the viewpoint of suppressing a side reaction due to a rapid reaction between compound (1) and compound (2), the rate at which compound (2) is added to compound (1) is preferably 1000 g/min or less. /min or less, more preferably 20 g/min or less, and particularly preferably 5 g/min or less.
The rate at which compound (2) is added to compound (1) may be constant, or may be changed within the above range. In the early stage of addition of compound (2), reaction between compound (1) and compound (2) is likely to occur, but in the latter stage of addition of compound (2), reaction between compound (1) and compound (2) is less likely to occur. Therefore, in some cases, it is preferable to slow down the rate of addition at the beginning of the addition and increase the rate of addition toward the end of the addition.

Ratio of the rate of adding compound (2) to compound (1) with respect to the mass of compound (1) (value obtained by dividing the mass of added compound (2) by the addition time and the mass of compound (1) used, means, mass specific addition rate) is not particularly limited as long as it is within the range generally used, but the reaction of compound (1) is completed and compound (1) ceases to exist, and compound (1) and compound By avoiding an excessive addition time such that the state where (2) does not react for a long time, the production method tends to be more economical, so it is preferable that it is 0.01 g / min / g or more. It is preferably 0.05 g/min/g or more, still more preferably 0.08 g/min/g or more, and particularly preferably 0.1 g/min/g or more. From the viewpoint of suppressing a side reaction due to a rapid reaction between compound (1) and compound (2), it is preferably 1000 g/min/g or less, more preferably 100 g/min/g or less, and 10 g /min/g or less, and particularly preferably 3 g/min/g or less.
The rate of addition of compound (2) to compound (1) relative to the mass of compound (1) may be constant or may be changed within the above range.

After the addition of compound (2) is completed, the time for reacting the mixture of compound (1) and compound (2) is not particularly limited as long as it is within the range generally used, but the yield of compound (3) is preferably 0.1 hours or more, more preferably 0.3 hours or more, and even more preferably 0.5 hours or more, because the stability of the time is further increased. By avoiding an excessive reaction time, the production method tends to be more economical, so it is preferably 100 hours or less, more preferably 50 hours or less from the same viewpoint, and 10 hours or less. It is more preferable that the time is 5 hours or less, and particularly preferably 5 hours or less.

The pressure at which the compound (1) and the compound (2) are reacted is not particularly limited as long as it is within the range normally used, and may be pressurized, atmospheric pressure, or reduced pressure, and may be changed during the reaction. good too. Depending on the type of compound (1), it may volatilize at the reaction temperature. If compound (1) cannot be liquefied and reused, it is effective to apply pressure above atmospheric pressure. When the compound (3) to be produced is separated during the reaction of compound (1) and compound (2), either atmospheric pressure or reduced pressure is preferred. From the viewpoint of promoting separation of compound (3), reduced pressure is more preferable.

The atmosphere in which the compound (1) and the compound (2) are reacted is not particularly limited as long as it is an ordinary atmosphere, and an air atmosphere, a nitrogen atmosphere, an argon atmosphere, or the like is usually used. Among these, a nitrogen atmosphere and an argon atmosphere are preferable because they tend to allow the compound (3) to be produced more safely. A nitrogen atmosphere is more preferable because it tends to be a more economical manufacturing method. Since the separation of compound (3) tends to be accelerated, a flowing atmosphere may be used as a preferred method.
One type of reaction atmosphere may be used alone, or a plurality of types of reaction atmospheres may be used in combination.

The method used for reacting the compound (1) and the compound (2) is not particularly limited as long as it is a generally used method. shaft, 3-axis, 4-axis), stirring blade shape (e.g., fan, propeller, cross, butterfly, dragonfly, turbine, disk turbine, dispa, paddle, inclined paddle, helical, double helical, ribbon, straight blade, 45° twist blades, 90° twisted blades, etc.), installation of baffles in the mixing tank, and the like.
More specifically, if the device used for reacting compound (1) and compound (2) is exemplified, a pressurized kneader manufactured by Nippon Spindle Mfg. Co., Ltd., a wonder kneader, a kneading test device mix lab, a small volume Pressure type kneader, MS type compact pressure kneader, double arm type kneader, kneader with valve, kneader ruder, special pressure type kneader, decompression type pressure kneader, twin-screw taper extruder, twin-screw single-screw extruder, and feeder ruder, KRC Kneader, Batch Kneader, Pressure Kneader, Extruder, CD Dryer, SC Processor, and CD Dryer manufactured by Kurimoto, Ltd., BDM Twin Shaft Mixer manufactured by Inoue Seisakusho Co., Ltd., Butterfly Mixer, CDM Concentric Twin Shaft Mixer, Pony Mixer, Trimix, Planetary Mixer, PD Mixer, Kneader, Flushing Kneader, Salt Milling Kneader, Pressure Kneader, KX Kneader, Taiheiyo Kiko Co., Ltd. Pam Apex Mixer, Super Double Mixer, Nishimura Kikai Co., Ltd. Vertical Mixer, Ribbon Mixer, high-speed paddle mixer, and paddle mixer, Hosokawa Micron Co., Ltd. Baimix, Nauta mixer, solid air, micron thermoprocessor, and torus disk, Nara Machinery Co., Ltd. paddle dryer, single paddle dryer, Buno cooler, multi-fin Processor, extruder, and high-speed stirring mixing granulator, Kobelco Eco-Solutions Co., Ltd. PV mixer and SV mixer, Okawara Seisakusho Co., Ltd. ribocon and flow jet granulator, Japan Steel Works, Ltd. twin-screw kneading extruder , Primix Co., Ltd. HIVIS MIX, HIVIS DISPER MIX, and COMBI MIX, Aikosha Seisakusho Co., Ltd. ACM Series, Shinagawa Kogyosho Co., Ltd. Mixer, Twin Servo Mixer, S Kneader, Spherical Kneader, Spherical Bent Kneader , and high-speed kneading granulator, Japan Eirich Co., Ltd. intensive mixer and Ebactherm, Sugiyama Heavy Industries Co., Ltd. axial mixer and hemisphere mixer, Katsuragi Industry Co., Ltd. vacuum stirring dryer, Yasujima Co., Ltd. vacuum stirring Dryer, MG Co., Ltd. mixer, semi-pressurized kneader, kneader ruder, and vacuum extruder, Kurimoto, Ltd. KID dryer, Rotrova dryer, rotary dryer, and rotary kiln, Kobelco Eco-Solutions Co., Ltd. Konica electric heating type rotary kiln, gas heating type rotary kiln, batch type rotary kiln, desktop rotary kiln, vacuum desktop rotary kiln, and special atmosphere + vacuum rotary kiln, super rotary dryer made by Okawara Seisakusho Co., Ltd. , eco dryer, rotary kiln manufactured by Sugiyama Heavy Industries Co., Ltd., double cone mixer, double cone dryer manufactured by Katsuragi Industry Co., Ltd., rotary kiln manufactured by Yasujima Co., Ltd., and the like.
A single mixing device may be used, or a plurality of mixing devices may be used in combination.

The method of adding compound (1) includes a method of adding using its own weight, a method of adding under pressure, and a liquid feeding pump (e.g., smooth flow pump, motor-driven metering pump, solenoid-driven metering pump, air driving pumps, dynamic vacuum pumps, tube pumps, slurry pumps, magnet pumps, air-driven bellows pumps, electromagnetically-driven metering pumps, rotating displacement pumps, etc.). A method using a liquid-sending pump is preferable because it tends to be excellent in controllability of the rate of addition of compound (1).
The method of adding the compound (2) includes a method of adding using its own weight, and a method of adding by circulating an air flow (for example, suction pneumatic transportation, low pressure pneumatic transportation, high pressure pneumatic transportation, etc.). and the pneumatic transportation may be dry air transportation, nitrogen transportation, transportation in different atmospheres such as argon transportation) and powder feeders (e.g., screw feeders, vibrating feeders, circle feeders, conveyor feeders, auger types Examples include a method of adding using a powder filling machine, a metering powder feeder, a positive displacement powder feeder, etc.). A method using a powder feeder is preferred because it tends to be excellent in controllability of the rate of addition of compound (2).

Each device, addition means, container, etc. described above (for example, a device for reacting compound (1) and compound (2), a container for adding compound (1) using its own weight, and compound (1) Liquid feed pump used for addition), pipes connecting each, etc., as materials used in places where compound (1) and / or compound (2) come into contact, are generally used materials Examples include, but are not limited to, metals, metal alloys, resins, composites of metals and resins, and ceramics. More specific examples include titanium, nickel, zirconia, platinum, carbon steel, alloy steel, cast iron, stainless steel (SUS304, SUS304L, SUS430, SUS410, SUS316, SUS316L, SUS329J1, SUS329J4L, etc.), nickel-titanium alloys, Nickel-chromium-molybdenum alloys (Inconel (registered trademark) 600, 625, 718, X750, etc., Hastelloy (registered trademark) C-22, C276, etc.), nickel-copper alloys (Monel (registered trademark) 400, K, S, H, nickel Vac (registered trademark) 400, Nicoros (registered trademark) 400, etc.), nickel-cobalt-chromium-molybdenum alloy, nickel-molybdenum alloy (Hastelloy (registered trademark) ALLOY B2, B, etc.), nickel-cobalt alloy, nickel-iron alloy, nickel-tungsten alloy , cobalt-chromium alloys, cobalt-chromium-molybdenum alloys (ELGILOY), PHYNOX (registered trademark), etc., platinum-enriched stainless steel, fluorine-based resins (Teflon (registered trademark), tetrafluoroethylene and perfluoroalkoxy copolymer with ethylene, perfluoroethylene propene copolymer, ethylene tetrafluoroethylene copolymer, polyvinylidene fluoride, polychlorotrifluoroethylene, ethylene chlorotrifluoroethylene copolymer, etc.), polyether ether ketone, polypropylene, polyphenylene ether, polyamide 6, polyamide 66, aromatic polyamide, polyphenylene sulfide, polysulfone, polyethersulfone, polyetherimide, polyamideimide and the like.
The above materials may be used singly or in combination.

By reacting compound (1) with compound (2), compound (4) is produced together with compound (3). Compounds (3) and (4) can be converted into raw materials for fluorine-based polymer electrolytes, which are main components of membranes for fuel cells, catalyst binder polymers for fuel cells, membranes for salt electrolysis, and various fluorine compounds. is known to be a useful compound as a raw material from which the be done.

The method for separating the compound (3) is not particularly limited as long as it is a generally used method. While the compound (1) and the compound (2) are reacted, the compound (3) is distilled off and separated. method, after the reaction between compound (1) and compound (2) is completed, compound (3) is distilled off and separated, compound (3) can be dissolved, but compound (4) can be dissolved Depending on the compound that cannot be dissolved, a method of preparing a solution containing compound (3), removing the compound used for dissolution, and separating compound (3) can be exemplified. Among these, the method of distilling off and separating the compound (3) while reacting the compound (1) and the compound (2) is preferable because the compound (3) can be separated without complicated operations. When compound (3) is distilled off while reacting compound (1) and compound (2), if the reaction temperature is a temperature at which compound (3) can be distilled off, the reaction may be carried out at normal pressure. Then, a gas (e.g., nitrogen) inert to compound (3) may be passed under normal pressure, or may be performed under reduced pressure, or a gas (e.g., nitrogen) inert to compound (3) may be passed under reduced pressure. ) may be distributed. Further, when the reaction temperature is insufficient to distill off the compound (3), an inert gas (e.g., nitrogen) may be passed through the compound (3) at normal pressure, It may be carried out under reduced pressure, or an inert gas (eg, nitrogen) may be passed through compound (3) under reduced pressure.

The compound (3) can be dissolved, but the compound (4) cannot be dissolved, as long as it is a compound used in general boats, but is not particularly limited, but n-pentane, n-hexane, isohexane, n-heptane, n-octane, isooctane, n-nonane, n-decane, cyclopentane, cyclohexane, cycloheptane, cyclooctane, benzene, toluene, xylene, ethylbenzene, diethylbenzene, isopropylbenzene, naphthalene, tetralin, biphenyl, methylene chloride, chloroform, tetra Carbon chloride, ethylene chloride, trichloroethane, tetrachloroethane, pentachloroethane, hexachloroethane, dichloroethylene, trichlorethylene, tetrachloroethylene, dichloropropane, trichloropropane, isopropyl chloride, butyl chloride, hexyl chloride, chlorobenzene, dichlorobenzene, trichlorobenzene, chlorotoluene, chloro Hydrocarbon compounds such as naphthalene, fluorine compounds such as hydrofluoroethers, hydrofluorocarbons, hydrofluoroolefins, hydrochlorofluorocarbons, and hydrochlorofluoroolefins (more specifically, 3M Novec (registered trademark) ) series, and Fluorinert (registered trademark) series, Bertrell (registered trademark) series manufactured by Chemours, Solcan (registered trademark) manufactured by Solvay, Asahiklin (registered trademark) series manufactured by AGC Corporation, and Amorea (registered trademark) series, Cerephine (registered trademark) manufactured by Central Glass Co., Ltd. can be exemplified.
Compounds in which compound (3) is soluble but compound (4) is insoluble may be used singly or in combination.

The separated compound (3) can be purified if necessary. The method for increasing the purity is not particularly limited as long as it is a commonly used method, but a method of increasing the purity by distillation, a method of increasing the purity by distillation, a compound having a large solubility in the compound whose purity is reduced, and separating from the compound (3) A method of reducing the content of a compound that reduces the purity contained in the compound (3) by using a compound (hereinafter also referred to as an “extracted compound”), a method of combining these, etc. can be exemplified. .

Distillation of compound (3) is not particularly limited as long as the conditions are generally used, and any of atmospheric distillation, pressurized distillation, and vacuum distillation may be used. The distillation apparatus may be a plate column, a packed column, or a column combining them. As the tray deck of the plate column, any tray deck of bubble cap, sieve tray, movable valve, and fixed valve may be used. As the packing of the packed column, either regular packing or irregular packing may be used. When the amount of compound (3) to be distilled is small, an Oldershaw distillation apparatus, a distillation apparatus equipped with a Vigreux column, a distillation apparatus equipped with a rotating band column, or a packed distillation apparatus can be used. The filler is not particularly limited as long as it is a commonly used filler, but Raschig Ring, Lessing Ring, Pall Ring, Cross Ring, Medalpack, Tallpack, Omnipack, Berle Saddle, Interox Saddle, Dixon Packing, and McMahon. Examples include Packing, Helipack, Merapack, Gempack, Technopack, Flexipack, Sulzerpacking, Goodrollpacking, and the like. The reflux ratio and the number of theoretical plates can be in the range generally used as long as the reflux ratio and the number of theoretical plates can achieve the desired purity of the compound (3). Although it depends on the number of theoretical plates, the reflux ratio is preferably 100 or less, more preferably 50 or less, and even more preferably 25 or less from the viewpoint of suppressing the energy required for distillation. Since the purity of compound (3) tends to improve, the reflux ratio is preferably 1 or more, more preferably 3 or more, and even more preferably 5 or more. The theoretical plate number is preferably 300 or less, more preferably 200 or less, and even more preferably 100 or less, because the cost of the distillation apparatus can be reduced and the economy tends to be excellent. Since the purity of compound (3) tends to be improved, the number of theoretical plates is preferably 1 or more, more preferably 5 or more, and even more preferably 10 or more.

The separated compound (3) or the compound (3) distilled after separation can be mixed with the extracted compound to form a mixed solution.
The extraction compound is not particularly limited as long as it is a commonly used compound, but water, an inorganic salt-containing aqueous solution, methanol, ethanol, propanol, butanol, hexanol, cyclohexanol, ethylene glycol, propylene glycol, glycerol, and other alcohol compounds. , N,N-dimethylformamide, N,N-diethylformamide, N,N-dimethylacetamide, N,N-diethylacetamide, N-methylpyrrolidone, tetramethylurea, and 1,3-dimethyl-2-imidazolidinone and sulfo compounds such as dimethylsulfoxide, dibutylsulfoxide, ethylmethylsulfone, ethylisopropylsulfone, sulfolane, and 3-methylsulfolane. Among these, water and an inorganic salt-containing aqueous solution are preferable because they tend to suppress contamination with the compound (3).
The extraction compounds may be used singly or in combination.

In the present embodiment, the inorganic salt-containing aqueous solution is at least one selected from the group consisting of carbonates, sulfates, thiosulfates, acetates, phosphates, citrates, tartrates, and tetraborates. Aqueous solutions containing various inorganic salt compounds may be used.

The inorganic salt compound is not particularly limited as long as it is a commonly used compound. Specific examples include lithium hydrogen carbonate, sodium hydrogen carbonate, potassium hydrogen carbonate, rubidium hydrogen carbonate, cesium hydrogen carbonate, and ammonium hydrogen carbonate. , Lithium carbonate, sodium carbonate, potassium carbonate, rubidium carbonate, cesium carbonate, carbonates such as ammonium carbonate, lithium hydrogen sulfate, sodium hydrogen sulfate, potassium hydrogen sulfate, rubidium hydrogen sulfate, cesium hydrogen sulfate, ammonium hydrogen sulfate, lithium sulfate, Sulfates such as sodium sulfate, potassium sulfate, rubidium sulfate, cesium sulfate and ammonium sulfate; thiosulfates such as lithium thiosulfate, sodium thiosulfate, potassium thiosulfate, rubidium thiosulfate, cesium thiosulfate, ammonium thiosulfate and magnesium thiosulfate; Acetates such as lithium acetate, sodium acetate, potassium acetate, rubidium acetate, cesium acetate, ammonium acetate, trilithium phosphate, trisodium phosphate, tripotassium phosphate, trirubidium phosphate, tricesium phosphate, triphosphate ammonium, dilithium hydrogen phosphate, disodium hydrogen phosphate, dipotassium hydrogen phosphate, dirubidium hydrogen phosphate, dicesium hydrogen phosphate, diammonium hydrogen phosphate, lithium dihydrogen phosphate, sodium dihydrogen phosphate, Phosphates such as potassium dihydrogen phosphate, rubidium dihydrogen phosphate, cesium dihydrogen phosphate, ammonium dihydrogen phosphate, trilithium citrate, trisodium citrate, tripotassium citrate, trirubidium citrate, citric acid tricesium acid, triammonium citrate, dilithium hydrogen citrate, disodium hydrogen citrate, dipotassium hydrogen citrate, dirubidium hydrogen citrate, cesium hydrogen citrate, diammonium hydrogen citrate, lithium dihydrogen citrate , sodium dihydrogen citrate, potassium dihydrogen citrate, rubidium dihydrogen citrate, cesium dihydrogen citrate, citrates such as ammonium dihydrogen citrate, lithium tartrate, sodium tartrate, potassium tartrate, rubidium tartrate, cesium tartrate , ammonium tartrate, lithium sodium tartrate, sodium potassium tartrate, sodium potassium tartrate, sodium ammonium tartrate, potassium ammonium tartrate and other tartrates, lithium tetraborate, sodium tetraborate, potassium tetraborate, rubidium tetraborate, tetraborate cesium oxide, Tetraborates such as ammonium borate and the like are included.

Among these, sodium hydrogen carbonate, potassium hydrogen carbonate, cesium hydrogen carbonate, ammonium hydrogen carbonate, lithium carbonate, sodium carbonate, potassium carbonate, rubidium carbonate, and cesium carbonate are easily available and tend to be economically efficient. , ammonium carbonate, sodium hydrogen sulfate, potassium hydrogen sulfate, lithium sulfate, sodium sulfate, potassium sulfate, rubidium sulfate, cesium sulfate, ammonium sulfate, sodium thiosulfate, ammonium thiosulfate, magnesium thiosulfate, lithium acetate, sodium acetate, potassium acetate, acetic acid Rubidium, cesium acetate, ammonium acetate, trilithium phosphate, trisodium phosphate, tripotassium phosphate, disodium hydrogen phosphate, dipotassium hydrogen phosphate, diammonium hydrogen phosphate, sodium dihydrogen phosphate, dihydrogen phosphate potassium hydrogen phosphate, ammonium dihydrogen phosphate, trilithium citrate, trisodium citrate, tripotassium citrate, triammonium citrate, disodium hydrogen citrate, diammonium hydrogen citrate, sodium tartrate, lithium tetraborate, tetra Sodium borate, potassium tetraborate, ammonium tetraborate are preferred, sodium hydrogen carbonate, potassium hydrogen carbonate, ammonium hydrogen carbonate, sodium carbonate, potassium carbonate, ammonium carbonate, sodium hydrogen sulfate, potassium hydrogen sulfate, sodium sulfate, potassium sulfate , ammonium sulfate, sodium thiosulfate, ammonium thiosulfate, sodium acetate, potassium acetate, ammonium acetate, trisodium phosphate, tripotassium phosphate, disodium hydrogen phosphate, dipotassium hydrogen phosphate, diammonium hydrogen phosphate, diphosphate sodium hydrogen phosphate, potassium dihydrogen phosphate, ammonium dihydrogen phosphate, trisodium citrate, tripotassium citrate, triammonium citrate, disodium hydrogen citrate, diammonium hydrogen citrate, sodium tartrate, sodium tetraborate, Potassium tetraborate, ammonium tetraborate are more preferable, sodium hydrogen carbonate, potassium hydrogen carbonate, sodium carbonate, potassium carbonate, sodium hydrogen sulfate, potassium hydrogen sulfate, sodium sulfate, potassium sulfate, sodium thiosulfate, sodium acetate, potassium acetate , trisodium phosphate, tripotassium phosphate, disodium hydrogen phosphate, dipotassium hydrogen phosphate, sodium dihydrogen phosphate, and potassium dihydrogen phosphate are more preferred, sodium hydrogen carbonate, Particular preference is given to sodium carbonate, sodium hydrogen sulfate, sodium sulfate, sodium thiosulfate, sodium acetate, trisodium phosphate, disodium hydrogen phosphate, sodium dihydrogen phosphate.

The concentration of the inorganic salt-containing aqueous solution is not particularly limited, with the solubility of the inorganic salt compound being the upper limit. When the inorganic salt-containing aqueous solution is discarded after one use, excessive use of the inorganic salt compound is suppressed, and the production of compound (3) tends to be economically efficient. The concentration is preferably 0.5 times or less the solubility, more preferably 0.2 times or less, even more preferably 0.1 times or less, and 0.05 times or less. is particularly preferred. When the inorganic salt-containing aqueous solution is used multiple times, the solubility of the inorganic salt compound is excellent because it tends to maintain the property of reducing the content of the compound that reduces the purity contained in the compound (3). The concentration is preferably 0.5 times or more, more preferably 0.7 times or more, and even more preferably 0.9 times or more.

<Ratio (ζ/ε) of the mass (ζ) of the extracted compound to the mass (ε) of the compound (3) separated after the reaction between the compound (1) and the compound (2)>
The ratio (ζ/ε) of the mass (ζ) of the extracted compound to the mass (ε) of the compound (3) separated after the reaction between the compound (1) and the compound (2) is contained in the compound (3) Since the content of compounds that reduce purity tends to be further reduced, it is preferably 0.1 or more, more preferably 0.3 or more, and further preferably 0.5 or more. preferable.

The upper limit of the ratio (ζ/ε) of the mass (ζ) of the extracted compound to the mass (ε) of the compound (3) separated after the reaction between the compound (1) and the compound (2) is not particularly limited, but the compound ( Since the amount of 3) dissolved in the extracted compound tends to decrease and the amount of compound (3) dispersed in the extracted compound tends to decrease, ζ/ε is preferably 100 or less, It is more preferably 20 or less, still more preferably 10 or less, and particularly preferably 5 or less.

After the reaction between the compound (1) and the compound (2), the separated compound (3) and the extracted compound are stirred and mixed to improve the dissolution rate of the compound whose purity is reduced in the extracted compound. There is a tendency. The method of stirring is not particularly limited as long as it is a commonly used stirring method. Specific examples include stirring methods (stirring blade type, homogenizer, high-pressure homogenizer, ultrahigh-pressure homogenizer, ultrasonic homogenizer, Polytron homogenizer, etc. ), stirring blade shape (e.g., fan, propeller, cross, butterfly, dragonfly, turbine, disk turbine, dispa, paddle, inclined paddle, etc.), installation of baffles in the reactor, homogenizer shaft shape (universal type, stirring type , multiple ultrasonic wave type, open type, closed type, etc.). In addition, an apparatus equipped with the above stirring method can be used.
The stirring method and the device equipped with the stirring method may be used singly or in combination.

The time for stirring and mixing is not particularly limited as long as it is within the range generally used. It is preferably 0.01 hours or more, more preferably 0.1 hours or more, still more preferably 0.5 hours or more, and particularly preferably 1 hour or more. By avoiding excessive stirring and mixing time, the manufacturing method tends to be more economical, so the time is preferably 100 hours or less, and from the same point of view, the time is more preferably 50 hours or less. It is more preferably 1 hour or less, and particularly preferably 5 hours or less.

After the compound (3) and the extract compound are stirred and mixed, the mixed solution is allowed to stand to allow phase separation into a phase containing the compound (3) and a phase containing the extract compound.
The time to stand for phase separation is not particularly limited as long as it is within a range generally used, but the amount of the phase containing compound (3) dispersed in the phase containing the extracted compound is reduced, and the compound ( Since the amount obtained in 3) tends to increase, the time is preferably 0.01 hours or more, more preferably 0.1 hours or more, and even more preferably 0.5 hours or more. Since the production method tends to be more economical by avoiding an excessive standing time, the time is preferably 100 hours or less, more preferably 50 hours or less from the same viewpoint, and 10 hours. It is more preferably 5 hours or less, and particularly preferably 5 hours or less.

The temperature at which the fluorine-containing vinyl sulfonic acid fluoride (3) and the extraction compound are stirred and mixed and the temperature at which the phases are separated by standing are not particularly limited as long as they are generally used temperatures. The amount of the compound that reduces the purity tends to dissolve in the extraction compound to increase, and the amount of the phase containing compound (3) dispersed in the phase containing the extraction compound is reduced, and compound (3 ) tends to increase, the temperature is preferably −40° C. or higher, more preferably −20° C. or higher. From the same point of view and because there is a tendency to be excellent in economic efficiency when adjusting the temperature on an industrial scale, the temperature is more preferably 0° C. or higher, and particularly preferably 10° C. or higher.

The upper limit of the temperature at which the fluorine-containing vinyl sulfonic acid fluoride (3) and the extraction compound are stirred and mixed, and the temperature at which the phases are separated by standing are not particularly limited, but the dissolution of the compound (3) in the extraction compound is suppressed. is preferably 120° C. or lower, more preferably 100° C. or lower, even more preferably 80° C. or lower, and particularly preferably 60° C. or lower.
The temperature at which the fluorine-containing vinyl sulfonic acid fluoride (3) and the extraction compound are stirred and mixed and the temperature at which they are allowed to stand and phase-separate may be constant, or may be changed during the above range. good.

The pressure at which the fluorine-containing vinyl sulfonic acid fluoride (3) and the extraction compound are stirred and mixed and the pressure at which the phase is separated by standing are not particularly limited as long as they are within the range normally used, and the reaction is usually performed under atmospheric pressure. is done. However, depending on the type of the compound (3) and the extracted compound, they may volatilize, so in order to suppress volatilization, it is an effective means to pressurize at a pressure higher than the atmospheric pressure. When the volatilizing compound is liquefied and reused, the pressure may be reduced to atmospheric pressure or less.
The pressure at which the fluorine-containing vinyl sulfonic acid fluoride (3) and the extraction compound are stirred and mixed and the pressure at which they are allowed to stand and phase-separate may be constant, or may be changed within the above range. good.

The atmosphere in which the fluorine-containing vinyl sulfonic acid fluoride (3) and the extraction compound are stirred and mixed and the atmosphere in which the phases are separated by standing are not particularly limited as long as they are atmospheres normally used, and are usually an air atmosphere or a nitrogen atmosphere. , and an argon atmosphere are used. Among these, a nitrogen atmosphere and an argon atmosphere are preferable because they tend to produce the compound (3) more safely. A nitrogen atmosphere is more preferable because it tends to be a more economical manufacturing method.
The atmosphere in which the fluorine-containing vinyl sulfonic acid fluoride (3) and the extraction compound are stirred and mixed and the atmosphere in which the mixture is allowed to stand and phase-separate may be used singly or in combination of a plurality of atmospheres. good too.

The fluorine-containing vinyl sulfonic acid fluoride (3) and the extract compound are stirred and mixed, and allowed to stand for phase separation. The obtained phase containing the extract compound is composed of compound (1) and compound (2). After the reaction, in order to increase the purity of the separated compound (3), it may be reused when preparing the mixed solution.
The fluorine-containing sulfonic acid fluoride (3) may be separated by distillation from the phase-separated phase containing the fluorine-containing sulfonic acid fluoride (3).

In the reaction between compound (1) and compound (2), the amount of compound (2) is used less than the amount of compound (1), leaving unreacted compound (1) to produce compound (3). ) is separated, a method for recovering compound (1) by separating compound (1) and compound (4) produced, or a method for separating compound (3) produced and compound (1) from compound (4) , a method of recovering compound (1) by separating compound (3) and compound (1). By reusing the compound (1) after separation, it is possible to suppress the disposal of the compound (1) and improve the economic efficiency of the production of the compound (3), but the process for recovery is necessary. From the above point of view and between compound (1) and compound (2), compound (2) is easier to obtain and tends to be more economical to produce compound (3). Using a larger amount of compound (2) than 1), reducing unreacted compound (1), and forming a mixture containing compound (2), compound (3), and compound (4), After separating compound (3), the method of separating compound (4) from a mixture containing compound (2) and compound (4) tends to be more economical in producing compound (3). It is considered to be in

A mixture containing compound (2) and compound (4) obtained after reacting compound (1) and compound (2) to produce compound (3) and separating compound (3) (hereinafter referred to as " The method for separating compound (4) from "reaction residue") is not particularly limited as long as it is a generally used method. A compound having a small solubility (hereinafter referred to as "dissolved compound") is added to 2), and a solution in which compound (4) is dissolved in the dissolved compound (hereinafter referred to as "fluorine-containing sulfonate solution"). After that, compound (2) is removed by filtration, and then a compound having a large solubility in compound (4) is distilled off, or compound (4) is crystallized to obtain compound (4). is mentioned.

The dissolving compound is not particularly limited as long as it is a commonly used compound, but it is preferably at least one compound selected from the group consisting of ether compounds, ketone compounds, ester compounds, carbonate compounds, and nitrile compounds. .

Specific examples of dissolved compounds include tetrahydrofuran, 2-methyltetrahydrofuran, tetrahydropyran, 4-methyltetrahydropyran, cyclopentyl methyl ether, diethyl ether, dipropyl ether, dibutyl ether, dipentyl ether, dihexyl ether, and diheptyl ether. , dioctyl ether, methyl tert-butyl ether, 1,4-dioxane, 1,2-dimethoxyethane, 1,2-diethoxyethane, ethylene glycol dibutyl ether, 1,2-dimethoxypropane, diethylene glycol dimethyl ether, diethylene glycol diethyl ether, diethylene glycol Ether compounds such as isopropyl methyl ether, diethylene glycol butyl methyl ether, triethylene glycol dimethyl ether, triethylene glycol butyl methyl ether, tetraethylene glycol dimethyl ether, and dipropylene glycol dimethyl ether, acetone, methyl acetone, ethyl methyl ketone, methyl propyl ketone, methyl ketone compounds such as butyl ketone, methyl isobutyl ketone, methylhexyl ketone, diethyl ketone, ethyl butyl ketone, dipropyl ketone, diisobutyl ketone, and cyclohexanone; ethyl acetate, propyl acetate, butyl acetate, isobutyl acetate, pentyl acetate, hexyl acetate; Ester compounds such as octyl acetate, cyclohexyl acetate, methyl propionate, ethyl propionate, butyl propionate, methyl benzoate, ethyl benzoate, propyl benzoate, butyl benzoate, and benzyl benzoate, dimethyl carbonate, diethyl carbonate, di Propyl carbonate, dibutyl carbonate, ethyl methyl carbonate, fluoromethyl methyl carbonate, difluoromethyl methyl carbonate, trifluoromethyl methyl carbonate, bis(fluoromethyl) carbonate, bis(difluoromethyl) carbonate, bis(trifluoro methyl) carbonate, fluoromethyl difluoromethyl carbonate, 2,2,2-trifluoroethyl methyl carbonate, pentafluoroethyl methyl carbonate, ethyl trifluoromethyl carbonate, bis(2,2,2-trifluoroethyl) carbonate, ethylene carbonate, propylene carbonate, fluoroethylene carbonate, 4-(trimeric fluoromethyl)-1,3-dioxolan-2-one, 4,4-difluoro-1,3-dioxolan-2-one, 4-fluoro-4-methyl-1,3-dioxolan-2-one, 4- (fluoromethyl)-1,3-dioxolan-2-one, 4,5-difluoro-1,3-dioxolan-2-one, 4-fluoro-5-methyl-1,3-dioxolan-2-one, 4 ,5-difluoro-4,5-dimethyl-1,3-dioxolan-2-one, vinylene carbonate, vinylethylene carbonate, methylvinylene carbonate, carbonate compounds such as ethylvinylene carbonate, acetonitrile, propionitrile, Butyronitrile, isobutyronitrile, 2-methylbutyronitrile, cyclohexanecarbonitrile, benzonitrile, adiponitrile, fluoroacetonitrile, difluoroacetonitrile, 2-fluorobenzonitrile, 2,4,5-trifluorobenzonitrile, o-(trifluoro) fluoromethyl)benzonitrile, pentafluorobenzonitrile are more preferred, nitrile compounds such as 2-fluorobenzonitrile, 2,4,5-trifluorobenzonitrile, o-(trifluoromethyl)benzonitrile, and pentafluorobenzonitrile etc.

Among the above ether compounds, tetrahydrofuran, 2-methyltetrahydrofuran, tetrahydropyran, 4-methyltetrahydropyran, cyclopentyl methyl ether, diethyl ether, dipropyl ether, dibutyl ether, dipentyl Ether, dihexyl ether, methyl tert-butyl ether, 1,4-dioxane, 1,2-dimethoxyethane, 1,2-diethoxyethane, ethylene glycol dibutyl ether, 1,2-dimethoxypropane, diethylene glycol dimethyl ether are preferred. Since compound (4) tends to be highly soluble, tetrahydrofuran, 2-methyltetrahydrofuran, tetrahydropyran, diethyl ether, dipropyl ether, dibutyl ether, methyl tert-butyl ether, 1,4-dioxane, 1,2- More preferred are dimethoxyethane, 1,2-diethoxyethane and 1,2-dimethoxypropane. Tetrahydrofuran, tetrahydropyran, methyl tert-butyl ether, 1,4-dioxane, and 1,2-dimethoxyethane are more preferable because they are easily available or produced and tend to be economically efficient.

Among the above ketone compounds, acetone, ethyl methyl ketone, methyl propyl ketone, methyl butyl ketone, methyl isobutyl ketone, and cyclohexanone are preferable because compound (4) tends to have high solubility, and acetone, ethyl methyl ketone, methyl Propyl ketone and methyl isobutyl ketone are more preferred. Acetone, ethyl methyl ketone, and methyl isobutyl ketone are more preferable because they are readily available and tend to be economically efficient.

Ethyl acetate, propyl acetate, butyl acetate, isobutyl acetate, pentyl acetate, hexyl acetate, cyclohexyl acetate, methyl propionate, ethyl propionate, propionic acid Butyl is preferred, and ethyl acetate, propyl acetate, butyl acetate, isobutyl acetate, methyl propionate, ethyl propionate and butyl propionate are more preferred. Ethyl acetate, butyl acetate, and isobutyl acetate are more preferable because they are readily available and tend to be economically efficient.

Among the above carbonate compounds, dimethyl carbonate, diethyl carbonate, dipropyl carbonate, dibutyl carbonate, ethyl methyl carbonate, ethylene carbonate, propylene carbonate, vinylene carbonate, and vinylene carbonate are easily available and tend to be economically efficient. Vinyl ethylene carbonate, methyl vinylene carbonate and ethyl vinylene carbonate are preferred, and dimethyl carbonate, diethyl carbonate, dipropyl carbonate, dibutyl carbonate, ethyl methyl carbonate, ethylene carbonate and propylene carbonate are more preferred. Dimethyl carbonate, diethyl carbonate, ethyl methyl carbonate, ethylene carbonate, and propylene carbonate are more preferable, and dimethyl carbonate and ethylene carbonate are particularly preferable, because compound (4) tends to have a high solubility.

Among the above nitrile compounds, acetonitrile, propionitrile, butyronitrile, isobutyronitrile, 2-methylbutyronitrile, cyclohexanecarbonitrile, benzonitrile, adiponitrile, because they are easily available and tend to be economical are preferred, and acetonitrile, propionitrile, butyronitrile, benzonitrile and adiponitrile are more preferred. Acetonitrile, propionitrile, and adiponitrile are more preferable because compound (4) tends to have high solubility.

<Ratio (δ/γ) of the mass (δ) of the dissolved compound to the mass (γ) of the reaction residue>
The ratio (δ/γ) of the mass (δ) of the dissolved compound to the mass (γ) of the reaction residue is 0.01 or more because the amount of the compound (4) contained in the dissolved compound tends to increase. It is preferably 0.1 or more, more preferably 0.5 or more, still more preferably 0.7 or more, and particularly preferably 1.0 or more. The upper limit of the ratio (δ/γ) of the mass (δ) of the dissolved compound to the mass (γ) of the reaction residue is not particularly limited. It is preferably 100 or less, more preferably 50 or less, even more preferably 25 or less, and particularly preferably 10 or less, because it tends to be economically efficient.

The method for stirring the reaction residue and the dissolved compound is not particularly limited as long as it is a commonly used stirring method. ultrasonic homogenizer, polytron homogenizer, etc.), stirring blade shape (e.g., fan, propeller, cross, butterfly, dragonfly, turbine, disk turbine, dispa, paddle, inclined paddle, etc.), installation of baffles in the reactor, homogenizer shaft Shapes (universal type, stirring type, multi-ultrasound type, open type, closed type, etc.) and the like can be mentioned. In addition, an apparatus equipped with the above stirring method can be used.
The stirring method and the device equipped with the stirring method may be used singly or in combination.

The time for stirring the reaction residue and the dissolved compound is not particularly limited as long as it is within the range generally used. It is preferably at least 0.1 hours, more preferably at least 0.5 hours, and particularly preferably at least 1 hour. By avoiding excessive stirring and mixing time, the manufacturing method tends to be more economical, so the time is preferably 100 hours or less, and from the same point of view, the time is more preferably 50 hours or less. It is more preferably 1 hour or less, and particularly preferably 5 hours or less.

The temperature at which the reaction residue and the dissolved compound are stirred is not particularly limited as long as it is a temperature that is generally used. It is preferably at least -20°C, more preferably at least -20°C. From the same point of view and because there is a tendency to be excellent in economic efficiency when adjusting the temperature on an industrial scale, the temperature is more preferably 0° C. or higher, and particularly preferably 10° C. or higher. The upper limit of the temperature for stirring the reaction residue and the dissolved compound is not particularly limited, but volatilization may occur depending on the type of the dissolved compound, so volatilization can be suppressed and precipitation of compound (4) tends to be suppressed. Therefore, the temperature is preferably 120° C. or lower, more preferably 100° C. or lower, even more preferably 80° C. or lower, and particularly preferably 60° C. or lower.
The temperature at which the reaction residue and dissolved compound are stirred may be constant, or may be changed within the above range.

The pressure for stirring the reaction residue and the dissolved compound is not particularly limited as long as it is within the range normally used, and the stirring is usually under atmospheric pressure. However, since some dissolved compounds may volatilize, it is an effective means to apply pressure higher than the atmospheric pressure in order to suppress volatilization. When the volatilizing compound is liquefied and reused, the pressure may be reduced to atmospheric pressure or less.
The pressure for stirring the reaction residue and the dissolved compound may be constant, or may be changed within the above range.

The atmosphere in which the reaction residue and the dissolved compound are stirred is not particularly limited as long as it is an atmosphere normally used, and air atmosphere, nitrogen atmosphere, argon atmosphere, or the like is usually used. Among these, a nitrogen atmosphere and an argon atmosphere are preferable because they tend to produce the compound (4) more safely. A nitrogen atmosphere is more preferable because it tends to be a more economical manufacturing method.
The atmosphere for stirring the reaction residue and the dissolved compound may be used singly or in combination of a plurality of atmospheres.

The method for separating the compound (2) not dissolved in the fluorine-containing sulfonate solution is not particularly limited as long as it is a generally used method. A method of precipitating the compound (2), separating the solid from the liquid, and collecting the supernatant can be used. Among them, filtration separation is preferable because the recovery amount of the compound (4) is increased and the economy tends to be excellent in the production of the compound (4).

The method of filtration separation is not particularly limited as long as it is a commonly used method, and examples include gravity filtration, centrifugal filtration, pressure filtration, reduced pressure filtration, compression filtration, magnetic filtration, and electrostatic A method such as filtration can be used. These may be batch systems or continuous systems.
The filtration device is not particularly limited as long as it is a device that is generally used by the filtration method. A single-chamber type device, a horizontal running type device, a siphon type device, a basket type device, a separating plate type device, a decanter type device, a candle filter, and the like.
Filtration devices may be used singly or in combination.

More specific examples of filtration devices include strainers, sand filters, coke filters, sintered filter media, Nutsche filters, vibrating screens, rotary screens, belt strainers, candle plate discs, rotary drum filters, rotary Gravity filtration devices such as disk filters, belt filters, table filters, pan filters, and internal feed drum filters; Centrifugal filtration devices such as batch filters, quarter filters, scroll filters, pushers, vibrators, and centrifugal filters; , filter press, edge filter, compartment filter, paper roll filter, centrifugal discharge leaf, repal leaf, piston press, plate press, screw press, Schneider filter, pressurized scraper discharge filter, bag filter, candle filter, Druck filter, baking Pressurized filtration equipment such as filter media; vacuum Nutsche, drum filter, Young filter, Dix filter, horizontal filter, horizontal belt filter, Nutsche filter, leaf filter, candle plate disk, rotary disk filter, rotary drum filter, belt filter , table filter, pan filter, internal feed type drum filter, sintered filter media filter, etc. Compression type filtration equipment such as belt press, screw press, tube press, Mars press, etc. Ring type magnetic separator, cylinder type magnetic filtration devices such as magnetic separators; electrostatic filtration devices such as rotary electrostatic separators;
A filtration device used for filtration separation is equipped with a filtration layer that collects solids and allows liquid to pass through. In the present application, the filtration layer is referred to as a filter medium.

Apparatus that can be used in the method of sedimenting compound (2) for solid-liquid separation and collecting the supernatant is not particularly limited as long as it is a generally used apparatus. machine, table machine, continuous sedimentation tank, batch sedimentation tank, tank with plate, sedimentation flotation tank, inclined classifier, spiral classifier, sedimentation cone, filter, thickener, scroll, scroll disc, gravitroll, disc batch, cylindrical bowl , concentric circular bowls, drum settlers, hydrocyclones, centers and the like.

In filtration separation, a filter aid can be used as needed. By using a filter aid, it is possible to improve the removal efficiency of compound (2) (reduce the residual amount and shorten the filtration time).

The filter aid is not particularly limited as long as it is a commonly used filter aid, but examples include diatomaceous earth (for example, radiolite manufactured by Showa Chemical Industry Co., Ltd., celite manufactured by Imerys, etc.), perlite ( Examples include Topco manufactured by Showa Chemical Industry Co., Ltd., Locahelp manufactured by Mitsui Kinzoku Mining Co., Ltd.), powdered cellulose (eg, KC Flock manufactured by Nippon Paper Industries Co., Ltd., Roca Ace Silky Aid manufactured by Musashino Chemical Research Institute, etc.), and the like. . Moreover, any of dried products, baked products, and flux-baked products can be used. Among these, in addition to the excellent removal efficiency of compound (2), it is easy to obtain, and the economy of the process of purifying the sulfonic acid group-containing monomer tends to improve, so diatomaceous earth and / or Perlite is preferred, and diatomaceous earth is more preferred.
The filter aid may be used singly or in combination.

The permeability (Darcy) of the filter aid is not particularly limited as long as it is within the range of generally used permeability (Darcy), but is preferably 0.01 to 30. Since the residual amount of compound (2) tends to be small and the filtration time tends to be short, it is preferably 0.03 or more, more preferably 0.05 or more. Since the filtration time of compound (2) tends to be short and the residual amount tends to be small, it is preferably 22 or less, more preferably 2 or less, and even more preferably 0.25 or less.

The amount of the filter aid used is not particularly limited as long as it is a commonly used amount. is preferably 0.1 to 100. Since the residual amount of compound (2) tends to be smaller and the filtration time tends to be shorter, θ/η is preferably 0.5 or more, more preferably 0.8 or more. , is more preferably 1 or more. Since the filtration time of compound (2) tends to be short, θ/η is preferably 50 or less, more preferably 30 or less. From the same point of view and the amount of filter aid used is reduced, and the economy tends to improve when producing compound (4), it is more preferably 20 or less, and 10 or less. Especially preferred.

In addition, the used amount of the filter aid here is the total mass of the filter aid used for filtration separation. For example, when the pre-coating method and the body-feeding method are used together, it is the total mass of the filter aid used in the two methods. In addition, when the filter aid layer formed by filtration separation is partially removed and the remaining filter aid layer is reused, the total mass of the supplied filter aid and the remaining filter aid layer is be.

The method of using the filter aid is not particularly limited as long as it is a commonly used method. A body-feed method, in which a filter aid is added to the liquid to be filtered, and the like. These may be used singly or in combination. Clogging of the filter medium tends to be suppressed, clogging of the surface of the filter aid layer tends to be suppressed, and the period of operation on an industrial scale tends to be extended. is preferably used in combination.

The filter medium used for filtration separation is not particularly limited as long as it is a generally used filter medium, and examples thereof include filter cloth, metal filters, metal sintered filters, and metal fiber/powder laminate types. These may be used singly or in combination. When a filter cloth is used, it can be used in combination with a filter medium such as a metal filter that supports the filter cloth in order to improve the strength of the filter cloth.

The material of the filter cloth is not particularly limited as long as it is generally used, and examples thereof include polypropylene, polyester, polyamide, vinylidene chloride, polyvinyl alcohol, polytetrafluoroethylene, modacrylic, and cotton. Polypropylene, polyester, and polyamide are preferred, and polypropylene and polyester are more preferred, because they are readily available and tend to improve the economic efficiency of the step of purifying the sulfonic acid group-containing monomer. Vinylidene chloride and polytetrafluoroethylene are preferable, and polytetrafluoroethylene is more preferable, when the durability of the filter cloth is required depending on the properties of the liquid to be filtered.

The material of the metal filter medium is not particularly limited as long as it is commonly used, but iron, carbon steel, stainless steel, alloys of nickel with molybdenum, chromium, iron, etc. (for example, Hastelloy (trade name) , Inconel (trade name), etc.), nickel, titanium, and the like. Iron, carbon steel, and stainless steel are preferable because they are readily available and tend to improve the economic efficiency of the process of refining the sulfonic acid group-containing monomer. Stainless steel is more preferred. If the properties of the liquid to be filtered require the durability of the metal filter medium, an alloy of nickel with molybdenum, chromium, iron, etc., or nickel is preferable. An alloy obtained by adding molybdenum, chromium, iron, etc. to nickel is more preferable.

The air permeability of the filter medium is not particularly limited as long as it is within a general range, but it is preferably 0.01 to 200 cm ³ /cm ² ·s. Since the filtration time of compound (2) tends to be short, it is preferably 0.05 cm ³ /cm ² ·s or more, more preferably 0.1 cm ³ /cm ² ·s or more. The residual amount of compound (2) tends to be smaller, and when a filter aid is used, the permeation amount of the filter aid tends to be smaller, so it should be 100 cm ³ /cm ² s or less is preferably 50 cm ³ /cm ² ·s or less, and even more preferably 20 cm ³ /cm ² ·s or less.

The temperature at the time of filtration separation is not particularly limited as long as it is within a general temperature range, but it is preferably 0 to 120°C. Since the viscosity of the filtrate tends to decrease, the filtration time tends to be shortened, and precipitation of substances other than compound (2) can be suppressed in some cases, the temperature for filtration separation is preferably 10 ° C. or higher. It is more preferably 20°C or higher. The temperature is preferably 100°C or lower, more preferably 80°C or lower, because the amount of volatile components generated from the liquid to be filtered tends to decrease, and the change in the state of the precipitate tends to be suppressed. Since the amount of compound (2) dissolved in the dissolved compound tends to be reduced and the residual amount of compound (2) tends to be smaller, it is more preferably 70° C. or lower, particularly 60° C. or lower. preferable.
The temperature during the filtration separation may be constant or may be changed.

The pressure on the side through which the liquid to be filtered across the filter media permeates (hereinafter referred to as "downstream pressure") is higher than the pressure on the side supplying the liquid to be filtered across the filter media (hereinafter referred to as "upstream pressure"). is low, the compound (2) can be collected on the side of the filter medium that supplies the liquid to be filtered, and the filtrate can be recovered on the side of the filter medium that is permeated by the liquid to be filtered.

The upstream pressure and downstream pressure at the time of filtration are the pressure states described above, and are not particularly limited as long as they are generally used pressures, and may be constant or variable.

When the filtration method is gravity filtration, the pressure on the upstream side is normal pressure, and the pressure generated by the weight of the liquid to be filtered enables filtration and separation.

When the filtration method is pressurized filtration, filtration separation can be performed by increasing the pressure on the upstream side. The upstream pressure in pressurized filtration is not particularly limited as long as it is a commonly used pressure, but is preferably 0.01 to 2.0 MPaG. Since the filtration time of compound (2) tends to be short, it is more preferably 0.05 MPaG or more, further preferably 0.1 MPaG or more. Even if the pressure resistance of the filtration device is low, it is possible to perform industrial filtration, and the general availability of filtration devices tends to be easy. It is more preferably 6 MPaG or less, and particularly preferably 0.4 MPaG or less. The downstream pressure in pressurized filtration is usually normal pressure, but can be reduced if the filtering time of compound (2) is desired to be shortened.
The upstream pressure and downstream pressure in pressurized filtration may be constant or variable.

The downstream pressure in decompression filtration is not particularly limited as long as it is a commonly used pressure, but is normal pressure or lower. Since the filtration time of compound (2) tends to be short, it is preferably 0.08 MPaA or less, more preferably 0.06 MPaA or less, and even more preferably 0.04 MPaA or less. The lower limit of the downstream pressure in decompression filtration is not particularly limited, and varies depending on the capacity of the pump for decompression and the airtightness of the filtration device, etc., but the size of the pump for decompression tends to be reduced. Because there is a tendency to suppress the complexity of the structure of the filtration device in order to increase the airtightness of the filtration device, it is preferably 0.1 kPaA or more, and more preferably 1 kPaA or more. It is preferably 2 kPaA or more, and more preferably 2 kPaA or more.
The downstream pressure in vacuum filtration may be constant or variable.

The centrifugal force for centrifugal filtration is not particularly limited as long as it is within the range of the generally used centrifugal force, but it is preferably 100 to 10000G. Since the filtration time of compound (2) tends to be short, it is more preferably 500 G or more, and even more preferably 1000 G or more. Since the structure of the centrifugal filter tends to be suppressed from becoming complicated, it is more preferably 8000 G or less, and even more preferably 7000 G or less.
The centrifugal force during centrifugal filtration may be constant or variable.

The supply amount of the liquid to be filtered is not particularly limited as long as it is within the general supply amount range, but is preferably 10 to 10000 kg/m ² ·hr. Since the amount of compound (4) recovered per hour is improved, and the economy of purification of compound (4) tends to be improved, it is more preferably 50 kg/m ² ·hr or more, and 80 kg / More preferably, it is m ² ·hr or more. When the amount of liquid to be filtered is large, it is necessary to increase the amount of liquid that permeates the filter medium. Therefore, it is necessary to lower the resistance of the filter medium and the filter aid, and it is necessary to increase the air permeability of the filter medium and the air permeability of the filter aid. As a result, the amount of residual compound (2) increases. From the above, since the residual amount of compound (2) tends to be reduced, it is more preferably 5000 kg/m ² ·hr or less, further preferably 1000 kg/m ² ·hr or less.
The amount of liquid to be filtered may be constant or variable.

The atmosphere for filtering is not particularly limited as long as it is an atmosphere that is normally used, and an air atmosphere, a nitrogen atmosphere, an argon atmosphere, or the like is usually used. Among these, a nitrogen atmosphere and an argon atmosphere are preferable because they tend to produce the compound (4) more safely. A nitrogen atmosphere is more preferable because it tends to be a more economical manufacturing method.
The atmosphere to be filtered may be used singly or in combination of a plurality of atmospheres.

A mixture containing compound (2) recovered by filtering the fluorine-containing sulfonate solution (hereinafter referred to as "filtrate") is subjected to a reaction to produce compound (3) from compound (1) and compound (2). can be reused for The filter cake may be used as it is, or the dissolved compound may be dried by vacuum drying or the like before use. Further, when reused in the reaction for producing compound (3) from compound (1) and compound (2), in the reaction for producing compound (3) from compound (1) and compound (2), The unused compound (2) may be mixed with filter cake or dried filter cake and used.

A method of obtaining compound (4) by filtering the fluorine-containing sulfonate solution and separating the dissolved compound from the collected solution containing compound (4) (hereinafter referred to as "fluorine-containing sulfonate-containing filtrate"). is not particularly limited as long as it is a generally used method. For example, under normal pressure or reduced pressure, normal temperature or under heating conditions, the dissolved compound is distilled off, and compound (4) is obtained. A method of separation can be mentioned. The temperature for heating to a temperature exceeding room temperature is not particularly limited as long as it is within a range generally used, but since deterioration of compound (4) tends to be suppressed, it is preferably 250° C. or less. , more preferably 200° C. or lower, more preferably 150° C. or lower, and particularly preferably 120° C. or lower.
The temperature during the heating may be constant or may be changed during the heating.

When the dissolved compound is distilled off and the compound (4) is separated, the lower limit of the pressure when the pressure is reduced to a pressure lower than the normal pressure is not particularly limited, and the ability of the pump for reducing the pressure, the airtightness of the device used, etc. Although it varies depending on the Therefore, it is preferably 0.1 kPaA or more, more preferably 1 kPaA or more, and more preferably 2 kPaA or more.
The pressure of the reduced pressure may be constant or variable.

The atmosphere in which the dissolved compound is distilled off and the compound (4) is separated is not particularly limited as long as it is an ordinary atmosphere, and an air atmosphere, a nitrogen atmosphere, an argon atmosphere, or the like is usually used. Among these, a nitrogen atmosphere and an argon atmosphere are preferable because they tend to produce the compound (4) more safely. A nitrogen atmosphere is more preferable because it tends to be a more economical manufacturing method. When the dissolved compounds are removed by distillation, circulating the atmosphere tends to facilitate the removal of the dissolved compounds by distillation, and is sometimes used as a preferred method.
As the atmosphere for distilling off the dissolved compound and separating the compound (4), one atmosphere may be used alone, or a plurality of atmospheres may be used in combination.

The device used for separating the dissolved compound from the fluorine-containing sulfonate-containing filtrate is not particularly limited as long as it is a generally used device. Dryers, vibration dryers, tray dryers, double cone dryers, belt dryers, rotary evaporators and the like can be mentioned. More specific examples include ribocone, inner tube rotary, sludge dryer, super rotary dryer, FV dryer, horizontal fluidized bed dryer, slit flow, conduction flow, slurry dryer, funnel through, custom dryer, eco dryer. , groovy dryer and H-VCD dryer (manufactured by Okawara Seisakusho Co., Ltd.), PV Mixer, SV Mixer, conical dryer and rotary filter dryer (manufactured by Kobelco Eco-Solutions Co., Ltd.), vacuum stirring dryer, vibrating fluidized bed device , vibration dryer, drum dryer, shelf vacuum dryer, double cone dryer (manufactured by Chuo Kakoki Co., Ltd.), paddle dryer, Buno cooler, single paddle dryer, multi-fin processor, continuous fluidized bed dryer, batch type fluidization Dryer, Tornesh dryer, medium fluidized dryer, tower dryer, flash dryer (manufactured by Nara Machinery Co., Ltd.), CD dryer, M-CD dryer, KID dryer, steam tube dryer, airflow drying system, fluidization Layer dryer, band dryer, rotor louver dryer, rotary dryer, flash dryer, SC processor, rotary kiln (manufactured by Kurimoto, Ltd.), band dryer, hot air box dryer, fluidized bed dryer, vibration fluidized bed dryer dryer, flash dryer, rotary crusher dryer, conical blender dryer, drum dryer, jacket rotary dryer, vacuum tray dryer, vacuum vibration dryer, and stirring dryer (manufactured by Nippon Dryer Co., Ltd.), drum dryer, vacuum type A drum dryer, a vacuum stirring dryer, a double cone dryer (manufactured by Katsuragi Industry Co., Ltd.), a high evaporator (manufactured by Sakura Seisakusho Co., Ltd.), and a vertical stirring dryer (manufactured by Salient Industry Co., Ltd.) can be mentioned.
These devices may be used singly or in combination.

Compound (4) separated from compound (2) as described above can be reused as a raw material for compound (1) according to the method described in WO2020/012913.

Dissolved compounds obtained by distilling off the dissolved compounds and separating compound (4) (for example, volatile components containing dissolved compounds) are mixed with the reaction residue and dissolved compounds to prepare a fluorine-containing sulfonate solution. can be reused in the process of When reused, the dissolved compound may be distilled off and the dissolved compound obtained when separating the compound (4) may be mixed with the unused dissolved compound.

The compound ( 4) (hereinafter referred to as "aqueous solution containing fluorine-containing sulfonate") can be prepared. When water is added to the fluorine-containing sulfonate-containing filtrate, water may be added once to distill off dissolved compounds to prepare an aqueous solution containing fluorine-containing sulfonate. The removal may be repeated several times to prepare the fluorine-containing sulfonate-containing aqueous solution. A method of repeating the addition and distillation of water multiple times is more preferable because it tends to reduce the total mass of water used when reducing the dissolved compounds contained in the fluorine-containing sulfonate-containing aqueous solution. When adding the fluorine-containing sulfonate-containing filtrate to water, after adding the fluorine-containing sulfonate-containing filtrate to water at once, the dissolved compounds are distilled off, and then water is further added as necessary. This is a preferred method because the total mass of water to be used tends to be reduced by distilling off.

The ratio (κ/ι) between the mass (ι) of the fluorine-containing sulfonate-containing filtrate and the total mass (κ) of the water used for preparing the fluorine-containing sulfonic acid aqueous solution is within a generally used range. Although there is no particular limitation as long as It is more preferably 1.0 or more, and particularly preferably 1.2 or more. Although the upper limit of κ/ι is not particularly limited depending on the desired concentration of compound (4) in the aqueous fluorine-containing sulfonic acid solution, the total mass of the fluorine-containing sulfonate-containing filtrate and water becomes small, and the dissolved compound is distilled. Since it tends to take less time to remove, it is preferably 100 or less, more preferably 50 or less, even more preferably 25 or less, and particularly preferably 10 or less. When the concentration of compound (4) in the desired fluorine-containing sulfonic acid aqueous solution is low, the dissolved compound is distilled off at a ratio where κ/ι is small, and water is added to obtain the desired fluorine-containing sulfonic acid aqueous solution. When the concentration of compound (4) is adjusted to , the volume of the device used for distillation tends to be smaller, and the heat source used and the energy required to drive the decompression pump when depressurizing is more preferable because it tends to be reduced.

The temperature at which water is added to the fluorine-containing sulfonate-containing filtrate, the temperature at which the fluorine-containing sulfonate-containing filtrate is added to water, and the temperature at which water is further added after distilling off the dissolved compounds are generally Although the temperature is not particularly limited as long as it is generally used, it is preferably −40° C. or higher, more preferably −20° C. or higher, because it tends to suppress the precipitation of compound (4). From the same point of view and because there is a tendency to be excellent in economic efficiency when adjusting the temperature on an industrial scale, the temperature is more preferably 0° C. or higher, and particularly preferably 10° C. or higher. The upper limits of the temperature at which water is added to the fluorine-containing sulfonate-containing filtrate, the temperature at which the fluorine-containing sulfonate-containing filtrate is added to water, and the temperature at which water is further added after distilling off the dissolved compounds are , Although not particularly limited, since volatilization may occur depending on the type of water and dissolved compounds, volatilization can be suppressed and precipitation of compound (4) tends to be suppressed. It is preferably 100° C. or lower, more preferably 80° C. or lower, and particularly preferably 60° C. or lower.
The temperature at which water is added to the fluorine-containing sulfonate-containing filtrate, the temperature at which the fluorine-containing sulfonate-containing filtrate is added to water, and the temperature at which water is further added after distilling off the dissolved compounds are kept constant. However, it may be changed in the middle.

The pressure at which water is added to the fluorine-containing sulfonate-containing filtrate, the pressure at which the fluorine-containing sulfonate-containing filtrate is added to water, and the pressure at which water is added after distilling off the dissolved compounds. The pressure is not particularly limited as long as it is within the range normally used, and the reaction is usually carried out under atmospheric pressure. However, since some dissolved compounds may volatilize, it is an effective means to apply pressure higher than the atmospheric pressure in order to suppress volatilization. When the volatilizing compound is liquefied and reused, the pressure may be reduced to atmospheric pressure or less.
The pressure at which water is added to the fluorine-containing sulfonate-containing filtrate, the pressure at which the fluorine-containing sulfonate-containing filtrate is added to water, and the pressure at which water is added after distilling off the dissolved compounds. The pressure may be constant, or may be changed within the above range.

The atmosphere in which water is added to the fluorine-containing sulfonate-containing filtrate, the atmosphere in which the fluorine-containing sulfonate-containing filtrate is added to water, and the atmosphere in which water is added after distilling off the dissolved compounds. The atmosphere is not particularly limited as long as it is an ordinary atmosphere, and an air atmosphere, a nitrogen atmosphere, an argon atmosphere, or the like is usually used. Among these, a nitrogen atmosphere and an argon atmosphere are preferable because they tend to produce the compound (4) more safely. A nitrogen atmosphere is more preferable because it tends to be a more economical manufacturing method.
The atmosphere in which water is added to the fluorine-containing sulfonate-containing filtrate, the atmosphere in which the fluorine-containing sulfonate-containing filtrate is added to water, and the atmosphere in which water is added after distilling off the dissolved compounds. One type of atmosphere may be used alone, or a plurality of types of atmospheres may be used in combination.

The temperature at which the dissolved compound is distilled off from the mixture of the filtrate containing the fluorine-containing sulfonate and water is not particularly limited as long as it is a temperature generally used. The temperature is preferably 0° C. or higher, more preferably 20° C. or higher, and further preferably 30° C. or higher. It is preferably 40° C. or higher, and particularly preferably 40° C. or higher. The upper limit of the temperature at which the dissolved compound is distilled off from the mixture of the filtrate containing the fluorine-containing sulfonate and water is not particularly limited, but since the deterioration of the compound (4) tends to be suppressed, it is 250° C. or less. is preferably 200° C. or lower, more preferably 150° C. or lower, and particularly preferably 120° C. or lower.
The temperature at which the dissolved compound is distilled off from the mixture of the filtrate containing the fluorine-containing sulfonate and water may be constant or may be changed during the process.

The pressure at which the dissolved compound is distilled off from the mixture of the filtrate containing the fluorine-containing sulfonate and water is not particularly limited as long as it is within the range normally used, and any pressure, normal pressure, or reduced pressure may be used. Although it is good, it is usually carried out under normal pressure and reduced pressure. When the dissolved compound is distilled off under reduced pressure, the temperature during the distillation can be lower than when distilled off at normal pressure, and depending on the type of compound (4), deterioration of compound (4) tends to be suppressed. It is therefore the preferred method. Distilling off the dissolved compounds at normal pressure is a preferred method because it eliminates the energy required to drive the device used to achieve the desired pressure.
The pressure at which the dissolved compound is distilled off from the mixture of the filtrate containing fluorine-containing sulfonate and water may be constant, or may be changed during the process as long as it is within the above range.

The atmosphere in which the dissolved compound is distilled off from the mixture of the filtrate containing the fluorine-containing sulfonate and water is not particularly limited as long as it is an atmosphere that is normally used, and is usually an air atmosphere, a nitrogen atmosphere, an argon atmosphere, or the like. is used. Among these, a nitrogen atmosphere and an argon atmosphere are preferable because they tend to produce the compound (4) more safely. A nitrogen atmosphere is more preferable because it tends to be a more economical manufacturing method.
The atmosphere for distilling off the dissolved compound from the mixture of the fluorine-containing sulfonate-containing filtrate and water may be used singly or in combination of a plurality of atmospheres.

The fluorine-containing sulfonic acid aqueous solution obtained as described above can be reused as a raw material for compound (1) according to the method described in WO2020/012913.

The dissolved compound obtained by distilling off the dissolved compound from the mixture of the fluorine-containing sulfonate-containing filtrate and water is completely or partially removed from the reaction residue and the dissolved compound to prepare a fluorine-containing sulfonate solution. can be reused when

From the mixture of the filtrate containing the fluorine-containing sulfonate and water, the dissolved compound obtained by distilling off the dissolved compound contains a large amount of water, and the compound (2) contained in the reaction residue is converted into a fluorine-containing sulfonate solution of the compound (2). If the amount of dissolved compound is large, the method of separating the dissolved compound and water by distillation, or depending on the type of dissolved compound, phase separation between the dissolved compound and water may occur. By using a method of separating, a method of distilling off the dissolved compound phase and separating the dissolved compound with an increased content, or a method of distilling off the water phase and separating the water with an increased content, Dissolved compounds and water can be obtained. All or part of the dissolved compound obtained by the above method can be reused in preparing a fluorine-containing sulfonate solution from the reaction residue and the dissolved compound. Moreover, all or part of the water obtained by the above method can be reused when preparing the fluorine-containing sulfonate-containing aqueous solution.

As described above, the present invention provides a fluorine-containing vinyl sulfonic acid fluoride (3 ) can be produced in high yield. In addition, a fluorine-containing vinyl sulfonate (4) that can be converted into various fluorine compounds can be produced. Furthermore, the fluorine-containing vinylsulfonic acid fluoride (3) and the fluorine-containing vinylsulfonate (4) can be separated, and the compounds used for the separation can be reused.

Examples that specifically describe the present embodiment will be exemplified below. The present invention is not limited to the following examples as long as the gist thereof is not exceeded.

The analysis methods used in Examples and Comparative Examples are as follows.

<Nuclear Magnetic Resonance Analysis (NMR): Molecular Structural Analysis by ¹⁹ F-NMR>
The products obtained in Examples and Comparative Examples were subjected to molecular structure analysis using ¹⁹ F-NMR under the following measurement conditions.
[Measurement condition]
Measuring device: JNM-ECZ400S type nuclear magnetic resonance device (manufactured by JEOL Ltd.)
Observation nucleus: ¹⁹ F
Solvent: heavy chloroform Reference substance: tetramethylsilane (0.00 ppm)
Observation frequency: 400MHz ( ¹ H)
Pulse width: 6.5 μs Waiting time: 2 seconds Accumulation times: 16 times

<Nuclear Magnetic Resonance Analysis (NMR): Molecular Structural Analysis by ¹ H-NMR>
The products obtained in Examples and Comparative Examples were subjected to molecular structure analysis using ¹ H-NMR under the following measurement conditions.
[Measurement condition]
Measuring device: JNM-ECZ400S type nuclear magnetic resonance device (manufactured by JEOL Ltd.)
Observation nucleus: ¹ H
Solvent: heavy chloroform Reference substance: tetramethylsilane (0.00 ppm)
Observation frequency: 400MHz ( ¹ H)
Pulse width: 7.3 μs Waiting time: 5 seconds Accumulation times: 8 times

<Gas Chromatography (GC)>
The products obtained in Examples were subjected to molecular structure analysis using GC under the following measurement conditions.
[Measurement condition]
Measuring device: GC-2010Plus
Column: US RESTEK capillary column RTX-200 (inner diameter 0.25 mm, length 60 m, film thickness 1 μm)
Carrier gas: Helium Carrier gas flow rate: 30 mL/min
Injection volume: 1 μL
Split ratio: 30
Vaporization chamber temperature: 200°C
Column temperature program: After holding at 40°C for 10 minutes, after raising the temperature at 20°C/min, holding at 280°C for 10 minutes Detection: FID, 200°C

Raw materials used in Examples and Comparative Examples are shown below.

[Production Example 1]
(Fluorine-containing vinyl sulfonic anhydride (1) (compound (1))
A compound (7) represented by the following formula (7) was produced according to JP-A-2019/156782.
CF2 _{= CFOCF2CF2SO3Na ( 7} )
Using the obtained compound of formula (7), compound (8) represented by formula (8) below was produced according to International Publication No. 2020/012913.
(CF2 _{= CFOCF2CF2SO2} ) _{2O ( 8} )
By distilling the obtained compound (8), a purified mixed compound (8) was obtained. The obtained mixed compound (8) had a purity of 98% by mass and contained 2% by mass of the compound (9) represented by the following formula (9).
CF2 _{= CFOCF2CF2SO3H ( 9} )

(Alkali metal fluoride (2) (compound (2))
・Potassium fluoride (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd., special reagent grade)
・ Rubidium fluoride (manufactured by Aldrich, purity 99.8%)
・Cesium fluoride (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd., special reagent grade)

(others)
・ Ethanol (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd., reagent grade)
・Hexafluorobenzene (manufactured by Tokyo Chemical Industry Co., Ltd.)
・Benzotrifluoride (manufactured by Tokyo Chemical Industry Co., Ltd.)
・Purified water (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.)
・ 2,2,2-trifluoroethanol (manufactured by Tokyo Chemical Industry Co., Ltd.)
・ Acetonitrile (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd., reagent grade)
・Butyl acetate (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd., reagent special grade)
・ 4-methyl-2-pentanone (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd., reagent special grade)
・ Dimethyl carbonate (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd., reagent grade)
・ 1,2-dimethoxyethane (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd., Wako special grade)
Aqueous sodium hydrogen carbonate solution: Prepared by mixing 18.0 g of sodium hydrogen carbonate (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd., special reagent grade) and 182.0 g of purified water.

[Example 1]
In a space of a nitrogen atmosphere, 349.8 g of the mixed compound (8) produced in Production Example 1 (342.8 g (0.637 mol) of compound (8) and 7.00 g (0.025 mol) of compound (9) ) was placed in a flask and fitted with a half-moon stirrer and a Liebig condenser with a receiver. Furthermore, a concentration flask containing potassium fluoride dried at 150° C. for 5 hours under vacuum was attached to the flask through an airless feedcock (manufactured by Asahi Seisakusho Co., Ltd.). Remove the flask from the space of the nitrogen atmosphere, attach the three-one motor (manufactured by Shinto Kagaku Co., Ltd., BLW300), circulate the -5 ° C. refrigerant in the Liebig condenser, and dry ice the receiver attached to the Liebig condenser. Chilled with chilled ethanol. A pipe made of Teflon (registered trademark) was installed so as to equalize the pressure between the concentrating flasks. The flask was placed in an oil bath (OHB-3100S, manufactured by Tokyo Rikakikai Co., Ltd.) set at 110° C., the pressure was reduced to 70 kPaA, and the mixture was stirred at 120 rpm for 10 minutes. Potassium fluoride was gradually introduced into the flask by operating the cock of the airless feed cock. It took 44 minutes to finish putting the potassium fluoride into the flask. After the reaction was completed, it was found that 58.1 g (1.00 mol) of potassium fluoride had been added by measuring the mass of the concentration flask with an airless feed cock before and after the addition. When the potassium fluoride was added, the liquid started to distill gradually, and when the speed of the liquid distilling into the receiver reached 2 drops/minute, the pressure was gradually lowered to 2 kPaA. The reaction was judged to be completed when no more liquid was distilled out into the receiver for 2 minutes or more, and the flask was removed from the oil bath to create a nitrogen atmosphere. The refrigerant flowing through the Liebig condenser was stopped, the receiver was returned to room temperature, and the mass of the fraction contained in the receiver was measured to be 176.5 g. For analysis, a fraction (0.30 g), hexafluorobenzene (1.30 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, fluorine-containing vinyl sulfonic acid fluoride (10) represented by the following general formula (10) was produced (amount of product: 170.5 g, amount of product: 0.609 mol, production rate: 95.6 %). In the analysis, from the mass of benzotrifluoride, the integrated value of _CF3 of benzotrifluoride and CF2 of fluorine _- containing vinylsulfonic acid fluoride (10), the production amount of fluorine-containing vinylsulfonic acid fluoride (10), etc., was determined. Calculated. The production rate of fluorine-containing vinyl sulfonic acid fluoride (10) was calculated by the following formula (1).
Production rate (%) of fluorine-containing vinyl sulfonic acid fluoride (10) = amount of substance of fluorine-containing vinyl sulfonic acid fluoride (10) / amount of substance of compound (8) × 100 (1)
For example, the production rate (%) of fluorine-containing vinyl sulfonic acid fluoride (10) in this example = 0.609 (mol)/0.637 (mol) x 100 = 95.6.
In this example, β/α was 1.6.
CF2 _{= CFOCF2CF2SO2F ( 10} )
¹⁹ F-NMR: δ (ppm) 42.43 (1F), -86.34 (2F), -114.21 (2F), -116.58 (1F), -123.87 (1F), -138 .96 (1F)
Also, the residue remaining in the flask was collected and the mass was measured to be 222.1 g. For analysis, the residue (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, it was also confirmed that a fluorine-containing vinyl sulfonate (11) represented by the following general formula (11) was produced (amount of product: 202.3 g, amount of product: 0.640 mol). In the analysis, from the mass of 2,2,2-trifluoroethanol, the integrated value of CF ₃ of 2,2,2-trifluoroethanol and CF ₂ of fluorine-containing vinyl sulfonate (11), fluorine-containing The amount of vinyl sulfonate (11) produced and the like were calculated.
CF2 _{= CFOCF2CF2SO3K ( 11} )
¹⁹ F-NMR: δ (ppm) -84.83 (2F), -113.83 (1F), -118.30 (2F), -122.05 (1F), -135.70 (1F)
In this example, the rate at which compound (2) was added to the flask (hereinafter referred to as "addition rate") was 1.3 g/min. The addition rate is 58.1 (g)/44 (min) = 1.3 (g/ min). Similar calculations were performed in the following examples.
In this example, the ratio of the rate of adding compound (2) to the flask with respect to the mass of compound (8) produced in Production Example 1 (hereinafter referred to as "mass ratio addition rate") was 0.23 g/ min/g. The mass-specific addition rate is the mass of compound (2) (58.1 g), the time required to add compound (2) (44 min), and the mass of compound (8) produced in Production Example 1 (349.8 g). , 58.1 (g)/44 (min)/349.8 (g) = 0.23 (g/min/g). Similar calculations were performed in the following examples.

[Example 2]
In a space of a nitrogen atmosphere, 250.1 g of the mixed compound (8) produced in Production Example 1 (245.1 g (0.455 mol) of compound (8) and 5.00 g (0.018 mol) of compound (9) ) was placed in a flask and fitted with a half-moon stirrer and a Liebig condenser with a receiver. Furthermore, a concentration flask containing potassium fluoride dried at 150° C. for 5 hours under vacuum was attached to the flask through an airless feedcock (manufactured by Asahi Seisakusho Co., Ltd.). Remove the flask from the space of the nitrogen atmosphere, attach the three-one motor (manufactured by Shinto Kagaku Co., Ltd., BLW300), circulate the -5 ° C. refrigerant in the Liebig condenser, and dry ice the receiver attached to the Liebig condenser. Chilled with chilled ethanol. A pipe made of Teflon (registered trademark) was installed so as to equalize the pressure between the concentrating flasks. The flask was placed in an oil bath (OHB-3100S, manufactured by Tokyo Rikakikai Co., Ltd.) set at 130° C., the pressure was reduced to 80 kPaA, and the mixture was stirred at 120 rpm for 10 minutes. Potassium fluoride was gradually introduced into the flask by operating the cock of the airless feed cock. It took 23 minutes to finish putting potassium fluoride into the flask. After the reaction was completed, it was found that 45.5 g (0.784 mol) of potassium fluoride had been added by measuring the mass of the concentration flask with an airless feed cock before and after the addition. When the potassium fluoride was added, the liquid started to distill gradually, and when the speed of the liquid distilling into the receiver reached 2 drops/minute, the pressure was gradually lowered to 2 kPaA. The reaction was judged to be completed when no more liquid was distilled out into the receiver for 2 minutes or more, and the flask was removed from the oil bath to create a nitrogen atmosphere. The refrigerant flowing through the Liebig condenser was stopped, the receiver was returned to room temperature, and the mass of the fraction contained in the receiver was measured to be 127.4 g. For analysis, a fraction (0.30 g), hexafluorobenzene (1.30 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, fluorine-containing vinylsulfonic acid fluoride (10) was produced (amount of product: 116.4 g, amount of product: 0.416 mol, production rate: 91.3%).
In this example, β/α was 1.7.
Also, the residue remaining in the flask was recovered and the mass was measured to be 162.5 g. For analysis, the residue (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of the analysis, it was also confirmed that a fluorine-containing vinyl sulfonate (11) represented by the following general formula (11) was produced (amount of product: 143.9 g, amount of product: 0.455 mol).
In this example, the addition rate was 2.0 g/min and the mass specific addition rate was 0.48 g/min/g.

[Example 3]
In a space of a nitrogen atmosphere, 100.2 g of the mixed compound (8) produced in Production Example 1 (98.2 g (0.182 mol) of compound (8) and 2.00 g (0.007 mol) of compound (9) ) was placed in a flask and fitted with a half-moon stirrer and a Liebig condenser with a receiver. Furthermore, a concentration flask containing potassium fluoride dried at 150° C. for 5 hours under vacuum was attached to the flask through an airless feedcock (manufactured by Asahi Seisakusho Co., Ltd.). Remove the flask from the space of the nitrogen atmosphere, attach the three-one motor (manufactured by Shinto Kagaku Co., Ltd., BLW300), circulate the -5 ° C. refrigerant in the Liebig condenser, and dry ice the receiver attached to the Liebig condenser. Chilled with chilled ethanol. A pipe made of Teflon (registered trademark) was installed so as to equalize the pressure between the concentrating flasks. The flask was placed in an oil bath (OHB-3100S, manufactured by Tokyo Rikakikai Co., Ltd.) set at 150° C., the pressure was reduced to 90 kPaA, and the mixture was stirred at 120 rpm for 10 minutes. Potassium fluoride was gradually introduced into the flask by operating the cock of the airless feed cock. It took 5 minutes to finish putting potassium fluoride into the flask. After the reaction was completed, it was found that 19.8 g (0.341 mol) of potassium fluoride had been added by measuring the mass of the concentration flask with an airless feed cock before and after the addition. When the potassium fluoride was added, the liquid started to distill gradually, and when the speed of the liquid distilling into the receiver reached 2 drops/minute, the pressure was gradually lowered to 2 kPaA. The reaction was judged to be completed when no more liquid was distilled out into the receiver for 2 minutes or more, and the flask was removed from the oil bath to create a nitrogen atmosphere. The refrigerant flowing through the Liebig condenser was stopped, the receiver was returned to room temperature, and the mass of the fraction contained in the receiver was measured to be 51.5 g. For analysis, a fraction (0.30 g), hexafluorobenzene (1.30 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, fluorine-containing vinylsulfonic acid fluoride (10) was produced (amount of product: 44.3 g, amount of product: 0.158 mol, production rate: 86.6%).
In this example, β/α was 1.9.
Also, the residue remaining in the flask was recovered and the mass was measured to be 66.8 g. For analysis, the residue (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, it was also confirmed that a fluorine-containing vinyl sulfonate (11) represented by the following general formula (11) was produced (amount of product: 57.6 g, amount of product: 0.182 mol).
In this example, the addition rate was 4.0 g/min and the mass specific addition rate was 2.4 g/min/g.

[Example 4]
In a space of a nitrogen atmosphere, 200.1 g of the mixed compound (8) produced in Production Example 1 (196.1 g (0.364 mol) of compound (8) and 4.00 g (0.014 mol) of compound (9) ) was placed in a flask and fitted with a half-moon stirrer and a Liebig condenser with a receiver. Furthermore, a concentration flask containing potassium fluoride dried at 150° C. for 5 hours under vacuum was attached to the flask through an airless feedcock (manufactured by Asahi Seisakusho Co., Ltd.). Remove the flask from the space of the nitrogen atmosphere, attach the three-one motor (manufactured by Shinto Kagaku Co., Ltd., BLW300), circulate the -5 ° C. refrigerant in the Liebig condenser, and dry ice the receiver attached to the Liebig condenser. Chilled with chilled ethanol. A pipe made of Teflon (registered trademark) was installed so as to equalize the pressure between the concentrating flasks. The flask was placed in an oil bath (OHB-3100S manufactured by Tokyo Rikakikai Co., Ltd.) set at 90° C., the pressure was reduced to 60 kPaA, and the mixture was stirred at 120 rpm for 10 minutes. Potassium fluoride was gradually introduced into the flask by operating the cock of the airless feed cock. It took 50 minutes to finish putting potassium fluoride into the flask. After the reaction was completed, it was found that 33.0 g (0.568 mol) of potassium fluoride had been added by measuring the mass of the concentration flask with an airless feed cock before and after the addition. When the potassium fluoride was added, the liquid started to distill gradually, and when the speed of the liquid distilling into the receiver reached 2 drops/minute, the pressure was gradually lowered to 2 kPaA. The reaction was judged to be completed when no more liquid was distilled out into the receiver for 2 minutes or more, and the flask was removed from the oil bath to create a nitrogen atmosphere. The refrigerant flowing through the Liebig condenser was stopped, the receiver was returned to room temperature, and the mass of the fraction contained in the receiver was measured to be 102.0 g. For analysis, a fraction (0.30 g), hexafluorobenzene (1.30 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, fluorine-containing vinylsulfonic acid fluoride (10) was produced (amount of product: 97.3 g, amount of product: 0.348 mol, production rate: 95.4%).
In this example, β/α was 1.6.
Also, the residue remaining in the flask was collected and the mass was measured to be 126.6 g. For analysis, the residue (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of the analysis, it was also confirmed that a fluorine-containing vinyl sulfonate (11) represented by the following general formula (11) was produced (amount of product: 115.4 g, amount of product: 0.365 mol).
In this example, the addition rate was 0.66 g/min and the mass specific addition rate was 0.20 g/min/g.

[Example 5]
In a space of a nitrogen atmosphere, 349.9 g of the mixed compound (8) produced in Production Example 1 (342.9 g (0.637 mol) of compound (8) and 7.00 g (0.025 mol) of compound (9) ) was placed in a flask and fitted with a half-moon stirrer and a Liebig condenser with a receiver. Furthermore, a concentration flask containing potassium fluoride dried at 150° C. for 5 hours under vacuum was attached to the flask through an airless feedcock (manufactured by Asahi Seisakusho Co., Ltd.). Remove the flask from the space of the nitrogen atmosphere, attach the three-one motor (manufactured by Shinto Kagaku Co., Ltd., BLW300), circulate the -5 ° C. refrigerant in the Liebig condenser, and dry ice the receiver attached to the Liebig condenser. Chilled with chilled ethanol. A pipe made of Teflon (registered trademark) was installed so as to equalize the pressure between the concentrating flasks. The flask was placed in an oil bath (OHB-3100S, manufactured by Tokyo Rikakikai Co., Ltd.) set at 110° C., the pressure was reduced to 70 kPaA, and the mixture was stirred at 120 rpm for 10 minutes. Potassium fluoride was gradually introduced into the flask by operating the cock of the airless feed cock. It took 32 minutes to finish adding potassium fluoride to the flask. After the reaction was completed, it was found that 42.2 g (0.727 mol) of potassium fluoride had been added by measuring the mass of the concentration flask with an airless feed cock before and after the addition. When the potassium fluoride was added, the liquid started to distill gradually, and when the speed of the liquid distilling into the receiver reached 2 drops/minute, the pressure was gradually lowered to 2 kPaA. The reaction was judged to be completed when no more liquid was distilled out into the receiver for 2 minutes or more, and the flask was removed from the oil bath to create a nitrogen atmosphere. The refrigerant flowing through the Liebig condenser was stopped, the receiver was returned to room temperature, and the mass of the fraction contained in the receiver was measured to be 183.3 g. For analysis, a fraction (0.30 g), hexafluorobenzene (1.30 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, fluorine-containing vinyl sulfonic acid fluoride (10) was produced (amount of product: 161.2 g, amount of product: 0.575 mol, production rate: 90.3%).
In this example, β/α was 1.1.
Also, the residue remaining in the flask was recovered and the mass was measured to be 202.9 g. For analysis, the residue (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of the analysis, it was also confirmed that a fluorine-containing vinyl sulfonate (11) represented by the following general formula (11) was produced (amount of product: 197.3 g, amount of product: 0.624 mol).
In this example, the addition rate was 1.3 g/min and the mass specific addition rate was 0.23 g/min/g.

[Example 6]
In a space of a nitrogen atmosphere, 100.1 g of the mixed compound (8) produced in Production Example 1 (98.1 g (0.182 mol) of compound (8) and 2.00 g (0.007 mol) of compound (9) ) was placed in a flask and fitted with a half-moon stirrer and a Liebig condenser with a receiver. Furthermore, a concentration flask containing potassium fluoride dried at 150° C. for 5 hours under vacuum was attached to the flask through an airless feedcock (manufactured by Asahi Seisakusho Co., Ltd.). Remove the flask from the space of the nitrogen atmosphere, attach the three-one motor (manufactured by Shinto Kagaku Co., Ltd., BLW300), circulate the -5 ° C. refrigerant in the Liebig condenser, and dry ice the receiver attached to the Liebig condenser. Chilled with chilled ethanol. A pipe made of Teflon (registered trademark) was installed so as to equalize the pressure between the concentrating flasks. The flask was placed in an oil bath (OHB-3100S, manufactured by Tokyo Rikakikai Co., Ltd.) set at 110° C., the pressure was reduced to 70 kPaA, and the mixture was stirred at 120 rpm for 10 minutes. Potassium fluoride was gradually introduced into the flask by operating the cock of the airless feed cock. It took 75 minutes to finish adding potassium fluoride to the flask. After the reaction was completed, it was found that 99.0 g (1.70 mol) of potassium fluoride had been added by measuring the mass of the concentration flask with an airless feed cock before and after the addition. When the potassium fluoride was added, the liquid started to distill gradually, and when the speed of the liquid distilling into the receiver reached 2 drops/minute, the pressure was gradually lowered to 2 kPaA. The reaction was judged to be completed when no more liquid was distilled out into the receiver for 2 minutes or more, and the flask was removed from the oil bath to create a nitrogen atmosphere. The refrigerant flowing through the Liebig condenser was stopped, the receiver was returned to room temperature, and the mass of the fraction contained in the receiver was measured to be 50.3 g. For analysis, a fraction (0.30 g), hexafluorobenzene (1.30 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, fluorine-containing vinyl sulfonic acid fluoride (10) was produced (amount of product: 48.8 g, amount of product: 0.174 mol, production rate: 95.6%).
In this example, β/α was 9.3.
Also, the residue remaining in the flask was collected and the mass was measured to be 145.6 g. For analysis, the residue (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of the analysis, it was also confirmed that a fluorine-containing vinyl sulfonate (11) represented by the following general formula (11) was produced (amount of product: 58.5 g, amount of product: 0.185 mol).
In this example, the addition rate was 1.3 g/min and the mass specific addition rate was 0.79 g/min/g.

[Example 7]
In a space of a nitrogen atmosphere, 100.0 g of the mixed compound (8) produced in Production Example 1 (98.0 g (0.182 mol) of compound (8) and 2.00 g (0.007 mol) of compound (9) ) was placed in a flask and fitted with a half-moon stirrer and a Liebig condenser with a receiver. Furthermore, a concentration flask containing rubidium fluoride dried at 150° C. for 5 hours under vacuum was attached to the flask via an airless feed cock (manufactured by Asahi Seisakusho Co., Ltd.). Remove the flask from the space of the nitrogen atmosphere, attach the three-one motor (manufactured by Shinto Kagaku Co., Ltd., BLW300), circulate the -5 ° C. refrigerant in the Liebig condenser, and dry ice the receiver attached to the Liebig condenser. Chilled with chilled ethanol. A pipe made of Teflon (registered trademark) was installed so as to equalize the pressure between the concentrating flasks. The flask was placed in an oil bath (OHB-3100S, manufactured by Tokyo Rikakikai Co., Ltd.) set at 80° C., the pressure was reduced to 70 kPaA, and the mixture was stirred at 120 rpm for 10 minutes. Rubidium fluoride was gradually introduced into the flask by operating the cock of the airless feed cock. It took 46 minutes to finish putting the rubidium fluoride into the flask. After the reaction was completed, it was found that 33.1 g (0.317 mol) of rubidium fluoride had been added by measuring the mass of the concentration flask with an airless feed cock before and after the addition. When the rubidium fluoride was added, the liquid began to distill gradually, and when the speed of the liquid distilling into the receiver reached 2 drops/minute, the pressure was gradually lowered to 2 kPaA. The reaction was judged to be completed when no more liquid was distilled into the receiver for 2 minutes or more, and the flask was removed from the oil bath to create a nitrogen atmosphere. The refrigerant flowing through the Liebig condenser was stopped, the receiver was returned to room temperature, and the mass of the fraction contained in the receiver was measured to be 49.0 g. For analysis, a fraction (0.30 g), hexafluorobenzene (1.30 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, fluorine-containing vinyl sulfonic acid fluoride (10) was produced (amount of product: 48.3 g, amount of product: 0.173 mol, production rate: 94.8%).
In this example, β/α was 1.7.
Also, the residue remaining in the flask was collected and the mass was measured to be 79.9 g. For analysis, the residue (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of the analysis, it was also confirmed that a fluorine-containing vinyl sulfonate (4) (a compound represented by the formula (4) in which m is 0, n is 2, and M is Rb) was produced. (amount of product: 66.7 g, amount of product: 0.184 mol).
In this example, the addition rate was 0.72 g/min and the mass specific addition rate was 0.43 g/min/g.

[Example 8]
In a space of a nitrogen atmosphere, 100.2 g of the mixed compound (8) produced in Production Example 1 (98.2 g (0.182 mol) of compound (8) and 2.00 g (0.007 mol) of compound (9) ) was placed in a flask and fitted with a half-moon stirrer and a Liebig condenser with a receiver. Furthermore, a concentration flask containing cesium fluoride dried at 150° C. for 5 hours under vacuum was attached to the flask via an airless feedcock (manufactured by Asahi Seisakusho Co., Ltd.). Remove the flask from the space of the nitrogen atmosphere, attach the three-one motor (manufactured by Shinto Kagaku Co., Ltd., BLW300), circulate the -5 ° C. refrigerant in the Liebig condenser, and dry ice the receiver attached to the Liebig condenser. Chilled with chilled ethanol. A pipe made of Teflon (registered trademark) was installed so as to equalize the pressure between the concentrating flasks. The flask was placed in an oil bath (OHB-3100S manufactured by Tokyo Rikakikai Co., Ltd.) set at 60° C., the pressure was reduced to 70 kPaA, and the mixture was stirred at 120 rpm for 10 minutes. Cesium fluoride was gradually introduced into the flask by operating the cock of the airless feed cock. It took 60 minutes to finish putting cesium fluoride into the flask. After the reaction was completed, it was found that 47.5 g (0.313 mol) of cesium fluoride had been added by measuring the mass of the concentration flask with an airless feed cock before and after the addition. When the cesium fluoride was added, the liquid began to distill gradually, and when the speed of the liquid distilling into the receiver reached 2 drops/minute, the pressure was gradually lowered to 2 kPaA. The reaction was judged to be completed when no more liquid was distilled out into the receiver for 2 minutes or more, and the flask was removed from the oil bath to create a nitrogen atmosphere. The refrigerant flowing through the Liebig condenser was stopped, the receiver was returned to room temperature, and the mass of the fraction contained in the receiver was measured to be 49.1 g. For analysis, a fraction (0.30 g), hexafluorobenzene (1.30 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, fluorine-containing vinyl sulfonic acid fluoride (10) was produced (amount of product: 48.6 g, amount of product: 0.173 mol, production rate: 95.0%).
In this example, β/α was 1.7.
Also, the residue remaining in the flask was collected and the mass was measured to be 93.9 g. For analysis, the residue (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of the analysis, it was also confirmed that a fluorine-containing vinyl sulfonate (4) (a compound represented by the formula (4) in which m is 0, n is 2, and M is Cs) was produced. (amount of product: 75.4 g, amount of product: 0.184 mol).
In this example, the addition rate was 0.79 g/min and the mass specific addition rate was 0.47 g/min/g.

[Comparative Example 1]
Potassium fluoride (54.7 g, 0.941 mol) was placed in a flask equipped with a three-one motor (manufactured by Shinto Kagaku Co., Ltd., BLW300), a crescent-shaped stirring bar, and a Liebig condenser with a receiver. OHB-3100S manufactured by Tokyo Rikaki Co., Ltd.), dried under vacuum at 150° C. for 5 hours, returned to room temperature, and placed in a nitrogen atmosphere. Mixed compound (8) prepared in Production Example 1 (324.8 g, consisting of 318.3 g (0.591 mol) of compound (8) and 6.50 g (0.023 mol) of compound (9)) was added. A −5° C. refrigerant was passed through the Liebig condenser, and a receiver attached to the Liebig condenser was cooled with ethanol cooled with dry ice. The pressure inside the flask was reduced to 50 kPaA, the three-one motor was rotated at 120 rpm, and the flask was placed in an oil bath set at 50°C. Since the liquid did not start to evaporate even after 1 hour, the pressure was gradually lowered, and the liquid started to evaporate, finally reaching 2 kPaA. The reaction was judged to be completed when no liquid was distilled off to the receiver for 2 minutes or more, and the flask was removed from the oil bath to create a nitrogen atmosphere, and then the three-one motor was stopped. The refrigerant flowing through the Liebig condenser was stopped, the receiver was returned to room temperature, and the mass of the fraction contained in the receiver was measured to be 279.3 g. For analysis, a fraction (0.30 g), hexafluorobenzene (1.30 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, fluorine-containing vinylsulfonic acid fluoride (10) was produced (amount of product: 40.2 g, amount of product: 0.143 mol, production rate: 24.3%).
In this example, β/α was 1.6.

[Comparative Example 2]
Potassium fluoride (27.8 g, 0.479 mol) was placed in a flask equipped with a three-one motor (manufactured by Shinto Kagaku Co., Ltd., BLW300), a crescent-shaped stirring bar, and a Liebig condenser with a receiver. OHB-3100S manufactured by Tokyo Rikaki Co., Ltd.), dried under vacuum at 150° C. for 5 hours, returned to room temperature, and placed in a nitrogen atmosphere. Mixed compound (8) prepared in Production Example 1 (168.4 g, consisting of 165.0 g (0.307 mol) of compound (8) and 3.37 g (0.012 mol) of compound (9)) was added. A −5° C. refrigerant was passed through the Liebig condenser, and a receiver attached to the Liebig condenser was cooled with ethanol cooled with dry ice. The pressure inside the flask was reduced to 95 kPaA, the three-one motor was rotated at 120 rpm, and the flask was placed in an oil bath set at 130°C. Distillation of the liquid started, and when the speed of the liquid distilled off to the receiver reached 2 drops/minute, the pressure was gradually lowered to 2 kPaA finally. The reaction was judged to be completed when no liquid was distilled off to the receiver for 2 minutes or more, and the flask was removed from the oil bath to create a nitrogen atmosphere, and then the three-one motor was stopped. The refrigerant flowing through the Liebig condenser was stopped, the receiver was returned to room temperature, and the mass of the fraction contained in the receiver was measured to be 100.3 g. For analysis, a fraction (0.30 g), hexafluorobenzene (1.30 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, fluorine-containing vinyl sulfonic acid fluoride (10) was produced (amount of product: 53.9 g, amount of product: 0.192 mol, production rate: 62.7%).
In this example, β/α was 1.6.

As shown in Examples 1 to 8, in the reaction between the fluorine-containing vinylsulfonic anhydride (1) and the alkali metal fluoride (2), the fluorine-containing vinylsulfonic anhydride (1) was heated to It was shown that the addition of alkali metal fluoride (2) yields fluorine-containing vinyl sulfonic acid fluoride (3) in high yield. It was also shown that a fluorine-containing vinyl sulfonate (4) can be obtained.

[Example 9]
10.0 g of the residue containing the fluorine-containing vinyl sulfonate (11) obtained in Example 1 was placed in a flask equipped with a stirrer, 36.9 g of acetonitrile was added, and the mixture was stirred for 30 minutes. The resulting solution was placed in a stainless steel holder with a tank equipped with a flask at the outlet (KST-47 manufactured by Advantech Toyo Co., Ltd. TR G940B2K manufactured by Nakao Filter Industry Co., Ltd. was used as the filter paper), and was evacuated to zero with nitrogen. It was pressurized to .2 MPaG and filtered. Volatile components are distilled off from the filtrate obtained in the flask using a rotary evaporator (N-1300V, manufactured by Tokyo Rikakiki Co., Ltd.), followed by vacuum drying with a vacuum dryer (AVO-250V, manufactured by AS ONE Co., Ltd.). Thus, a solid was obtained. For analysis, the obtained solid (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, it was confirmed that 9.02 g (28.5 mmol) of fluorine-containing vinyl sulfonate (11) was obtained.
In this example, γ/δ was 3.7.

[Example 10]
10.3 g of the residue containing fluorine-containing vinyl sulfonate (11) obtained in Example 1 was placed in a flask equipped with a stirrer, 101.0 g of butyl acetate was added, and the mixture was stirred for 30 minutes. The obtained solution was placed in a stainless steel holder with a tank equipped with a flask at the outlet (KST-47 manufactured by Advantech Toyo Co., Ltd. TR G940B2K manufactured by Nakao Filter Industry Co., Ltd. was used as the filter paper), and was evacuated to zero with nitrogen. It was pressurized to .2 MPaG and filtered. Volatile components are distilled off from the filtrate obtained in the flask using a rotary evaporator (N-1300V, manufactured by Tokyo Rikakiki Co., Ltd.), followed by vacuum drying with a vacuum dryer (AVO-250V, manufactured by AS ONE Co., Ltd.). Thus, a solid was obtained. For analysis, the obtained solid (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, it was confirmed that 9.27 g (29.3 mmol) of fluorine-containing vinyl sulfonate (11) was obtained.
In this example, γ/δ was 9.8.

[Example 11]
10.1 g of the residue containing the fluorine-containing vinyl sulfonate (11) obtained in Example 1 was placed in a flask equipped with a stirrer, 84.7 g of 4-methyl-2-pentanone was added, and the mixture was stirred for 30 minutes. did. The resulting solution was placed in a stainless steel holder with a tank equipped with a flask at the outlet (KST-47 manufactured by Advantech Toyo Co., Ltd. TR G940B2K manufactured by Nakao Filter Industry Co., Ltd. was used as the filter paper), and was evacuated to zero with nitrogen. It was pressurized to .2 MPaG and filtered. Volatile components are distilled off from the filtrate obtained in the flask using a rotary evaporator (N-1300V, manufactured by Tokyo Rikakiki Co., Ltd.), followed by vacuum drying with a vacuum dryer (AVO-250V, manufactured by AS ONE Co., Ltd.). Thus, a solid was obtained. For analysis, the obtained solid (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, it was confirmed that 9.06 g (28.7 mmol) of fluorine-containing vinyl sulfonate (11) was obtained.
In this example, γ/δ was 8.4.

[Example 12]
50.2 g of the residue containing the fluorine-containing vinyl sulfonate (11) obtained in Example 1 was placed in a flask equipped with a stirrer, 117.6 g of dimethyl carbonate was added, and the mixture was stirred for 1 hour. The resulting solution was placed in a stainless steel holder with a tank equipped with a flask at the outlet (KST-47 manufactured by Advantech Toyo Co., Ltd. TR G940B2K manufactured by Nakao Filter Industry Co., Ltd. was used as the filter paper), and was evacuated to zero with nitrogen. It was pressurized to .2 MPaG and filtered. Volatile components are distilled off from the filtrate obtained in the flask using a rotary evaporator (N-1300V, manufactured by Tokyo Rikakiki Co., Ltd.), followed by vacuum drying with a vacuum dryer (AVO-250V, manufactured by AS ONE Co., Ltd.). Thus, a solid was obtained. For analysis, the obtained solid (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, it was confirmed that 45.1 g (0.143 mol) of fluorine-containing vinyl sulfonate (11) was obtained.
In this example, γ/δ was 2.3.
As a result of analysis by ¹ H-NMR of the volatile components distilled off by the rotary evaporator, dimethyl carbonate was confirmed to be the main component. 30.0 g of the volatile component mainly composed of dimethyl carbonate and 10.0 g of the residue containing the fluorine-containing vinyl sulfonate (11) obtained in Example 1 were mixed and filtered in the same manner as described in this example. Then, volatile components were distilled off from the filtrate, and a solid was obtained by vacuum drying. As a result of analyzing the resulting solid by ¹⁹ F-NMR, it was confirmed that fluorine-containing vinyl sulfonate (11) was obtained.
The filter cake obtained on the filter paper by filtration was vacuum-dried with a vacuum dryer (AVO-250V, manufactured by AS ONE Co., Ltd.) to obtain 5.05 g of the dried filter cake. In a space of a nitrogen atmosphere, 24.0 g of the mixed compound (8) produced in Production Example 1 (23.5 g (43.7 mmol) of compound (8) and 0.48 g (1.73 mmol) of compound (9) ) was placed in a flask and fitted with a half-moon stirrer and a Liebig condenser with a receiver. The concentration flask containing the dried filter cake was attached to the flask via an airless feedcock (manufactured by Asahi Seisakusho Co., Ltd.). Remove the flask from the space of the nitrogen atmosphere, attach the three-one motor (manufactured by Shinto Kagaku Co., Ltd., BLW300), circulate the -5 ° C. refrigerant in the Liebig condenser, and dry ice the receiver attached to the Liebig condenser. Chilled with chilled ethanol. A pipe made of Teflon (registered trademark) was installed so as to equalize the pressure between the concentrating flasks. The flask was placed in an oil bath (OHB-3100S, manufactured by Tokyo Rikakikai Co., Ltd.) set at 110° C., the pressure was reduced to 70 kPaA, and the mixture was stirred at 120 rpm for 10 minutes. By operating the cock of the airless feed cock, the dried filter cake was gradually introduced into the flask. It took 10 minutes to finish putting the dried filter cake into the flask. When the dried filter cake was added, the liquid gradually started to distill, and when the speed of the liquid distilled to the receiver reached 2 drops/minute, the pressure was gradually lowered to 2 kPaA. The reaction was judged to be completed when no more liquid was distilled out into the receiver for 2 minutes or more, and the flask was removed from the oil bath to create a nitrogen atmosphere. The refrigerant flowing through the Liebig condenser was stopped, the receiver was returned to room temperature, and the mass of the fraction contained in the receiver was measured to be 12.1 g. For analysis, a fraction (0.30 g), hexafluorobenzene (1.30 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, fluorine-containing vinylsulfonic acid fluoride (10) was produced (amount of product: 11.0 g, amount of product: 39.5 mmol, production rate: 90.2%).
In this example, the addition rate was 0.42 g/min and the mass specific addition rate was 1.1 g/min/g.

[Example 13]
10.1 g of the residue containing the fluorine-containing vinyl sulfonate (11) obtained in Example 1 was placed in a flask equipped with a stirrer, 14.4 g of 1,2-dimethoxyethane was added, and the mixture was stirred for 1 hour. . The resulting solution was placed in a stainless steel holder with a tank equipped with a flask at the outlet (KST-47 manufactured by Advantech Toyo Co., Ltd. TR G940B2K manufactured by Nakao Filter Industry Co., Ltd. was used as the filter paper), and was evacuated to zero with nitrogen. It was pressurized to .2 MPaG and filtered. Volatile components are distilled off from the filtrate obtained in the flask using a rotary evaporator (N-1300V, manufactured by Tokyo Rikakiki Co., Ltd.), followed by vacuum drying with a vacuum dryer (AVO-250V, manufactured by AS ONE Co., Ltd.). Thus, a solid was obtained. For analysis, the obtained solid (0.20 g), purified water (1.00 g) and 2,2,2-trifluoroethanol (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis, it was confirmed that 9.02 g (28.5 mmol) of fluorine-containing vinyl sulfonate (11) was obtained.
In this example, γ/δ was 1.4.

[Example 14]
51.0 g of the residue containing the fluorine-containing vinyl sulfonate (11) obtained in Example 1 was placed in a flask equipped with a stirrer, 108.4 g of dimethyl carbonate was added, and the mixture was stirred for 1 hour. The resulting solution was placed in a stainless steel holder with a tank equipped with a flask at the outlet (KST-47 manufactured by Advantech Toyo Co., Ltd. TR G940B2K manufactured by Nakao Filter Industry Co., Ltd. was used as the filter paper), and was evacuated to zero with nitrogen. It was pressurized to .2 MPaG and filtered. Transfer 100.0 g of the filtrate obtained in the flask to another flask, add 55.7 g of purified water, and use a rotary evaporator (manufactured by Tokyo Rikakiki Co., Ltd., N-1300V) to distill off the volatile components (flask The amount of contents was 88.1 g). 55.7 g of purified water was added to the flask, and the volatile components were distilled off using a rotary evaporator (manufactured by Tokyo Rikakiki Co., Ltd., N-1300V) (the amount of the flask contents was 86.5 g). . 55.7 g of purified water was added to the flask, and the volatile components were distilled off using a rotary evaporator (manufactured by Tokyo Rikakiki Co., Ltd., N-1300V) (the amount of the flask content was 85.7 g). . For analysis, 2,2,2-trifluoroethanol (0.10 g) was mixed with the resulting contents of the flask (1.00 g) and analyzed by ¹⁹ F-NMR and ¹ H-NMR. As a result of analysis by ¹⁹ F-NMR, it was confirmed that 30.0 g of fluorine-containing vinyl sulfonate (11) was contained in the contents of the flask. As a result of ¹ H-NMR analysis, no dimethyl carbonate was observed. From this, it was confirmed that the content of the flask was an aqueous solution of the fluorine-containing vinyl sulfonate (11).
When all the volatile components distilled off by the evaporator were recovered, they were separated into two phases. As a result of analyzing each phase by ¹ H-NMR, it was confirmed that the lower phase was composed mainly of dimethyl carbonate and the upper phase was composed mainly of water. Using a separating funnel, a phase (95.0 g) containing dimethyl carbonate as a main component and a phase (124.8 g) containing water as a main component were separated. As a result of analyzing the water content of the phase containing dimethyl carbonate as the main component with a Karl Fischer moisture meter (MKC-710D manufactured by Kyoto Electronics Industry Co., Ltd.), the water content was 3.0% by mass.
11.1 g of the obtained phase containing dimethyl carbonate as a main component and 5.20 g of the residue containing the fluorine-containing vinyl sulfonate (11) obtained in Example 1 were mixed and mixed in the same manner as described in this example. After filtration, volatile components were distilled off from the filtrate, and a solid was obtained by vacuum drying. As a result of analyzing the resulting solid by ¹⁹ F-NMR, it was confirmed that fluorine-containing vinyl sulfonate (11) was obtained.
The resulting dimethyl carbonate-based phase (84.0 g) was placed in a flask of a distillation apparatus and the volatile components were distilled off (flask content was 67.4 g). As a result of analyzing the water content of the resulting flask contents with a Karl Fischer moisture meter (manufactured by Kyoto Electronics Industry Co., Ltd., MKC-710D), the water content was 1.0% by mass, and the water content was reduced. A dimethyl carbonate-based phase could be prepared. 20.8 g of a phase mainly composed of dimethyl carbonate with a reduced water content and 9.80 g of the residue containing the fluorine-containing vinyl sulfonate (11) obtained in Example 1 were mixed, and the Similarly, filtration was performed, volatile components were removed from the filtrate, and a solid was obtained by vacuum drying. As a result of analyzing the resulting solid by ¹⁹ F-NMR, it was confirmed that fluorine-containing vinyl sulfonate (11) was obtained.
39.8 g of an aqueous solution of fluorine-containing vinyl sulfonate (11) (containing 13.9 g (44.1 mmol) of fluorine-containing vinyl sulfonate (11)) was placed in a separable flask, and sulfuric acid Special reagent grade manufactured by Kojunyaku Co., Ltd.) (8.64 g) was gradually added. Subsequently, cyclopentyl methyl ether (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd., Wako special grade) (27.9 g) was added, stirred for 1 hour, and then allowed to stand for 2 hours. The upper cyclopentyl methyl ether phase (1.0 g) was taken out and analyzed by ¹⁹ F-NMR. As a result, it was confirmed that compound (9) was obtained.

[Example 15]
39.9 g of the fluorine-containing vinyl sulfonic acid fluoride (10) obtained in Example 1 was placed in a flask of a distillation apparatus (using Sulzer EX laboratory packing manufactured by Sulzer Co. as a packing material) and distilled. An initial stream of 1.93 g was separated, followed by a 34.7 g distillate. The resulting fraction (0.30 g), hexafluorobenzene (3.00 g) and benzotrifluoride (0.10 g) were mixed and analyzed by GC. , 99.9%.

[Example 16]
39.6 g of the fluorine-containing vinyl sulfonic acid fluoride (10) obtained in Example 1 and 19.8 g of purified water were placed in a flask equipped with a stirrer and stirred for 30 minutes. After standing for a minute, an upper phase (20.2 g) and a lower phase (38.7 g) were obtained. For analysis, the obtained lower phase (0.30 g), 1,2-dimethoxyethane (1.00 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis by ¹⁹ F-NMR, it was confirmed that 37.8 g of fluorine-containing vinylsulfonic acid fluoride (10) was contained in the lower phase taken.
ζ/ε in this example was 0.50.
The above lower phase was placed in a flask of a distillation apparatus (using Sulzer EX laboratory packing manufactured by Sulzer Co. as a packing material) and distilled. A 3.10 g portion was taken as the initial stream, followed by a 32.5 g fraction. The resulting fraction (0.30 g), hexafluorobenzene (3.00 g) and benzotrifluoride (0.10 g) were mixed and analyzed by GC. , 99.9%.
The obtained upper phase (10.3 g) and 10.1 g of the fluorine-containing vinylsulfonic acid fluoride (10) obtained in Example 1 were placed in a flask equipped with a stirrer, stirred for 30 minutes, and separated. It was placed in a funnel and allowed to stand for 30 minutes to obtain a lower phase (9.91 g). The obtained lower phase (0.30 g), 1,2-dimethoxyethane (1.00 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis by ¹⁹ F-NMR, it was confirmed that 9.64 g of fluorine-containing vinylsulfonic acid fluoride (10) was contained in the lower phase taken.

[Example 17]
40.5 g of the fluorine-containing vinyl sulfonic acid fluoride (10) obtained in Example 1 and 40.5 g of an aqueous sodium hydrogencarbonate solution were placed in a flask equipped with a stirrer, stirred for 30 minutes, and placed in a separating funnel. , and allowed to stand for 30 minutes to obtain an upper phase (40.5 g) and a lower phase (39.3 g). For analysis, the obtained lower phase (0.30 g), 1,2-dimethoxyethane (1.00 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis by ¹⁹ F-NMR, it was confirmed that 38.6 g of fluorine-containing vinylsulfonic acid fluoride (10) was contained in the lower phase taken.
ζ/ε in this example was 1.0.
The above lower phase was placed in a flask of a distillation apparatus (using Sulzer EX laboratory packing manufactured by Sulzer Co. as a packing material) and distilled. An initial stream of 2.56 g was separated, followed by a 33.6 g distillate. The resulting fraction (0.30 g), hexafluorobenzene (3.00 g) and benzotrifluoride (0.10 g) were mixed and analyzed by GC. , 99.9%.
The obtained upper phase (20.4 g) and 10.2 g of the fluorine-containing vinylsulfonic acid fluoride (10) obtained in Example 1 were placed in a flask equipped with a stirrer, stirred for 30 minutes, and separated. It was placed in a funnel and allowed to stand for 30 minutes to obtain a lower phase (9.94 g). The obtained lower phase (0.30 g), 1,2-dimethoxyethane (1.00 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis by ¹⁹ F-NMR, it was confirmed that 9.73 g of fluorine-containing vinylsulfonic acid fluoride (10) was contained in the lower phase taken.

[Example 18]
10.6 g of the fluorine-containing vinyl sulfonic acid fluoride (10) obtained in Example 1 and 53.0 g of an aqueous sodium hydrogen carbonate solution were placed in a flask equipped with a stirrer, stirred for 30 minutes, and placed in a separating funnel. , and allowed to stand for 30 minutes to obtain an upper phase (52.6 g) and a lower phase (10.3 g). For analysis, the obtained lower phase (0.30 g), 1,2-dimethoxyethane (1.00 g) and benzotrifluoride (0.10 g) were mixed and analyzed by ¹⁹ F-NMR. As a result of analysis by ¹⁹ F-NMR, it was confirmed that 10.1 g of fluorine-containing vinylsulfonic acid fluoride (10) was contained in the lower phase taken.
ζ/ε in this example was 5.0.

A fluorine-containing vinylsulfonic acid fluoride (3) obtained by reacting a fluorine-containing vinylsulfonic anhydride (1) with an alkali metal fluoride (2) as shown in Examples 9 to 18, or It was shown that the fluorine-containing vinyl sulfonate (4) could be separated. It was also shown that the compounds used for separation can be reused.

According to the production method of the present invention, the fluorine-containing vinyl sulfonic acid fluoride (3) can be produced at a higher yield than conventionally, and various fluorine-containing compounds, ion-exchange resins, ion-exchange membranes, salt electrolytic membranes, and fuels can be produced. It can be suitably used in the production of raw materials for battery membranes, membranes for redox flow batteries, membranes for water electrolysis, and the like. In addition, a fluorine-containing vinyl sulfonate (4) that can be converted into various fluorine compounds can be produced. Furthermore, the fluorine-containing vinylsulfonic acid fluoride (3) and/or the fluorine-containing vinylsulfonate (4) can be separated, and the compounds used for separation can be reused.

Claims (29)

The following general formula (3):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6)
Fluorinated vinyl sulfonic acid fluoride (3) represented by and/or the following general formula (4):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6, and M is K, Rb, or Cs.)
A method for producing a fluorine-containing vinyl sulfonate (4) represented by
The following general formula (1):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6)
A fluorine-containing vinyl sulfonic anhydride (1) represented by
The following general formula (2):
MF (2)
(In the formula, M is K, Rb, or Cs.)
In the reaction with an alkali metal fluoride (2) represented by
adding an alkali metal fluoride (2) to a fluorine-containing vinylsulfonic anhydride (1) under heating;
A manufacturing method characterized by: The production method according to claim 1, wherein the reaction temperature is 60 to 250°C. Claim 1, wherein the ratio (β/α) of the amount (β) of the alkali metal fluoride (2) to the amount (α) of the fluorine-containing vinylsulfonic anhydride (1) is 1 to 100. Or the production method according to 2. The following general formula (3):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6)
The production method according to claim 1, which is a production method of the fluorine-containing vinyl sulfonic acid fluoride (3) represented by. The following general formula (4):

(Wherein, m is an integer of 0 to 3, n is an integer of 1 to 6, and M is K, Rb, or Cs.)
The production method according to claim 1, which is a production method of the fluorine-containing vinyl sulfonate (4) represented by 2. The production method according to claim 1, comprising a step of separating the fluorine-containing vinylsulfonic acid fluoride (3). 7. The production method according to claim 6, comprising a step of distilling the fluorine-containing sulfonic acid fluoride (3). 7. The production method according to claim 6, comprising the step of mixing said fluorine-containing sulfonic acid fluoride (3) with an extraction compound. 9. The production method according to claim 8, wherein the extraction compound is at least one compound selected from the group consisting of water, an inorganic salt-containing aqueous solution, an alcohol compound, an amide compound, and a sulfo compound. The inorganic salt-containing aqueous solution contains at least one inorganic salt compound selected from the group consisting of carbonates, sulfates, thiosulfates, acetates, phosphates, citrates, tartrates, and tetraborates. The production method according to claim 9, which is an aqueous solution containing The production method according to claim 8, wherein the ratio (ζ/ε) of the mass (ζ) of the extraction compound to the mass (ε) of the fluorine-containing sulfonic acid fluoride (3) is 0.1-100. The mixed solution obtained by the above step of mixing the fluorine-containing sulfonic acid fluoride (3) and the extraction compound is allowed to stand, and a phase containing the fluorine-containing sulfonic acid fluoride (3) and a phase containing the extraction compound are formed. 9. The manufacturing method according to claim 8, comprising the step of separating into 13. The production method according to claim 12, wherein the phase containing the extraction compound is reused in the step of mixing the fluorine-containing sulfonic acid fluoride (3) and the extraction compound. 13. The production method according to claim 12, comprising a step of separating the fluorine-containing sulfonic acid fluoride (3) from the phase containing the fluorine-containing sulfonic acid fluoride (3) by distillation. 2. The production method according to claim 1, comprising a step of separating reaction residues. 16. The production method according to claim 15, comprising the step of mixing the reaction residue and a dissolved compound to prepare a fluorine-containing sulfonate solution. 17. The production method according to claim 16, wherein the dissolved compound is at least one compound selected from the group consisting of ether compounds, ketone compounds, ester compounds, carbonate compounds, and nitrile compounds. The production method according to claim 16, wherein the ratio (δ/γ) of the mass (δ) of the dissolved compound to the mass (γ) of the reaction residue is 0.01-100. 17. The production method according to claim 16, comprising filtering the fluorine-containing sulfonate solution to obtain a fluorine-containing sulfonate-containing filtrate. 17. The production method according to claim 16, comprising filtering the fluorine-containing sulfonate solution to obtain a filter cake containing the alkali metal fluoride (2). 21. The production according to claim 20, wherein the filter cake containing the alkali metal fluoride (2) is reused for the reaction between the fluorine-containing vinylsulfonic anhydride (1) and the alkali metal fluoride (2). Method. 20. The production method according to claim 19, comprising a step of separating volatile components including the dissolved compound from the fluorine-containing sulfonate-containing filtrate to obtain the fluorine-containing vinyl sulfonate (4). 23. The production method according to claim 22, wherein the volatile component containing the dissolved compound is reused in the step of mixing the reaction residue and the dissolved compound to prepare the fluorine-containing sulfonate solution. 20. The production method according to claim 19, comprising adding water to the fluorine-containing sulfonate-containing filtrate and mixing. The production method according to claim 24, wherein the ratio (κ/ι) of the mass (ι) of the fluorine-containing sulfonate-containing filtrate to the total mass (κ) of the water is 0.1-100. a step of separating volatile components including the dissolved compound from the solution obtained by the step of adding water to the fluorine-containing sulfonate-containing filtrate and mixing to prepare a fluorine-containing sulfonate-containing aqueous solution; 25. The manufacturing method according to claim 24. A volatile component containing the dissolved compound is separated from the solution obtained by adding water to the fluorine-containing sulfonate-containing filtrate and mixing, and separated in a step of preparing a fluorine-containing sulfonate-containing aqueous solution. 27. The method of claim 26, comprising separating water from the volatile components comprising dissolved compounds dissolved in the water. 28. The production method according to claim 26 or 27, wherein the volatile component containing the dissolved compound is mixed with the reaction residue and the dissolved compound and reused in the step of preparing the fluorine-containing sulfonate solution. A volatile component containing the dissolved compound is separated from the solution obtained by adding water to the fluorine-containing sulfonate-containing filtrate and mixing, and separated in a step of preparing a fluorine-containing sulfonate-containing aqueous solution. 25. The method according to claim 24, wherein the water separated in the step of separating water from the volatile components containing the dissolved compound is reused in the step of adding and mixing water to the fluorine-containing sulfonate-containing filtrate. Method of manufacture as described.