WO2014157412A1 - シクロアルキルアルキルエーテル化合物の製造方法 - Google Patents
シクロアルキルアルキルエーテル化合物の製造方法 Download PDFInfo
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- WO2014157412A1 WO2014157412A1 PCT/JP2014/058679 JP2014058679W WO2014157412A1 WO 2014157412 A1 WO2014157412 A1 WO 2014157412A1 JP 2014058679 W JP2014058679 W JP 2014058679W WO 2014157412 A1 WO2014157412 A1 WO 2014157412A1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/05—Preparation of ethers by addition of compounds to unsaturated compounds
- C07C41/06—Preparation of ethers by addition of compounds to unsaturated compounds by addition of organic compounds only
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/06—Systems containing only non-condensed rings with a five-membered ring
- C07C2601/08—Systems containing only non-condensed rings with a five-membered ring the ring being saturated
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- the present invention relates to a cycloalkyl alkyl useful as a cleaning solvent for electronic parts and precision machine parts, a solvent for chemical reaction, a solvent for extraction, a solvent for crystallization, a chromatographic eluent, a solvent for electronic and electrical materials, and a release agent.
- the present invention relates to a method for producing an ether compound in an industrially advantageous manner.
- Patent Document 1 discloses a method using crystalline aluminosilicate as a catalyst
- Patent Document 2 discloses a method using a special aluminosilicate having a large number of acid points on the outer surface
- Patent Document 3 discloses a catalyst as a catalyst.
- a method of using an oxide of tungsten in which water of crystallization of a heteropoly acid is adjusted to an average of 3.0 molecules or less per molecule of the heteropoly acid is disclosed in Patent Document 4 as an acid having a water content of 5% by mass or less as a catalyst.
- Patent Document 4 A method using an ion exchange resin is disclosed.
- this method has the following problems, that is, when a cycloalkyl alkyl ether is produced on an industrial scale using these solid acid catalysts and an alicyclic olefin as a starting material, the process is continued for a long time.
- the catalyst activity decreases with time during operation. For this reason, it has been necessary to frequently regenerate a catalyst with reduced activity or to replenish or replace it.
- Patent Document 5 discloses a method using a raw material alicyclic olefin having a chain conjugated diene compound content of 10 ppm or less
- Patent Document 6 discloses a raw material alicyclic olefin.
- the olefin a method using a chain conjugated diene compound and a cyclic conjugated diene compound both containing 10 ppm or less has been proposed.
- these methods can suppress a decrease in catalyst activity over time, they have not been sufficiently satisfactory in terms of reaction efficiency and productivity.
- the present invention has been made in view of the above-described prior art, and the object thereof is to reduce the catalytic activity with time, and to achieve a high reaction efficiency even when the raw material supply is increased. It is to provide a method by which alkyl ethers can be produced.
- a cyclopentene or a cyclohexene and an alcohol in the presence of an acidic ion exchange resin having a specific surface area, an average pore diameter, and a total exchange capacity in a specific range. It has been found that when a compound is reacted in a gaseous state, a cycloalkyl alkyl ether can be stably produced with high reaction efficiency even when the amount of raw material supply is increased, and the present invention has been completed.
- the cycloalkyl alkyl ether can be produced with high reaction efficiency even when the catalyst activity is less likely to decrease with time and the raw material supply is increased.
- the target cycloalkyl alkyl ether compound can be produced industrially advantageously.
- FIG. 1 It is a schematic diagram of the reaction apparatus for enforcing the manufacturing method of this invention. It is a schematic diagram of the apparatus which combined the reaction apparatus and the distillation apparatus for enforcing the manufacturing method of this invention.
- Space velocity feed gas inflow rate per unit volume of reaction tube (h ⁇ 1 ), hereinafter referred to as “GHSV (h ⁇ 1 )”.
- GHSV feed gas inflow rate per unit volume of reaction tube
- the method for producing a cycloalkyl alkyl ether compound of the present invention comprises a cyclopentene which may have a substituent in the presence of an acidic ion exchange resin, or a cyclohexene which may have a substituent, and the formula (2).
- the acidic ion exchange resin has a specific surface area of 20 to 50 m 2 / g, an average pore size of 20 to 70 nm, and a total exchange capacity of 4.8 to 6.0 eq / What is characterized by using an LR wet resin.
- an alcohol compound (2) is reacted with an optionally substituted group (cyclopentene or cyclohexene).
- substituent cyclopentene or cyclohexene
- substituent used in the present invention include a methyl group, an ethyl group, an n-propyl group, an isopropyl group, an n-butyl group, a t-butyl group, a sec- Alkyl groups having 1 to 4 carbon atoms such as butyl group and isobutyl group; carbon numbers such as methoxy group, ethoxy group, n-propoxy group, sec-propoxy group, n-butoxy group, t-butoxy group and sec-butoxy group 1 to 4 alkoxy groups; alkylthio groups having 1 to 4 carbon atoms such as methylthio, ethylthio, n-propylthio, sec-butylthio, and t-
- cyclopentenes which may have a substituent
- cyclopentenes include cyclopentene; 1-methylcyclopentene, 2-methylcyclopentene, 3-methylcyclopentene, 3-ethylcyclopentene.
- Alkylcyclopentene such as 3-sec-butylcyclopentene, 2-t-butylcyclopentene, 1,3-dimethylcyclopentene; 3-methoxycyclopentene, 3-ethoxycyclopentene, 2-sec-butoxycyclopentene, 3-t-butoxycyclopentene, etc.
- Alkoxycyclopentenes such as 3-methylthiocyclopentene, 3-ethylthiocyclopentene, 2-sec-butylthiocyclopentene, and 3-t-butylthiocyclopentene; Le Orosi black pentene, 2-chloro-cyclopentene, 3-chloro-cyclopentene, 2-bromo-cyclopentene cyclopentene halides such as 3-bromo-cyclopentene; 1-phenyl-cyclopentene such aryl cyclopentene; and the like.
- cyclohexenes include cyclohexene; 1-methylcyclohexene, 4-methylcyclohexene, 3-ethylcyclohexene, 3-ethyl alkylcyclohexene such as sec-butylcyclohexene, 2-t-butylcyclohexene, 1,3-dimethylcyclohexene; alkoxycyclohexene such as 3-methoxycyclohexene, 3-ethoxycyclohexene, 2-sec-butoxycyclohexene, 3-t-butoxycyclohexene Alkylthiocyclohexene such as 3-methylthiocyclohexene, 3-ethylthiocyclohexene, 2-sec-butylthiocyclohexene, 3-t-butylthiocyclohexene, etc .; 1-fluor
- the alcohol compound (2) used in the present invention is a compound represented by the formula (2): R 1 OH, wherein R 1 is an alkyl having 1 to 10 carbon atoms which may have a substituent. Or a cycloalkyl group having 3 to 8 carbon atoms which may have a group or a substituent.
- Examples of the optionally substituted alkyl group having 1 to 10 carbon atoms include methyl group, ethyl group, n-propyl group, isopropyl group, n-butyl group, sec-butyl group, t-butyl group, n -C1-C10 alkyl groups such as pentyl, neopentyl, n-hexyl, n-heptyl, n-octyl, n-nonyl, n-decyl; methoxymethyl, 1-methoxyethyl Groups, alkoxyalkyl groups such as 2-ethoxy-tert-butyl group, 2-ethoxy-n-hexyl group; methylthiomethyl group, 1-methylthioethyl group, 2-methylthio-tert-butyl group, 4-methylthio-n- Alkylthioalkyl groups such as hexyl group; chloromethyl group, bromomethyl group
- Examples of the cycloalkyl group having 3 to 8 carbon atoms which may have a substituent include cyclopropyl group, cyclobutyl group, cyclopentyl group, cyclohexyl group, cycloheptyl group, cyclooctyl group and the like.
- Alkyl groups alkoxycycloalkyl groups such as 2-methoxy-cyclopropyl group and 3-ethoxy-cyclohexyl group; alkylthiocycloalkyl groups such as 2-methylthio-cyclopropyl group and 3-ethylthio-cyclohexyl group; 2-chloro-cyclo And halogenated cycloalkyl groups such as propyl group and 3-bromo-cyclohexyl group.
- the alcohol compound (2) examples include methanol, ethanol, 2-methoxyethanol, n-propanol, 2-chloro-n-propanol, isopropanol, n-butanol, 3-methylthio-n-butanol, 2-bromo- In the above formula (2) such as n-butanol, sec-butanol, isobutanol, tert-butanol, n-pentanol, n-hexanol, cyclopropyl alcohol, etc., R 1 may have a substituent.
- cyclopentene or cyclohexene and an alcohol compound in which R 1 is an alkyl group having 1 to 10 carbon atoms in the above formula (2) are used. It is preferable to use cyclopentene and an alcohol compound in which R 1 in the formula (2) is an alkyl group having 1 to 10 carbon atoms.
- the amount of the alcohol compound (2) used is usually 0.002 to 11 mol, preferably 0.02 to 7 mol, relative to 1 mol of cyclopentenes (cyclohexenes).
- the reaction temperature is usually in the range of 50 to 150 ° C., preferably 80 to 120 ° C.
- a specific acidic ion exchange resin is used as a reaction catalyst.
- the acidic ion exchange resin is composed of an insoluble and porous synthetic resin having an acidic ion exchange group on a fine three-dimensional network polymer base, and is generally called a cation exchange resin.
- acidic ion exchange resins can be broadly classified into gel type, porous type, and high porous type as classified from the geometrical structure, but any type can be used in the present invention. .
- the acidic ion exchange resin a strongly acidic cation ion exchange resin having a sulfonic acid group as an ion exchange group on a styrene-based polymer substrate; an acrylic acid group or methacryl as an ion exchange group on an acrylic or methacrylic polymer substrate.
- a weakly acidic cation exchange resin having an acid group and the like.
- the acidic ion exchange resin used in the present invention has a specific surface area of 20 to 50 m 2 / g, preferably 30 to 50 m 2 / g, more preferably 35 to 45 m 2 / g, and an average pore size of 20 to 70 nm, preferably 20 to 40 nm, more preferably 22 to 30 nm, and the total exchange capacity is 4.8 to 6.0 eq / LR wet resin, preferably 5.0 to 5.5 eq / LR wet resin, more preferably Is a 5.2 to 5.4 eq / LR wet resin.
- the specific surface area refers to the surface area (m 2 ) per unit mass (g). It can be said that the larger the specific surface area, the better the function as a catalyst. However, when the specific surface area is large, the object becomes unstable in the system.
- the average pore diameter means an average value of pore diameters (nm).
- the total exchange capacity refers to the total number of ion exchange groups involved in ion exchange per unit resin amount in a wet state (resin is usually commercially available in this state). In the present application, the equivalent per 1 L of acidic ion exchange resin, that is, “eq / LR” (R represents a wet resin).
- the apparent density (g / LR) of the acidic ion exchange resin A is usually 500 to 1000, preferably 600 to 900.
- the apparent density is generally the density when the solid itself and the internal voids are in volume.
- the specific surface area, average pore diameter, total exchange capacity, and apparent density of the acidic ion exchange resin can be measured and determined by known methods.
- the acidic ion exchange resin A is usually used in a proton type, and can be used repeatedly by performing a normal regeneration treatment.
- the specific surface area is 20 to 50 m 2 / g
- the average pore diameter is 20 to 70 nm
- the total exchange capacity is 4.8 to 6.
- a resin that is a 0 eq / LR wet resin Preferable specific examples of the acidic ion exchange resin used in the present invention include trade name: CT276 (manufactured by Purolite), trade names: Amberist 35, Amberlist 36 (manufactured by Organo), and the like.
- the acidic ion exchange resin A is preferably used after dehydration.
- the water content is preferably 5% by mass or less, more preferably 3% by mass or less, and particularly preferably 2% by mass or less.
- an acidic ion exchange resin A having a water content of 5% by mass or less it may be dried in advance before use to remove moisture.
- the method for drying the acidic ion exchange resin A is not particularly limited as long as it is a method that can be dried to obtain the acidic ion exchange resin A having a water content of 5% by mass or less.
- a normal heat dehydration operation can be employed.
- the heat dehydration operation include: (i) a method in which the acidic ion exchange resin A is accommodated in a normal dryer and heated at 50 to 120 ° C., preferably 80 to 100 ° C. for several minutes to several hours; (ii) acidic ions A method in which the exchange resin A is heated and dried at a predetermined temperature (room temperature to about 100 ° C.) for several minutes to several hours under inert gas flow conditions; and (iii) a combination of the methods (i) and (ii); Is mentioned.
- Examples of the inert gas used in the latter method include air, nitrogen, argon, helium, hydrogen, aliphatic hydrocarbons, and aromatic hydrocarbons.
- the flow rate of the inert gas is not particularly limited, but the space velocity in the apparatus is usually 1 to 200 h ⁇ 1 in terms of gas volume at the heating temperature.
- the method for bringing the cyclopentenes (cyclohexenes) into contact with the alcohol compound (2) in the presence of the acidic ion exchange resin A is not particularly limited.
- a method of adding acidic ion exchange resin A to a mixture of cyclopentenes (cyclohexenes) and alcohol compound (2) (hereinafter also referred to as “mixture”) and stirring the mixture (batch type), acidic ion exchange A method (flow type) in which the resin A is packed in a column and the mixture is circulated in the column (hereinafter referred to as “reaction column”) can be used.
- a flow type in which the resin A is packed in a column and the mixture is circulated in the column
- reaction column it is more preferable to adopt a flow type from the viewpoint of working efficiency and continuous purification of the reaction product.
- cyclopentenes (cyclohexenes) and alcohol compound (2) may be mixed at a predetermined ratio.
- a liquid mixture of cyclopentenes (cyclohexenes) and alcohol compound (2) can be prepared in advance, stored in a tank, and sent from the tank to the reaction column in a gaseous state.
- Cyclopentenes (Cyclohexenes) and the alcohol compound (2) are stored in separate tanks, from which the cyclopentenes (cyclohexenes) and the alcohol compound (2) are separately fed and immediately before entering the reaction column. Both can be mixed to form a gas state.
- the water content of the resulting mixture is preferably as low as possible in order to obtain the target product more efficiently, but is preferably 1% by mass or less, particularly preferably 500 ppm or less.
- a predetermined amount of acidic ion exchange resin A, cyclopentenes (cyclohexenes) and alcohol compound (2) are added to the reactor, and the reaction mixture is stirred at a predetermined temperature and a predetermined pressure.
- the amount of acidic ion exchange resin A used in this case is usually 0.01 to 200 parts by weight, preferably 0.1 to 150 parts by weight, more preferably 1 to 1 part by weight per 100 parts by weight of cyclopentenes (cyclohexenes). The range is 100 parts by weight.
- the use ratio of the cyclopentenes (cyclohexenes) and the alcohol compound (2) is not particularly limited, but it is preferable to use the alcohol compound (2) in excess.
- the use ratio of the cyclopentenes (cyclohexenes) and the alcohol compound (2) is usually 1/1 to 1/50, preferably in a molar ratio of [(cyclopentenes (cyclohexenes)) / (alcohol compound (2)). Is 1/1 to 1/30, more preferably 1/1 to 1/20.
- the mixture is circulated in the reaction column.
- a column having a heating device is used, and the mixture is circulated in a gaseous state in the reaction column heated to a predetermined temperature (reaction temperature).
- the mixed solution is fed from the mixed solution storage tank 1a, and the mixed solution is gasified by the heating / vaporization device 2a. And a method of feeding the reaction column 3a in a gaseous state.
- the size of the column to be used is not particularly limited, and various sizes can be selected and used depending on the reaction scale.
- the acidic ion exchange resin A filled in each column may be the same or different.
- a down flow type in which the mixture is circulated from the upper part of the reaction columns 3b and 3c.
- the up-flow type (not shown) may be used for circulating the mixture from the lower side of the reaction column. From the viewpoint of obtaining the desired product with a higher conversion and selectivity, the down flow method is preferred.
- the pressure when the mixture passes through the reaction column is usually in the range of normal pressure to 30 MPa, preferably normal pressure to 10 MPa, more preferably normal pressure to 5 MPa.
- the space velocity of the mixture in the case of employing a flow-type is generally 50 ⁇ 1000h -1, preferably in the range of 200 ⁇ 800h -1.
- reaction temperature, a distribution rate, etc. can be changed for every reaction column.
- the use ratio of the cyclopentenes (cyclohexenes) and the alcohol compound (2) is not particularly limited, but it is preferable to use the cyclopentenes (cyclohexenes) excessively.
- the cyclopentenes (cyclohexenes) do not polymerize.
- the alcohol compound (2) is used in excess, the amount of by-produced dialkyl ether is reduced. This is because it increases.
- the use ratio of cyclopentenes (cyclohexenes) to alcohol compound (2) is usually 1/3 to 20/1, preferably [cyclopentenes (cyclohexenes)] / (alcohol compound (2)) in a molar ratio. It is 1/3 to 10/1, more preferably 1/3 to 5/1, still more preferably 1/3 to 3/1.
- the target cycloalkyl alkyl ether compound can be isolated by a usual separation / purification method such as solvent extraction and distillation of the reaction solution. Distillation may be performed multiple times.
- the distillation apparatus for example, a known distillation apparatus such as a continuous rectification apparatus having a rectification column can be used. Further, as shown in FIG. 2, after the mixed liquid was circulated through the reaction column 3g filled with the acidic ion exchange resin A, the obtained reaction liquid was passed through the reaction column 3h, for example, filled with Raschig rings. Distillation can be carried out continuously by the distillation device 4. According to this method, the unreacted cyclopentenes (cyclohexenes) and the alcohol compound (2) can be returned to the reaction column 3g via the pipe 5 and used again for the reaction, and the target product can be obtained at a higher conversion rate. it can.
- cyclopentenes cyclohexenes
- the alcohol compound (2) can be returned to the reaction column 3g via the pipe 5 and used again for the reaction, and the target product can be obtained at a higher conversion rate. it can.
- the reaction can be carried out in the absence of a solvent, or can be carried out by dissolving the starting cyclopentenes or cyclohexenes and diluting with an inert solvent that is not mixed with water.
- solvent used examples include aliphatic saturated hydrocarbons such as n-butane, n-pentane, n-hexane, n-heptane, n-octane, n-nonane, and n-decane; benzene, toluene, ethylbenzene, xylene , Aromatic hydrocarbons such as anisole, cumene, nitrobenzene; cyclopentane, alkyl-substituted cyclopentanes, alkoxy-substituted cyclopentanes, nitro-substituted cyclopentanes, cyclohexane, alkyl-substituted cyclohexanes, alkoxy-substituted cyclohexanes, nitro-substituted cyclohexane , Cycloheptane, alkyl-substituted cycloheptanes,
- the amount of the diluent used is not particularly limited, and any amount can be selected as long as the reaction is not inhibited.
- the amount of the solvent used is usually 10 to 90% by volume, preferably 20 to 80% by volume, based on the total amount of the reaction solution.
- the target formula (1) can be obtained with high reaction efficiency even when there is little decrease in the catalyst activity over time and the raw material supply is increased.
- a cycloalkyl alkyl ether represented by R 1 —O—R 2 can be produced.
- R 1 represents the same meaning as described above, and R 2 has a cyclopentyl group or a substituent which may have a substituent derived from the used cyclopentenes or cyclohexenes. It is a cyclohexyl group that may be used.
- cyclopentyl group or cyclohexyl group alkylcyclopentyl group such as 2-methyl-cyclopentyl group, 3-ethyl-cyclohexyl group, 3-sec-butyl-cyclopentyl group, 2-t-butyl-cyclohexyl group, or alkylcyclohexyl A group; an alkoxycyclopentyl group or an alkoxycyclohexyl group such as a 3-methoxy-cyclopentyl group, a 3-ethoxy-cyclohexyl group, a 2-sec-butoxy-cyclopentyl group, a 3-t-butoxy-cyclohexyl group; a 3-methylthio-cyclopentyl group; Alkylthiocyclopentyl group such as 3-ethylthio-cyclohexyl group, 2-sec-butylthio-cyclopentyl group, 3-t-butylthio-cyclohexyl
- the water content was measured by the Karl Fischer coulometric titration method using a Hiranuma moisture measuring device (manufactured by Hiranuma Sangyo Co., Ltd., product number: AQ-7), and Hydranal R (manufactured by Sigma Aldrich) and Aqua Wright RS-A was used as a counter electrode solution using Aqualite CN (manufactured by Kanto Chemical Co., Inc.).
- Acidic ion exchange resin B (manufactured by Organo, trade name: Amberlyst Amberlyst-35, water content 55% by mass) Water content after dehydration 1.8% by mass Acidic ion exchange resin C (manufactured by Organo Corporation, trade name: Amberlyst Amberlyst-36, water content 55% by mass) Water content after dehydration 1.8% by mass Acidic ion exchange resin D (Mitsubishi Chemical Co., Ltd., trade name: Diaion RCP-160M, water content 47% by mass) Water content after dehydration 1.5% by mass Acidic ion exchange resin E (Made by Mitsubishi Chemical Co., Ltd., trade name: Diaion PK-228, water content 40% by mass) Water content after dehydration 1.3% by mass Acidic ion-exchange resin F (manufactured by LANXESS, trade name: Le
- Example 1 (Examples 2 and 3, Comparative Examples 1 to 3)
- the reaction was carried out in the same manner as in Example 1 except that the dehydrated acidic ion exchange resin used was changed to that shown in Table 1 below.
- the STY (kg / hr / m 3 ) of cyclopentyl methyl ether produced by each GHSV (h ⁇ 1 ) is shown in Table 1 below as in Example 1.
- FIG. 3 is a graph showing the relationship between GHSV (h ⁇ 1 ) and STY (kg / hr / m 3 ).
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Abstract
Description
しかしながら、これらの方法は、触媒活性の経時的な低下を抑制できる方法ではあるものの、反応効率や生産性の面で十分に満足のいく製造方法とはいえなかった。
〔1〕酸性イオン交換樹脂の存在下に、置換基を有していてもよいシクロペンテン、又は置換基を有していてもよいシクロヘキセンと、式(2):R1OH(式中、R1は置換基を有していてもよい炭素数1~10のアルキル基、又は置換基を有していてもよい炭素数3~8のシクロアルキル基を表す。)で表されるアルコール化合物を気体状態で反応させる、式(1):R1-O-R2(式中、R1は前記と同じ意味を表し、R2は、置換基を有していてもよいシクロペンチル基又は置換基を有していてもよいシクロヘキシル基を表す。)で表されるシクロアルキルアルキルエーテル化合物の製造方法において、
酸性イオン交換樹脂として、比表面積が20~50m2/gであり、平均孔径が20~70nmであり、且つ総交換容量が4.8~6.0eq/L-R湿潤樹脂であるものを用いるシクロアルキルアルキルエーテル化合物の製造方法。
〔3〕前記イオン交換樹脂の比表面積が35~45m2/gである〔1〕又は〔2〕に記載のシクロアルキルアルキルエーテル化合物の製造方法。
〔4〕前記イオン交換樹脂の総交換容量が5.0~5.5eq/L-R湿潤樹脂である〔1〕~〔3〕いずれかに記載のシクロアルキルアルキルエーテル化合物の製造方法。
本発明の製造方法によれば、目的とするシクロアルキルアルキルエーテル化合物を工業的に有利に製造することができる。
本発明のシクロアルキルアルキルエーテル化合物の製造方法は、酸性イオン交換樹脂の存在下に、置換基を有していてもよいシクロペンテン、又は置換基を有していてもよいシクロヘキセンと、式(2):R1OHで表されるアルコール化合物(以下、「アルコール化合物(2)」ということがある。)とを気体状態で反応させる、式(1):R1-O-R2で表されるシクロアルキルアルキルエーテル化合物の製造方法において、酸性イオン交換樹脂として、比表面積が20~50m2/gであり、平均孔径が20~70nmであり、且つ総交換容量が4.8~6.0eq/L-R湿潤樹脂であるものを用いることを特徴とする。
本発明に用いる置換基を有していてもよい(シクロペンテン又はシクロヘキセン)の置換基としては、メチル基、エチル基、n-プロピル基、イソプロピル基、n-ブチル基、t-ブチル基、sec-ブチル基、イソブチル基等の炭素数1~4のアルキル基;メトキシ基、エトキシ基、n-プロポキシ基、sec-プロポキシ基、n-ブトキシ基、t-ブトキシ基、sec-ブトキシ基等の炭素数1~4のアルコキシ基;メチルチオ基、エチルチオ基、n-プロピルチオ基、sec-ブチルチオ基、t-ブチルチオ基等の炭素数1~4のアルキルチオ基;フッ素原子、塩素原子、臭素原子、ヨウ素原子等のハロゲン原子;フェニル基等のアリール基;等が挙げられる。これらの中でも、炭素数1~4のアルキル基が好ましく、メチル基又はエチル基が特に好ましい。
これらの中でも、シクロペンテン又はシクロヘキセンが好ましく、シクロペンテンが特に好ましい。
酸性イオン交換樹脂は、微細な三次元網目構造の高分子基体に酸性のイオン交換基を有する不溶性で多孔質の合成樹脂からなり、一般的に陽イオン交換樹脂と称されるものである。
また、酸性イオン交換樹脂は、幾何学的構造面からの分類としてゲル型、ポーラス型、ハイポーラス型に大別することができるが、本発明においてはいずれの型のものも使用することができる。
このような酸性イオン交換樹脂(以下、「酸性イオン交換樹脂A」ということがある。)を用いることで、触媒活性の経時的な低下が少なく、かつ、原料供給を大きくした場合であっても、高い反応効率で目的とするシクロアルキルアルキルエーテルを製造することができる。
平均孔径とは、細孔の孔径(nm)の平均値をいう。
総交換容量とは、湿潤状態(樹脂はこの状態での市販が普通)の単位樹脂量あたりのイオン交換にかかわる全部のイオン交換基数をいう。本願においては、酸性イオン交換樹脂1Lあたりの当量、すなわち「eq/L-R」で表す(Rは湿潤樹脂を示す。)。
本発明に用いる酸性イオン交換樹脂の好ましい具体例としては、商品名:CT276(ピューロライト社製)、商品名:アンバリスト35、アンバリスト36(オルガノ社製)等が挙げられる。
なお、式(1)中、R1は前記と同じ意味を表し、R2は、用いたシクロペンテン類又はシクロヘキセン類由来の、置換基を有していてもよいシクロペンチル基又は置換基を有していてもよいシクロヘキシル基である。
具体的には、シクロペンチル基又はシクロヘキシル基;2-メチル-シクロペンチル基、3-エチル-シクロヘキシル基、3-sec-ブチル-シクロペンチル基、2-t-ブチル-シクロヘキシル基等のアルキルシクロペンチル基又はアルキルシクロヘキシル基;3-メトキシ-シクロペンチル基、3-エトキシ-シクロヘキシル基、2-sec-ブトキシ-シクロペンチル基、3-t-ブトキシ-シクロヘキシル基等のアルコキシシクロペンチル基又はアルコキシシクロヘキシル基;3-メチルチオ-シクロペンチル基、3-エチルチオ-シクロヘキシル基、2-sec-ブチルチオ-シクロペンチル基、3-t-ブチルチオ-シクロヘキシル基等のアルキルチオシクロペンチル基又はアルキルチオシクロヘキシル基;2-クロロ-シクロペンチル基、3-クロロ-シクロペンチル基、2-ブロモ-シクロヘキシル基、3-ブロモ-シクロヘキシル基等のハロゲン化シクロペンチル基又はハロゲン化シクロヘキシル基;等である。
市販の酸性イオン交換樹脂A(ピューロライト社製、商品名:CT276、含水量55質量%)500mLをガラスカラムに充填し、水含有量50ppmの脱水メチルアルコール5LをLHSV〔触媒単位容積当たりの液体流入速度〕2h-1で、ガラスカラムにダウンフローで流通させてイオン交換樹脂を洗浄した。さらに純窒素1Lをガラスカラムにダウンフローで流通させて樹脂粒子間に滞留しているメチルアルコールを除去した。この脱水したイオン交換樹脂の含水量をカールフィッシャー電量滴定法で測定したところ、1.8質量%であった。得られた酸性イオン交換樹脂(以下、「脱水酸性イオン交換樹脂A」という。)を反応に使用した。
・酸性イオン交換樹脂B(オルガノ社製、商品名:アンバリストAmberlyst-35、含水量55質量%)脱水処理後の含水量1.8質量%
・酸性イオン交換樹脂C(オルガノ社製、商品名:アンバリストAmberlyst-36、含水量55質量%)脱水処理後の含水量1.8質量%
・酸性イオン交換樹脂D(三菱化学社製、商品名:ダイヤイオンRCP-160M、含水量47質量%)脱水処理後の含水量1.5質量%
・酸性イオン交換樹脂E(三菱化学社製、商品名:ダイヤイオンPK-228、含水量40質量%)脱水処理後の含水量1.3質量%
・酸性イオン交換樹脂F(ランクセス社製、商品名:レバチットK 2621、含水量50質量%(旧バイエル社製、商品名:SPC118))脱水処理後の含水量1.6質量%
図1(a)に示す反応装置を使用して、次の実験を行った。
直径2.54cm、長さ20cmのSUS製の反応カラム3aに、製造例1で得られた脱水酸性イオン交換樹脂Aを72ml充填し、カラム3aの全体を90℃に保温した。
一方、シクロペンテン及びメタノールの混合液(混合モル比:シクロペンテン/メタノール=1.6/1)を貯蔵したタンク1から送液し、加熱・気化装置2aにより90℃に加熱・気化させて、常圧、90℃、GHSVが220~460h-で、反応カラム3a内に連続的に送りこんだ。反応開始から1時間経過後、反応カラム3aの一方の出口から流出する反応液を、ガスクロマトグラフィーにより分析した。
GHSV(h-1)を変化させて生成した、シクロペンチルメチルエーテルのSTY(kg/hr/m3)を下記表1に示す。
実施例1において、使用する脱水酸性イオン交換樹脂を下記表1に記載のものに変更した他は、実施例1と同様にして反応を行った。各GHSV(h-1)により生成した、シクロペンチルメチルエーテルのSTY(kg/hr/m3)を実施例1と同様に下記表1に示す。
また、GHSV(h-1)とSTY(kg/hr/m3)との関係を示すグラフ図を図3に示す。
実施例1~3では、GHSV(h-1)が大きくなっても高い反応性を示す(STY(kg/hr/m3)の値は75~154)ことが分かる。
一方、本発明の要件を満たしていない酸性イオン交換樹脂を使用した比較例では、比較例1は、流速が小さいときの反応性に差はないが、流速が大きくなると反応性が小さくなり、比較例2及び3は、流速が小さいときでも反応性が小さいことが分かる。
2a、2b、2c、2d・・・加熱・気化装置
3a、3b、3c、3d、3e、3f、3g、3h・・・反応カラム
4・・・蒸留装置
5・・・配管
Claims (5)
- 酸性イオン交換樹脂の存在下に、置換基を有していてもよいシクロペンテン、又は置換基を有していてもよいシクロヘキセンと、式(2):R1OH(式中、R1は置換基を有していてもよい炭素数1~10のアルキル基、又は置換基を有していてもよい炭素数3~8のシクロアルキル基を表す。)で表されるアルコール化合物を気体状態で反応させる、式(1):R1-O-R2(式中、R1は前記と同じ意味を表し、R2は置換基を有していてもよいシクロペンチル基又は置換基を有していてもよいシクロヘキシル基を表す。)で表されるシクロアルキルアルキルエーテル化合物の製造方法において、
酸性イオン交換樹脂として、比表面積が20~50m2/gであり、平均孔径が20~70nmであり、且つ総交換容量が4.8~6.0eq/L-R湿潤樹脂であるものを用いるシクロアルキルアルキルエーテル化合物の製造方法。 - 前記式(1)におけるR1が炭素数1~10のアルキル基であり、R2がシクロペンチル基である請求項1記載のシクロアルキルアルキルエーテル化合物の製造方法。
- 前記酸性イオン交換樹脂の比表面積が、35~45m2/gである請求項1に記載のシクロアルキルアルキルエーテル化合物の製造方法。
- 前記酸性イオン交換樹脂の総交換容量が、5.0~5.5eq/L-R湿潤樹脂である請求項1に記載のシクロアルキルアルキルエーテル化合物の製造方法。
- 前記酸性イオン交換樹脂の水含有量が、5質量%以下である請求項1に記載のシクロアルキルアルキルエーテル化合物の製造方法。
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