WO2014109232A1 - ポリヒドロキシ不飽和炭化水素系重合体水素化物の製造方法 - Google Patents
ポリヒドロキシ不飽和炭化水素系重合体水素化物の製造方法 Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F136/00—Homopolymers of compounds having one or more unsaturated aliphatic radicals, at least one having two or more carbon-to-carbon double bonds
- C08F136/02—Homopolymers of compounds having one or more unsaturated aliphatic radicals, at least one having two or more carbon-to-carbon double bonds the radical having only two carbon-to-carbon double bonds
- C08F136/04—Homopolymers of compounds having one or more unsaturated aliphatic radicals, at least one having two or more carbon-to-carbon double bonds the radical having only two carbon-to-carbon double bonds conjugated
- C08F136/06—Butadiene
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08C—TREATMENT OR CHEMICAL MODIFICATION OF RUBBERS
- C08C19/00—Chemical modification of rubber
- C08C19/02—Hydrogenation
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F36/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, at least one having two or more carbon-to-carbon double bonds
- C08F36/02—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, at least one having two or more carbon-to-carbon double bonds the radical having only two carbon-to-carbon double bonds
- C08F36/04—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, at least one having two or more carbon-to-carbon double bonds the radical having only two carbon-to-carbon double bonds conjugated
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F8/00—Chemical modification by after-treatment
- C08F8/04—Reduction, e.g. hydrogenation
Definitions
- the present invention relates to a method for producing a hydride of a polyhydroxy unsaturated hydrocarbon polymer. More specifically, the present invention relates to a method for producing a hydride of a polyhydroxy unsaturated hydrocarbon polymer capable of suppressing a side reaction such as a hydrogenolysis reaction of a terminal hydroxyl group and achieving a high hydrogenation rate in a short reaction time.
- a side reaction such as a hydrogenolysis reaction of a terminal hydroxyl group and achieving a high hydrogenation rate in a short reaction time.
- a so-called terminal hydroxyl group-modified polybutadiene hydride in which a hydroxyl group is bonded to the end of the main chain of polybutadiene hydride is known.
- This terminal hydroxyl group-modified polybutadiene hydride can be obtained by hydrogenating the main chain or side chain carbon-carbon double bond in the terminal hydroxyl group-modified polybutadiene.
- Patent Document 1 discloses that polyhydroxypolybutadiene was hydrogenated in the presence of a carbon-supported ruthenium catalyst or an alumina-supported ruthenium catalyst at 100 ° C. while maintaining an internal pressure of 50 mg / cm 2 (about 4.9 Pa). Is described.
- the reaction temperature for example, 120 ° C.
- An object of the present invention is to provide a method for producing a hydride of a polyhydroxy unsaturated hydrocarbon polymer capable of suppressing a side reaction such as a hydrogenolysis reaction of a terminal hydroxyl group and achieving a high hydrogenation rate in a short reaction time. That is.
- the present inventors conducted a hydrogenation reaction until a hydrogenation rate of 30 mol% or more was reached in a temperature range of 80 ° C. to 130 ° C., and then 98 mol at a temperature higher than 130 ° C. It has been found that the above problem can be solved by a method including performing a hydrogenation reaction until a hydrogenation rate of at least% is reached, and the present invention has been completed.
- this invention includes the following forms.
- the hydrogenation catalyst is at least one selected from the group consisting of a nickel-based catalyst, a cobalt-based catalyst, a ruthenium-based catalyst, a rhodium-based catalyst, a palladium-based catalyst, and a platinum-based catalyst [1] to [3] The method as described in any one of.
- a hydride of a polyhydroxy unsaturated hydrocarbon polymer can be produced at a high hydrogenation rate while suppressing side reactions.
- the polyhydroxy unsaturated hydrocarbon polymer used in the present invention has a carbon-carbon double bond in the main chain or side chain of the molecule, and has an average of 0.5 or more hydroxyl groups in the molecule. It is a hydrocarbon polymer.
- the polyhydroxy unsaturated hydrocarbon polymer can be produced by various methods. For example, a conjugated diene monomer alone, a mixture of two or more conjugated diene monomers, or a mixture of a conjugated diene monomer and another monomer copolymerizable therewith 1) Polymerized using hydrogen peroxide as a reaction initiator 2) a method of polymerizing using another initiator, for example, an azobisisonitrile compound having a functional group, and 3) an alkali metal such as sodium or lithium, or an alkali metal and a polycyclic aroma
- An anion polymerization using a complex with a group compound as a catalyst, followed by a reaction with an alkylene oxide, epichlorohydrin or the like, and a treatment with a protonic acid such as hydrochloric acid, sulfuric acid or acetic acid can be used.
- examples of the raw material conjugated diene monomer include 1,3-butadiene, isoprene, 1,3-pentadiene, chloroprene, and the other copolymerizable monomers include styrene, acrylonitrile, acrylic acid, Examples include methacrylic acid, acrylic acid alkyl ester, and methacrylic acid alkyl ester.
- Specific examples of the polymer obtained by the above method include polyhydroxypolybutadiene, polyhydroxypolyisoprene, polyhydroxypoly1,3-pentadiene, and the above copolymers having a hydroxy group. Of these, polybutadiene having hydroxyl groups at both ends is preferred.
- the polyhydroxy unsaturated hydrocarbon polymer used in the present invention may be composed of only 1,4-bonds or only 1,2-bonds. It is preferable that a compound composed of the above (1,4-bond unit) and a compound composed of 1,2-bond (1,2-bond unit) coexist.
- the molar ratio of 1,2-bond units / 1,4-bond units is not particularly limited, but is preferably 45/55 to 95/5, more preferably 50/50 to 90/10.
- the polyhydroxy unsaturated hydrocarbon polymer used in the present invention preferably has a number average molecular weight of 300 to 10,000, more preferably 500 to 6,000.
- the number of hydroxyl groups contained in the polyhydroxy unsaturated hydrocarbon polymer is preferably 50 KOHmg / g or more, more preferably 60 KOHmg / g or more, as a hydroxyl value.
- a commercially available polyhydroxy unsaturated hydrocarbon polymer can be used.
- NISSO-PB-G-1000 manufactured by Nippon Soda Co., Ltd.
- NISSO-PB-G-2000 manufactured by Nippon Soda Co., Ltd.
- NISSO-PB-G-3000 manufactured by Nippon Soda Co., Ltd.
- PoIy bd R45HT Idemitsu Kosan Co., Ltd.
- the hydrogenation catalyst used in the present invention is not particularly limited as long as it is a catalyst for smoothly performing a hydrogenation reaction of a polyhydroxy unsaturated hydrocarbon polymer.
- the hydrogenation catalyst that can be used in the present invention include nickel-based catalysts, cobalt-based catalysts, ruthenium-based catalysts, rhodium-based catalysts, palladium-based catalysts, platinum-based catalysts, and mixtures or alloy-based catalysts thereof. Of these, nickel-based catalysts and ruthenium-based catalysts are preferable from the viewpoint that hydroxyl group hydrogenolysis hardly occurs.
- hydrogenation catalysts can be used alone, as a solid or soluble homogeneous complex, or as a carrier-supported type supported on a carrier such as carbon, silica, or diatomaceous earth. Of these, a catalyst supported on a diatomaceous earth support is preferred. Furthermore, as the hydrogenation catalyst, in addition to the above metal catalyst, a metal complex obtained by reducing a compound containing nickel, titanium, cobalt and the like with an organometallic compound (for example, trialkylaluminum, alkyllithium, etc.) can also be used.
- organometallic compound for example, trialkylaluminum, alkyllithium, etc.
- the amount of the hydrogenation catalyst used in the method of the present invention is preferably 0.01 to 20% by weight with respect to the polyhydroxy unsaturated hydrocarbon polymer, although it varies depending on the kind of metal and the amount supported. .
- the hydrogenation catalyst may be attached to the reactor as a fixed bed or suspended in the reaction solvent.
- reaction solvent used in the present invention various conventionally used organic solvents are used.
- organic solvent include hexane, heptane, octane, nonane, decane, cyclohexane, methylcyclohexane, isoparaffin, benzene, toluene, xylene, trimethylbenzene, solvent naphtha and other hydrocarbons; n-propyl alcohol, isopropyl alcohol, n-butyl.
- Examples include alcohols such as alcohols; ethers such as diethyl ether, dipropyl ether and tetrahydrofuran; esters such as ethyl acetate and butyl acetate; or mixed solvents composed of any combination thereof. It is not limited to things.
- the amount of the reaction solvent used in the method of the present invention is not particularly limited, but is preferably 30 to 300 parts by weight with respect to 100 parts by weight of the polyhydroxy unsaturated hydrocarbon polymer.
- the hydrogen used in the present invention is not particularly limited as long as it does not contain a component that becomes a catalyst poison.
- the hydrogenation reaction is performed in at least two stages.
- the stage (I) is a stage from the start of the hydrogenation reaction to a predetermined hydrogenation rate or higher.
- the predetermined hydrogenation rate is 30 mol%, preferably 40 mol%, more preferably 60 mol%, and most preferably 85 mol%.
- the upper limit of the predetermined hydrogenation rate that is the end point of the stage (I) is preferably 97 mol%. If the hydrogenation rate as the end point of stage (I) is set too low, the ratio of occurrence of hydrogenolysis reaction of hydroxyl groups and thermal polymerization of unsaturated bonds in stage (II) increases, and polyhydroxy unsaturated hydrocarbon system There is a tendency for the hydroxyl value of the polymer hydride to decrease.
- A is the number of moles of monomer unit units hydrogenated in the polyhydroxy unsaturated hydrocarbon polymer hydride
- B is the total number of hydrogen contained in the polyhydroxy unsaturated hydrocarbon polymer hydride.
- the number of moles of monomer unit. A and B are calculated by 1 H-NMR integration ratio.
- the temperature is maintained in the range of 80 to 130 ° C., preferably 100 to 130 ° C., more preferably 120 to 130 ° C.
- the reaction temperature is lowered, the hydrogenation reaction does not proceed or the reaction tends to become extremely slow.
- the reaction temperature in the stage (I) increases, the rate at which the thermal polymerization reaction (side reaction) between the polyhydroxy unsaturated hydrocarbon polymers proceeds tends to increase.
- the hydrogen pressure is preferably adjusted to 6 MPa or less, more preferably 4 MPa or less, and further preferably 2 MPa or less by introducing hydrogen gas.
- the lower limit of the hydrogen pressure is preferably 0.2 MPa.
- the stage (II) is a stage from the predetermined hydrogenation rate until the hydrogenation rate becomes 98% or more.
- the step (II) may be performed in the reactor used in the step (I), or may be performed by transferring the reaction solution to a reactor different from the reactor used in the step (I). It is preferable from the viewpoint of production efficiency that the step (I) and the step (II) are performed without interruption.
- the temperature is higher than 130 ° C, preferably 140 ° C or higher.
- the upper limit of the temperature in the stage (II) is 190 ° C.
- the hydrogen pressure is preferably adjusted to 2 MPa or more, more preferably 4 MPa or more, and further preferably 6 MPa or more by introducing hydrogen gas.
- the upper limit of the hydrogen pressure is determined by the pressure limit of the reactor, but is preferably 10 MPa.
- the product polyhydroxy unsaturated hydrocarbon polymer hydride can be isolated and purified according to a known method.
- the hydrogenation catalyst when the hydrogenation catalyst is suspended in the reaction solvent, the liquid containing the reaction product can be filtered to recover the hydrogenation catalyst.
- the recovered hydrogenation catalyst can be regenerated by a known method and reused in a hydrogenation reaction or the like.
- the reaction solvent can be removed by isolating the liquid containing the reaction product by thin film drying, vacuum drying, or the like, and the product can be isolated.
- Hydroxyl value This is the number of mg of potassium hydroxide required to acetylate the OH group contained in 1 g of the sample. It measured by the method based on JISK0070: 1992. The ratio of the hydroxyl value after hydrogenation to the hydroxyl value before hydrogenation was defined as the hydroxyl group retention.
- Iodine number This is a value obtained by converting the amount of halogen that reacts with 100 grams of the sample into grams of iodine. It measured by the method based on JISK0070: 1992.
- Example 1 In an autoclave having a capacity of 0.98 liter equipped with a heater for heating, a stirring mechanism and a thermometer, 12.01 g of nickel catalyst supported on diatomaceous earth was charged and purged with nitrogen. To this was added 250 g of a 60 wt% octane solution of terminal hydroxyl group-modified polybutadiene (“G-1000” manufactured by Nippon Soda Co., Ltd., number average molecular weight: 1400). Next, hydrogen gas was pressurized and sealed in the autoclave until the pressure became 2.0 MPa. The hydrogenation reaction was performed while maintaining the temperature at 120 to 130 ° C. Hydrogen gas was consumed by the reaction, and the hydrogen pressure in the autoclave dropped to 0.2 MPa.
- G-1000 60 wt% octane solution of terminal hydroxyl group-modified polybutadiene
- the temperature inside the autoclave was raised to 165 ° C. Hydrogen gas was pressurized and sealed until the hydrogen pressure in the autoclave reached 9.2 MPa. The hydrogenation reaction was carried out for 3 hours while maintaining the temperature at 165 ° C. Hydrogen gas was consumed by the reaction, and the hydrogen pressure in the autoclave became 8.3 MPa.
- the autoclave was cooled to room temperature. The liquid containing the reaction product was filtered to remove the hydrogenation catalyst.
- the obtained terminal hydroxyl group-modified polybutadiene hydride had a hydrogenation rate of 99%, an iodine value of 13.8 Ig / 100 g, a hydroxyl value of 64.3 KOHmg / g, and a hydroxyl value retention of 90.4%.
- Example 2 A terminal hydroxyl group-modified polybutadiene hydride was obtained in the same manner as in Example 1 except that the hydrogen pressure in the hydrogen enclosure after raising the temperature in the autoclave to 165 ° C. was changed to 6.4 MPa.
- the obtained terminal hydroxyl group-modified polybutadiene hydride had a hydrogenation rate of 99%, an iodine value of 14.9 Ig / 100 g, a hydroxyl value of 64.0 KOHmg / g, and a hydroxyl value retention of 90.0%.
- Example 3 In an autoclave having a capacity of 0.98 liter equipped with a heater for heating, a stirring mechanism, and a thermometer, 12.01 g of a diatomaceous earth-supported nickel catalyst was charged and purged with nitrogen. To this was added 250 g of a 60 wt% octane solution of terminal hydroxyl group-modified polybutadiene (“G-1000” manufactured by Nippon Soda Co., Ltd., number average molecular weight: 1400). Next, hydrogen gas was pressurized and sealed in the autoclave until the pressure became 2.0 MPa. The hydrogenation reaction was performed while maintaining the temperature at 120 to 130 ° C.
- G-1000 60 wt% octane solution of terminal hydroxyl group-modified polybutadiene
- the obtained terminal hydroxyl group-modified polybutadiene hydride had a hydrogenation rate of 99%, an iodine value of 15.1 Ig / 100 g, a hydroxyl value of 63.4 KOHmg / g, and a hydroxyl value retention of 89.2%.
- Example 4 In an autoclave having a capacity of 0.98 liter equipped with a heater for heating, a stirring mechanism, and a thermometer, 12.01 g of a diatomaceous earth-supported nickel catalyst was charged and purged with nitrogen. To this was added 250 g of a 60 wt% octane solution of terminal hydroxyl group-modified polybutadiene (“G-1000” manufactured by Nippon Soda Co., Ltd., number average molecular weight: 1400). Next, hydrogen gas was pressurized and sealed in the autoclave until the pressure became 2.0 MPa. The hydrogenation reaction was performed while maintaining the temperature at 120 to 130 ° C. Hydrogen gas was consumed by the reaction, and the hydrogen pressure in the autoclave dropped to 0.2 MPa.
- G-1000 60 wt% octane solution of terminal hydroxyl group-modified polybutadiene
- the obtained terminal hydroxyl group-modified polybutadiene hydride had a hydrogenation rate of 99%, an iodine value of 13.9 Ig / 100 g, a hydroxyl value of 62.1 KOHmg / g, and a hydroxyl value retention of 87.3%.
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Abstract
Description
本願は、2013年1月10日に、日本に出願された特願2013-002503号に基づき優先権を主張し、その内容をここに援用する。
〔1〕 水素雰囲気にて、ポリヒドロキシ不飽和炭化水素系重合体を、水素化触媒および反応溶媒の存在下、
(I)80℃~130℃の温度範囲で水素化率30mol%以上となるまで水素化反応を行い、
(II)その後、130℃より高い温度で水素化率98mol%以上となるまで水素化反応を行うことを含むポリヒドロキシ不飽和炭化水素系重合体水素化物の製造方法。
〔2〕(I)の段階における水素圧力が6MPa以下である〔1〕に記載の方法。
〔3〕(II)の段階における水素圧力が2MPa以上である〔1〕または〔2〕に記載の方法。
〔4〕水素化触媒が、ニッケル系触媒、コバルト系触媒、ルテニウム系触媒、ロジウム系触媒、パラジウム系触媒、および白金系触媒からなる群から選ばれる少なくとも1つである〔1〕~〔3〕のいずれかひとつに記載の方法。
本発明に用いられるポリヒドロキシ不飽和炭化水素系重合体は、分子の主鎖または側鎖に炭素-炭素二重結合を有し、かつ、その分子中に平均0.5個以上の水酸基を有する炭化水素系重合体である。
上記方法で得られる重合体の具体例としては、ポリヒドロキシポリブタジエン、ポリヒドロキシポリイソプレン、ポリヒドロキシポリ1,3-ペンタジエン、およびヒドロキシ基を有する上記各共重合体等が挙げられる。これらのうち、両末端に水酸基を有するポリブタジエンが好ましい。本発明に用いられるポリヒドロキシ不飽和炭化水素系重合体は1,4-結合のみで構成されたものまたは1,2-結合のみで構成されたものであってもよいが、1,4-結合で構成されたもの(1,4-結合ユニット)と1,2-結合で構成されたもの(1,2-結合ユニット)とが共存するものであることが好ましい。1,2-結合ユニット/1,4-結合ユニットのモル比は、特に限定されないが、好ましくは45/55~95/5、より好ましくは50/50~90/10である。また、本発明に用いられるポリヒドロキシ不飽和炭化水素系重合体は、数平均分子量が好ましくは300~10000、より好ましくは500~6000である。ポリヒドロキシ不飽和炭化水素系重合体に含まれる水酸基の数は、水酸基価として、好ましくは50KOHmg/g以上、より好ましくは60KOHmg/g以上である。
水素化率(mol%)=(A/B)×100
式中、Aは、ポリヒドロキシ不飽和炭化水素系重合体水素化物中の水素化されているモノマー単位ユニットのモル数、Bは、ポリヒドロキシ不飽和炭化水素系重合体水素化物中に含まれる全モノマー単位ユニットのモル数である。AおよびBは1H-NMRの積分比によって算出する。
試料1g中に含まれるOH基をアセチル化するために要する水酸化カリウムのmg数である。JIS K 0070:1992に準拠した方法で測定した。水素化前の水酸基価に対する水素化後の水酸基価との比率を水酸基保持率と定義した。
(ヨウ素価)
試料100グラムと反応するハロゲンの量をヨウ素のグラム数に換算した値である。JIS K 0070:1992に準拠した方法で測定した。
加温用ヒーター、攪拌機構および温度計を備えた容量0.98リットルのオートクレーブに、珪藻土担持ニッケル触媒12.01gを仕込み、窒素置換した。これに末端水酸基変性ポリブタジエン(「G-1000」日本曹達社製、数平均分子量:1400)の60重量%オクタン溶液250gを加えた。
次に、このオートクレーブ内に水素ガスを2.0MPaとなるまで加圧封入した。120~130℃に維持して水素化反応を行った。反応によって水素ガスが消費され、オートクレーブ内の水素圧力が0.2MPaまで下がった。
0.2MPになった時点で、水素ガスを2.0MPaとなるまで加圧封入した。この操作を水素化率が84%となるまで繰り返した。所要時間は15時間であった。この段階で得られた生成物の水酸基価は63.2KOHmg/gであった。
オートクレーブを室温まで冷却した。反応生成物を含む液を濾過して水素化触媒を除去した。得られた末端水酸基変性ポリブタジエン水素化物は、水素化率が99%、ヨウ素価が13.8Ig/100g、水酸基価が64.3KOHmg/g、水酸基価保持率が90.4%であった。
オートクレーブ内を165℃に昇温した後の水素封入の水素圧力を6.4MPaに変えた以外は実施例1と同じ方法で末端水酸基変性ポリブタジエン水素化物を得た。得られた末端水酸基変性ポリブタジエン水素化物は、水素化率が99%、ヨウ素価が14.9Ig/100g、水酸基価が64.0KOHmg/g、水酸基価保持率が90.0%であった。
加温用ヒーター、攪拌機構および温度計を備えた容量0.98リットルのオートクレーブに、珪藻土担持ニッケル触媒12.01gを仕込み窒素置換した。これに末端水酸基変性ポリブタジエン(「G-1000」日本曹達社製、数平均分子量:1400)の60重量%オクタン溶液250gを加えた。
次に、オートクレーブ内に水素ガスを2.0MPaとなるまで加圧封入した。120~130℃に維持して水素化反応を行った。反応によって水素ガスが消費され、オートクレーブ内の水素圧力が0.2MPaまで下がった。
0.2MPaになった時点で、水素ガスを2.0MPaとなるまで加圧封入した。この操作を水素化率が32%となるまで繰り返した。所要時間は5時間であった。この段階で得られた生成物の水酸基価は65.8KOHmg/gであった。
オートクレーブを室温まで冷却した。反応生成物を含む液をろ過して水素化触媒を除去した。得られた末端水酸基変性ポリブタジエン水素化物は、水素化率が99%、ヨウ素価が15.1Ig/100g、水酸基価が63.4KOHmg/g、水酸基価保持率が89.2%であった。
加温用ヒーター、攪拌機構および温度計を備えた容量0.98リットルのオートクレーブに、珪藻土担持ニッケル触媒12.01gを仕込み窒素置換した。これに末端水酸基変性ポリブタジエン(「G-1000」日本曹達社製、数平均分子量:1400)の60重量%オクタン溶液250gを加えた。
次に、オートクレーブ内に水素ガスを2.0MPaとなるまで加圧封入した。120~130℃に維持して水素化反応を行った。反応によって水素ガスが消費され、オートクレーブ内の水素圧力が0.2MPaまで下がった。
0.2MPaになった時点で、水素ガスを2.0MPaとなるまで加圧封入した。この操作を水素化率が34%となるまで繰り返した。所要時間は5時間であった。この段階で得られた生成物の水酸基価は67.3KOHmg/gであった。
165℃に達した時点で、オートクレーブ内の水素圧力が7.8MPaとなるまで水素ガスを加圧封入した。温度を165℃に維持して3時間水素化反応を行った。反応によって水素ガスが消費され、オートクレーブ内の水素圧力が5.7MPaになった。
オートクレーブを室温まで冷却した。反応生成物を含む液をろ過して水素化触媒を除去した。得られた末端水酸基変性ポリブタジエン水素化物は、水素化率が99%、ヨウ素価が13.9Ig/100g、水酸基価が62.1KOHmg/g、水酸基価保持率が87.3%であった。
加温用ヒーター、攪拌機構および温度計を備えた容量0.98リットルのオートクレーブに、珪藻土担持ニッケル触媒12.01gを仕込み窒素置換した。これに末端水酸基変性ポリブタジエン(「G-1000」日本曹達社製、数平均分子量:1400)の60重量%オクタン溶液250gを加えた。
次に、オートクレーブ内に水素ガスを2.0MPaとなるまで加圧封入した。120~130℃に維持して水素化反応を行った。反応によって水素ガスが消費され、オートクレーブ内の水素圧力が0.2MPaまで下がった。
0.2MPaになった時点で、水素ガスを2.0MPaとなるまで加圧封入した。この操作を水素化率が96%となるまで繰り返した。所要時間は15時間であった。
オートクレーブを室温まで冷却した。反応生成物を含む液をろ過して水素化触媒を除去した。得られた末端水酸基変性ポリブタジエン水素化物は、水素化率が96%、ヨウ素価が30.7Ig/100g、水酸基価が65.5KOHmg/g、水酸基価保持率が92.1%であった。
加温用ヒーター、攪拌機構および温度計を備えた容量0.98リットルのオートクレーブに、珪藻土担持ニッケル触媒12.01gを仕込み窒素置換した。これに末端水酸基変性ポリブタジエン(「G-1000」日本曹達社製、数平均分子量:1400)の60重量%オクタン溶液250gを加えた。
次に、オートクレーブ内に水素ガスを2.0MPaとなるまで加圧封入した。140~150℃に維持して水素化反応を行った。反応によって水素ガスが消費され、系内の水素圧力が0.2MPaまで下がった。
0.2MPaになった時点で、水素ガスを2.0MPaとなるまで加圧封入した。この操作を水素化率が98%となるまで繰り返した。所要時間は15時間であった。
オートクレーブを室温まで冷却した。反応生成物を含む液をろ過して水素化触媒を除去した。得られた末端水酸基変性ポリブタジエン水素化物は、水素化率が98%、ヨウ素価が20.8Ig/100g、水酸基価が61.8KOHmg/g、水酸基価保持率が86.9%であった。
これに対して、本発明の方法によれば、水酸基価をほとんど低下させずに、短い反応時間で高い水素化率にすることができる。
Claims (4)
- 水素雰囲気にて、ポリヒドロキシ不飽和炭化水素系重合体を、水素化触媒および反応溶媒の存在下、
(I)80℃~130℃の温度範囲で水素化率30mol%以上となるまで水素化反応を行い、
(II)その後、130℃より高い温度で水素化率98mol%以上となるまで水素化反応を行うことを含むポリヒドロキシ不飽和炭化水素系重合体水素化物の製造方法。 - (I)の段階における水素圧力が6MPa以下である請求項1に記載の方法。
- (II)の段階における水素圧力が2MPa以上である請求項1または2に記載の方法。
- 水素化触媒が、ニッケル系触媒、コバルト系触媒、ルテニウム系触媒、ロジウム系触媒、パラジウム系触媒、および白金系触媒からなる群から選ばれる少なくとも1つである請求項1~3のいずれかひとつに記載の方法。
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US14/758,872 US9487605B2 (en) | 2013-01-10 | 2013-12-25 | Method for producing hydrogenated unsaturated polyhydroxyhydrocarbon polymer |
CN201380069385.0A CN104918970B (zh) | 2013-01-10 | 2013-12-25 | 多羟基不饱和烃系聚合物氢化物的制造方法 |
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