JPS5841832A - Preparation of magnesium dialkoxide - Google Patents
Preparation of magnesium dialkoxideInfo
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- JPS5841832A JPS5841832A JP13983281A JP13983281A JPS5841832A JP S5841832 A JPS5841832 A JP S5841832A JP 13983281 A JP13983281 A JP 13983281A JP 13983281 A JP13983281 A JP 13983281A JP S5841832 A JPS5841832 A JP S5841832A
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- magnesium
- alcohol
- saturated hydrocarbon
- added
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Abstract
Description
【発明の詳細な説明】
本発明はマグネシウムジアルコキシドの製造方法に関し
、詳しくは粒子状で高純度のマグネシウムジアルコキシ
ドを効率よく製造する方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for producing magnesium dialkoxide, and more particularly to a method for efficiently producing particulate, highly pure magnesium dialkoxide.
従来からアルコールと金属マグネシウムを反応させてマ
グネシウムジアルコキシドを合成する方法はよく知られ
ている。また、この反応を芳香族炭化水素、例えばトル
エンやキシレンの存在下で行なうことも知られている（
Ｊ、 Ａｍ、Ｃｈｅｍ、Ｓａｃ、。The method of synthesizing magnesium dialkoxide by reacting alcohol with magnesium metal is well known. It is also known that this reaction can be carried out in the presence of aromatic hydrocarbons, such as toluene and xylene (
J, Am, Chem, Sac,.
６８．８８９および時分・昭５２−１１１５０８号公報
）。68.889 and Time/Bun/1982-111508).
しかし、これらの方法では、一定の粒子形状のものを効
率よく製造することは困難であった。However, with these methods, it has been difficult to efficiently produce particles with a constant shape.
そこで本発明者らは、上記従来方法の欠点を解消して、
粒子状で取扱いの容易なマグネシウムジアルコキシドな
高純度でしかも効果よく製造しうる方法を開発すべく研
究を重ね、本発明を完成するに至った。Therefore, the present inventors solved the drawbacks of the above conventional methods, and
The present invention has been completed through repeated research in order to develop a method for producing magnesium dialkoxide with high purity and high efficiency, which is in the form of particles and easy to handle.
すなわち本発明は、金属マグネシウムとアルコールを活
性化剤の存在下で反応させてマグネシウムジアルコキシ
ドを製造する方法において、反応系に飽和炭化水素を存
在させることを特徴とするマグネシウムジアルコキシド
の製造方法を提供するものである。That is, the present invention provides a method for producing magnesium dialkoxide by reacting metallic magnesium and alcohol in the presence of an activator, which is characterized in that a saturated hydrocarbon is present in the reaction system. This is what we provide.
本発明の方法に用いる金属マグネシウムの形状は、’ｌ
！ｌｌＩＣ１１４＠はなく使用目的等に応じて適宜選定
すればよいが、通常は、反応性、取扱いの便宜などの観
点から粒状あるいはけずり状とすることが好ましい。The shape of the metallic magnesium used in the method of the present invention is 'l
! Although there is no llIC114@, it may be selected as appropriate depending on the purpose of use, etc., but it is usually preferable to form it into granules or scraps from the viewpoint of reactivity, ease of handling, etc.
一方、上記金属マグネシウムと反応するアルコールは、
様々なものがあるが、通常は一般式ＲＯＨで表わされる
アルコールであり、ここでＲは炭素数１〜２０のアルキ
ル基、シクロアルキル基、アラルキル基の範囲から選ば
れる。特に好ましいアルコールとしては、メタノール、
エタノール、プ０ ハ／−ル、フタノール、アシルアル
コール、ヘキシルアルコール、オクチルアルコールなど
がある。ここで加えるべきアルコールの量は、通常は金
属マグネシウムに対して過剰量とすべきであり、好まし
くは金属マグネシウム１グラム原子に対し、２．０５モ
ル以上、より好ましくは２．１θ〜２０モルとすべきで
ある。ここで加えられた過剰量のアルコールは、反応原
料としてのみならず、反応系の溶媒としても作用する。On the other hand, the alcohol that reacts with the metal magnesium is
Although there are various alcohols, it is usually an alcohol represented by the general formula ROH, where R is selected from the range of an alkyl group having 1 to 20 carbon atoms, a cycloalkyl group, and an aralkyl group. Particularly preferred alcohols include methanol,
Examples include ethanol, alcohol, phthanol, acyl alcohol, hexyl alcohol, and octyl alcohol. The amount of alcohol to be added here should normally be in excess of metal magnesium, preferably 2.05 mol or more, more preferably 2.1θ to 20 mol per 1 gram atom of metal magnesium. Should. The excess amount of alcohol added here acts not only as a reaction raw material but also as a solvent for the reaction system.
本発明の方法においては、上記金属マグネシウムとアル
コールの反応系に、飽和炭化水素を存在せしめることが
必要である。この反応系において、アルコールのみを用
いる場合に比べて、本発明の如く飽和炭化水素を用いる
と、反応速度が大きくなると共Ｋ、反応速度のコントロ
ールが容易となり好ましい。In the method of the present invention, it is necessary that a saturated hydrocarbon be present in the reaction system of the metal magnesium and alcohol. In this reaction system, it is preferable to use a saturated hydrocarbon as in the present invention, as compared to the case where only alcohol is used, because the reaction rate increases and the reaction rate can be easily controlled.
ここで用いる飽和炭化水素としては、各−条件に応じて
定めればよ（、通常は炭素数５〜１５の脂肪族あるいは
脂環族の炭化水素などがあげられる。そのうち特に好ま
しいものとしては、ヘキサン、ヘプタン、オクタンなど
がある。The saturated hydrocarbons used here may be determined depending on each condition (usually, aliphatic or alicyclic hydrocarbons having 5 to 15 carbon atoms, etc.) are particularly preferred. Examples include hexane, heptane, and octane.
また本発明の方法においては、反応系に活性化剤を加え
る。この活性化剤としては、各種のものが考えられるが
、好ましいものとしてヨウ素、）・ロゲン化アルキル（
ヨウ化メチル、臭化メチル。Further, in the method of the present invention, an activator is added to the reaction system. Various kinds of activators can be used as this activator, but preferred ones include iodine,
Methyl iodide, methyl bromide.
塩化メチル、ヨウ化エチル、臭化エチル、塩化エチルな
ど）、酢酸、ギ酸エステル、塩化第二水銀などをあげる
ことができる。Methyl chloride, ethyl iodide, ethyl bromide, ethyl chloride, etc.), acetic acid, formate, mercuric chloride, etc.
なおこの活性化剤はそのまま反応系に加えてもよいが、
好ましくは、前述した飽和炭化水素に１〜５０ ｐｐｍ
程度の濃度に溶解したものを、反応系に徐々に添加する
ことが好ましい。Note that this activator may be added to the reaction system as it is, but
Preferably, from 1 to 50 ppm to the aforementioned saturated hydrocarbons.
It is preferable to gradually add a solution dissolved at a certain concentration to the reaction system.
以上のように、本発明の方法は、金属マグネシウムと過
剰量のアルコールならびに飽和炭化水素を反応系に加支
、さらに飽和炭化水素に予め溶解せしめた活性化剤を徐
々に反応系に添加して、反応を進行させるものであるが
、ここでアルコールと飽和炭化水素の添加量の割合は、
適宜定めればよいが、好ましくは反応系に加える飽和炭
化水素と活性化剤の溶剤と゛しての飽和炭化水素の合計
量に対して、アルコールを２〜７（容積比）の範囲とす
べきである。ここでアルコールの添加量が飽和炭化水素
に対して２未満では、生成物の粒子径・が大きくなりす
ぎるおそれがあり、一方、７を超えると微粉末となる−
おそれがあり好ましくな（・。As described above, the method of the present invention involves adding metal magnesium, an excess amount of alcohol, and a saturated hydrocarbon to the reaction system, and then gradually adding an activator predissolved in the saturated hydrocarbon to the reaction system. , which allows the reaction to proceed, but here the ratio of the amounts of alcohol and saturated hydrocarbon added is:
It may be determined as appropriate, but preferably the alcohol should be in the range of 2 to 7 (volume ratio) to the total amount of the saturated hydrocarbon added to the reaction system and the saturated hydrocarbon as a solvent for the activator. It is. If the amount of alcohol added is less than 2 relative to the saturated hydrocarbon, the particle size of the product may become too large, while if it exceeds 7, it will become a fine powder.
There is a possibility that this is not desirable (・.
本発明の方法によれば、上記反応系に活性化剤の溶液を
１０分〜２０時間かけて徐々に添加し、反応温度３０〜
２００°Ｃ１反応圧力常圧〜５０気圧の条件にて、水素
が発生しなくなるまで反応を続けることＫよって、粒子
状のマグネシウムジアルコキシドを高純度で製造するこ
とができる。According to the method of the present invention, an activator solution is gradually added to the reaction system over a period of 10 minutes to 20 hours, and the reaction temperature is 30 to 30 minutes.
Particulate magnesium dialkoxide can be produced with high purity by continuing the reaction at a reaction pressure of 200 DEG C. and a normal pressure to 50 atmospheres until no hydrogen is generated.
本発明の方法による長所をさらに詳しく述べれば、まず
反応速度が大きく、またその速度のコントロールも容易
である。さらに反応に際して、反応容器ＩＩＫ反広物が
付着したり、反応物粒子同士が凝集したりすることがな
〜・ため、操作力を容易であると共に反応後の生成物の
洗浄が容易である。To describe the advantages of the method of the present invention in more detail, first, the reaction rate is high and the rate can be easily controlled. Furthermore, during the reaction, there is no possibility that the reaction container IIK membranes will adhere or the reactant particles will aggregate, making it easy to operate and to wash the product after the reaction.
またその結果、所望する大きさの粒子状のマグネシウム
ジアルコキシドを高純度のものとして得ることができる
。Moreover, as a result, particulate magnesium dialkoxide of a desired size can be obtained with high purity.
かくして得られたマグネシウムジアルコキシドは、粒子
状で取扱いが容易であり、しかも高純度のものであるた
め、乾燥剤、エポキシ樹脂硬化剤。The magnesium dialkoxide thus obtained is easy to handle in particulate form, and is of high purity, so it is used as a desiccant and an epoxy resin curing agent.
各種触媒および触媒担体などに広くかつ有効に坪Ｕ用す
ることができるものである。It can be widely and effectively used for various catalysts and catalyst carriers.
次に本発明の実施例を比較例と共に示す。Next, examples of the present invention will be shown together with comparative examples.
実施例１
５ｇ容の四ロフラスコを乾燥し、４５〜１００メツシユ
（平均粒径２４８μ）の金属マグネシウム３１９ｇ（１
，３１グラム原子）、脱水エタノール（水分４５０ｐｐ
ｍ）７５０ｍ（１２，６モル）およびヘキサン（市販１
級、水分ｓ ｐｐｍ以下）５０ｄを加え、還流温度（７
３°Ｃ）に加熱した。この系に、ヨウ素５．０９をヘキ
サン１００−に溶力箋した溶液を１時間にわたって滴１
した。滴下と同時に反応が始まり水素が発生した。滴下
終了後、２時間還流させて反応を完結させた。反応の進
行にしたがって、マグネシウムの形状が変化し、球状に
生長していくのが認められた。また反応中、フラスコ壁
への付着や粒子同士の凝集は全く認められなかった。Example 1 A 5 g four-hole flask was dried and 319 g (1
, 31 g atoms), dehydrated ethanol (450 ppp water
m) 750 m (12,6 mol) and hexane (commercially available 1
grade, water content s ppm or less) was added, and the reflux temperature (7 ppm or less) was added.
3°C). To this system, a solution of 5.09 iodine in 100% hexane was added dropwise over 1 hour.
did. At the same time as the dropping, the reaction started and hydrogen was generated. After the dropwise addition was completed, the reaction was completed by refluxing for 2 hours. As the reaction progressed, the shape of the magnesium changed and was observed to grow into a spherical shape. Further, during the reaction, no adhesion to the flask wall or aggregation of particles was observed.
反応終了後、室温まで冷却し、静置して上澄液を抜き去
り、ヘキサンで洗浄後、減圧下で乾燥して球状のマグネ
シウムジェトキシド１４９ｇを得た。原料の金属マグネ
シウムあたりの収率ははぼ１００％であり、また生成物
であるマグネシウムジェトキシドの平均粒子径は６８０
μであった。After the reaction was completed, the reaction mixture was cooled to room temperature, allowed to stand, and the supernatant liquid was removed, washed with hexane, and dried under reduced pressure to obtain 149 g of spherical magnesium jetoxide. The yield per metallic magnesium raw material is almost 100%, and the average particle size of the product magnesium jetoxide is 680%.
It was μ.
原料の金属マグネシウムの粒径分布および生成物である
マグネシウムジェトキシドの粒径分布を第１図に示す。FIG. 1 shows the particle size distribution of magnesium metal as a raw material and the particle size distribution of magnesium jetoxide as a product.
実施例２
実施例１において、ヨウ素５．０ ｍｇを溶解スルヘキ
サンの量を１００ｍから２００ｍに変えたこと以外は、
実施例１と同様の操作を行なった。反応中、フラスコ壁
への付着や粒子同士の凝集は全くなかった。また生成し
たマグネシウムジェトキシドの平均粒子径は７５０μで
あり、粒径分布は第１図に示すとおりであった。Example 2 In Example 1, except that the amount of sulfexane dissolved in 5.0 mg of iodine was changed from 100 m to 200 m.
The same operation as in Example 1 was performed. During the reaction, there was no adhesion to the flask wall or aggregation of particles. The average particle size of the produced magnesium jetoxide was 750μ, and the particle size distribution was as shown in FIG.
実施例３
実施例】において、”金属マグネシウムとしテケずり状
（長径０．８ ｍ 、短径０．３ ｍ ）のものを用い
たこと以外は、実施例１と同様の操作を行なった。Example 3 In Example 3, the same operations as in Example 1 were carried out except that metal magnesium was used in the shape of a lever (length: 0.8 m, breadth: 0.3 m).
反応は極めて円滑に進行し、付着や凝集は皆無であった
。また、生成したマグネシウムジェトキシドの形状は球
状に近い粒子状であり、平均粒子径ハ１４００μで太き
（、均一であって、分布はシャープであった。The reaction proceeded extremely smoothly, with no adhesion or aggregation. In addition, the shape of the produced magnesium jetoxide was a particle shape close to a spherical shape, and the average particle diameter was 1400 μm, thick (uniform, and the distribution was sharp).
実施例４
５１容の四日フラスコを乾燥し、４５〜１００メツシユ
（平均粒径２４８μ）の金楓マグネシウム２．８２９（
０，１１６グラム原子）、脱水ｎ−プロパツール１０４
ｍ１（１，３９モル）およびヘキサン（市ｋｘ級、水分
５ ｐｐｍ以下）１０１１を加え、還流温度（約７３℃
）に加熱した。この系Ｋ、ヨウ素５ Ｑをヘキサン１６
ｍ１に溶がした溶液を０．５時間にわたって滴下した。Example 4 A 51-volume four-day flask was dried and 45 to 100 meshes (average particle size 248μ) of 2.829 g
0,116 g atom), dehydrated n-propatool 104
Add m1 (1,39 mol) and 1011 hexane (city KX grade, water content 5 ppm or less), and heat to reflux temperature (approximately 73°C).
). This system K, iodine 5 Q, hexane 16
A solution dissolved in m1 was added dropwise over 0.5 hour.
滴下と同時に反応が始まり水素が発生した。滴下終了後
、１５時間還流させて反応を完結させた。反応の進行に
したがって、マグネシウムの形状が変化し、球状に生長
してい（のが認められた。また反応中、フラスコ壁への
付着や粒子同士の凝集は全く認められながった。At the same time as the dropping, the reaction started and hydrogen was generated. After the dropwise addition was completed, the reaction was completed by refluxing for 15 hours. As the reaction progressed, the shape of the magnesium changed and it was observed to grow into a spherical shape.During the reaction, no adhesion to the flask wall or aggregation of particles was observed at all.
反応終了後、室温まで冷却し、静置して上澄液を抜き去
り、ヘキサンで洗浄後、減圧下で乾燥して球状のマグネ
シウムジロープロポキシド１６．３２を得た。原料の金
属マグネシウムあたりの収率はほぼ１００％であり、ま
た生成物であるマグネシウムジｎ−グロボキシドの平均
粒子径は５ｏ。After the reaction was completed, the reaction mixture was cooled to room temperature, left to stand, and the supernatant liquid was removed, washed with hexane, and dried under reduced pressure to obtain spherical magnesium diropropoxide 16.32. The yield per raw material magnesium metal is approximately 100%, and the product magnesium di-n-globoxoxide has an average particle size of 5o.
μであった。It was μ.
比較例１
５１容の四日フラスコを乾燥し、４５〜１００メツシユ
（平均粒径２４８μ）の金属マグネシウム４．０ｇ（０
，１６５グラム原子）、脱水エタノール（水分４５０
ｐｐｆｎ ） １７４１１４ （３，０２モル）および
ｐ−キシレン５ｄを加え、還流温度（７３°Ｃ）Ｋ加熱
した。この系に、ヨウ素５０富ｇをｐ−キシレン７．６
ｄに溶かした溶液を０５時間にわたって滴下した。滴下
と同時に反応が始まり水素が発生した。滴下終了後、１
８５時間還流させて反応を完結させた。反応中、フラス
コ壁への付着や粒子同士の凝集は全く認められなかった
。Comparative Example 1 A 51-volume four-day flask was dried, and 4.0 g (0.0
, 165 grams atom), dehydrated ethanol (water 450
ppfn) 174114 (3.02 mol) and p-xylene 5d were added and heated to reflux temperature (73°C) K. To this system, add 50 g of iodine to 7.6 g of p-xylene.
The solution dissolved in d was added dropwise over 05 hours. At the same time as the dropping, the reaction started and hydrogen was generated. After dropping, 1
The reaction was completed by refluxing for 85 hours. During the reaction, no adhesion to the flask wall or aggregation of particles was observed.
反応終了後、室温まで冷却し、静置して上澄液を抜き去
り、ヘキサンで洗浄後、減圧下で乾燥して粒子状のマグ
ネシウムジェトキシド１６９ｇを得た。原料の金属マグ
ネシウムあたりの収率はほぼ９０≦であり、また生成物
であるマグネシウムジェトキシドの平均粒子径は１５μ
であった。After the reaction was completed, the reaction mixture was cooled to room temperature, allowed to stand, and the supernatant liquid was removed, washed with hexane, and dried under reduced pressure to obtain 169 g of particulate magnesium jetoxide. The yield per raw material magnesium metal is approximately 90≦, and the average particle size of the product magnesium jetoxide is 15μ.
Met.
比較例２
５１容の四日フラスコを乾燥し、４５〜１００メツシユ
（平均粒径２４８μ）の金属マグネシウム４．０ｇ（０
，１６５グラム原子）、脱水エタノール（水分４５０ｐ
ｐｍ）１７４ｓ＋ｊ（３，０２モル）およびｐ−キシレ
ン１０ｍを加え、還流温度（７３℃）に加熱した。この
系に、ヨウ素５０叩をｐ−キシレン４１．２１１７に溶
かした溶液を０．５時間にわたって滴下した。滴下と同
時に反応が始まり水素が発生した。滴下終了後、６時間
還流させて反応を完結させた。反応中、フラスコ壁への
付着や粒子同士の凝集が認められた。Comparative Example 2 A 51-volume four-day flask was dried, and 4.0 g (0.0
, 165 grams atom), dehydrated ethanol (water 450p
pm) 174s+j (3.02 mol) and 10 m of p-xylene were added and heated to reflux temperature (73°C). A solution of 50 iodine dissolved in 41.2117 p-xylene was added dropwise to this system over 0.5 hours. At the same time as the dropping, the reaction started and hydrogen was generated. After the dropwise addition was completed, the reaction was completed by refluxing for 6 hours. During the reaction, adhesion to the flask wall and aggregation of particles were observed.
反応終了後、室温まで冷却し、静置して上澄液を抜き去
り、ヘキサンで洗浄後、減圧下で乾燥して粒子状のマグ
ネシウムジェトキシド１８．７ｇを得た。原料の金属マ
グネシウムあたりの収率ははぼ１００％であり、また生
成物であるマグネシウムジェトキシドの平均粒子径は９
００μであった。After the reaction was completed, the reaction mixture was cooled to room temperature, allowed to stand, and the supernatant liquid was removed, washed with hexane, and dried under reduced pressure to obtain 18.7 g of particulate magnesium jetoxide. The yield per metallic magnesium raw material is almost 100%, and the average particle size of the product magnesium jetoxide is 9.
It was 00μ.
第１図は、実施例１において用いた金属マグネシウムお
よび実施例１の生成物ならびに実施例２の生成物のそれ
ぞれの粒径分布を示す。
特許出願人 出光興産株式会社FIG. 1 shows the particle size distribution of the magnesium metal used in Example 1 and the product of Example 1 and the product of Example 2, respectively. Patent applicant Idemitsu Kosan Co., Ltd.
Claims (1)
で反応させてマグネシウムジアルコキシドを製造する方
法において、反応系に飽和炭化水素を存在させることを
特徴とするマグネシウムジアルコキシドの製造方法。1. A method for producing magnesium dialkoxide by reacting magnesium metal and an alcohol in the presence of an activator, which is characterized in that a saturated hydrocarbon is present in the reaction system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13983281A JPS5841832A (en) | 1981-09-07 | 1981-09-07 | Preparation of magnesium dialkoxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13983281A JPS5841832A (en) | 1981-09-07 | 1981-09-07 | Preparation of magnesium dialkoxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5841832A true JPS5841832A (en) | 1983-03-11 |
| JPS634815B2 JPS634815B2 (en) | 1988-02-01 |
Family
ID=15254526
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP13983281A Granted JPS5841832A (en) | 1981-09-07 | 1981-09-07 | Preparation of magnesium dialkoxide |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5841832A (en) |
Cited By (25)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6251633A (en) * | 1985-08-28 | 1987-03-06 | シエル・インタ−ナシヨネイル・リサ−チ・マ−チヤツピイ・ベ−・ウイ | Manufacture of spherical magnesium alkoxide particle |
| JPS63194164U (en) * | 1987-06-02 | 1988-12-14 | ||
| EP0461268A1 (en) * | 1989-12-28 | 1991-12-18 | Idemitsu Petrochemical Co. Ltd. | Process for producing olefin polymerization catalyst component and polyolefin |
| US6297188B1 (en) * | 1998-10-27 | 2001-10-02 | Degussa-Huels Aktiengesellschaft | Magnesium ethoxide having a high coarse particle content, process for its preparation and its use |
| WO2004020480A1 (en) | 2002-08-29 | 2004-03-11 | Toho Catalyst Co., Ltd | Solid catalyst component for olefin polymerization and catalyst |
| WO2006033512A1 (en) * | 2004-09-23 | 2006-03-30 | Samsung Total Petrochemicals Co., Ltd. | Method of preparation of spherical support for olefin polymerization catalyst |
| WO2012060361A1 (en) | 2010-11-04 | 2012-05-10 | 東邦チタニウム株式会社 | Method for producing solid catalyst component for olefin polymerization, catalyst for olefin polymerization, and olefin polymers |
| WO2013005463A1 (en) | 2011-07-06 | 2013-01-10 | 東邦チタニウム株式会社 | Solid catalyst component for olefin polymerization, catalyst for olefin polymerization, and method for producing olefin polymer |
| WO2013027560A1 (en) | 2011-08-25 | 2013-02-28 | 東邦チタニウム株式会社 | Method for producing solid catalyst component for olefin polymerization, catalyst for olefin polymerization, and method for producing olefin polymer |
| WO2013042400A1 (en) | 2011-09-20 | 2013-03-28 | 東邦チタニウム株式会社 | Solid catalyst component for polymerization of olefin, catalyst for polymerization of olefin, and method for producing olefin polymer |
| WO2014013916A1 (en) | 2012-07-18 | 2014-01-23 | 東邦チタニウム株式会社 | Method for producing solid catalyst component for use in polymerization of olefin, catalyst for use in polymerization of olefin, and method for producing olefin polymer |
| WO2014050809A1 (en) | 2012-09-28 | 2014-04-03 | 東邦チタニウム株式会社 | Solid catalyst component for polymerization of olefins, catalyst for polymerization of olefins, and method for producing olefin polymer |
| WO2014132806A1 (en) | 2013-02-27 | 2014-09-04 | 東邦チタニウム株式会社 | Production method for solid catalyst component for polymerizing olefins, catalyst for polymerizing olefins, and production method for polymerized olefins |
| WO2014132805A1 (en) | 2013-02-27 | 2014-09-04 | 東邦チタニウム株式会社 | Production method for solid catalyst component for polymerizing olefins, catalyst for polymerizing olefins, and production method for polymerized olefins |
| WO2014132777A1 (en) | 2013-02-27 | 2014-09-04 | 東邦チタニウム株式会社 | Solid catalyst component for polymerizing olefins, catalyst for polymerizing olefins, and production method for polymerized olefins |
| WO2014132759A1 (en) | 2013-02-27 | 2014-09-04 | 東邦チタニウム株式会社 | Method for producing propylene block copolymer |
| US10113014B1 (en) | 2017-06-27 | 2018-10-30 | Toho Titanium Co., Ltd. | Method for producing solid catalyst component containing vanadium compound for olefin polymerization, olefin polymerization catalyst, and method for producing olefin polymer |
| WO2019005261A1 (en) | 2017-06-27 | 2019-01-03 | Exxonmobil Chemical Patents Inc. | High stiffness polypropylene impact copolymer |
| WO2019005262A1 (en) | 2017-06-27 | 2019-01-03 | Exxonmobil Chemical Patents Inc. | High impact polypropylene impact copolymer |
| US10246530B2 (en) | 2017-06-27 | 2019-04-02 | Toho Titanium Co., Ltd. | Method for producing solid catalyst component for olefin polymerization, catalyst for olefin polymerization and a process for propylene polymerization |
| WO2019064967A1 (en) | 2017-09-29 | 2019-04-04 | 東邦チタニウム株式会社 | CATALYST FOR OLEFIN POLYMERIZATION, METHOD FOR PRODUCING CATALYST FOR OLEFIN POLYMERIZATION, METHOD FOR PRODUCING OLEFIN POLYMER, AND PROPYLENE-α-OLEFIN COPOLYMER |
| WO2019202800A1 (en) | 2018-04-20 | 2019-10-24 | 東邦チタニウム株式会社 | Olefin polymer and method for producing olefin polymer |
| WO2021105373A1 (en) | 2019-11-29 | 2021-06-03 | Thai Polyethylene Co., Ltd. | Catalyst composition for the polymerization of olefins |
| WO2021220644A1 (en) | 2020-04-28 | 2021-11-04 | 東邦チタニウム株式会社 | Solid catalytic component for olefin polymerization and production method therefor, catalyst for olefin polymerization and production method therefor, and production method for olefin polymer |
| WO2022250034A1 (en) | 2021-05-26 | 2022-12-01 | 東邦チタニウム株式会社 | Olefin polymerization solid catalyst component, olefin polymerization catalyst, manufacturing method for olefin polymer, olefin polymer, manufacturing method for propylene-based block copolymer, and propylene-based block copolymer |
-
1981
- 1981-09-07 JP JP13983281A patent/JPS5841832A/en active Granted
Cited By (26)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6251633A (en) * | 1985-08-28 | 1987-03-06 | シエル・インタ−ナシヨネイル・リサ−チ・マ−チヤツピイ・ベ−・ウイ | Manufacture of spherical magnesium alkoxide particle |
| JPS63194164U (en) * | 1987-06-02 | 1988-12-14 | ||
| EP0461268A1 (en) * | 1989-12-28 | 1991-12-18 | Idemitsu Petrochemical Co. Ltd. | Process for producing olefin polymerization catalyst component and polyolefin |
| US6297188B1 (en) * | 1998-10-27 | 2001-10-02 | Degussa-Huels Aktiengesellschaft | Magnesium ethoxide having a high coarse particle content, process for its preparation and its use |
| JP2010202667A (en) * | 1998-10-27 | 2010-09-16 | Evonik Degussa Gmbh | Magnesium ethoxide having coarse particle content, method for producing the same and its use |
| WO2004020480A1 (en) | 2002-08-29 | 2004-03-11 | Toho Catalyst Co., Ltd | Solid catalyst component for olefin polymerization and catalyst |
| WO2006033512A1 (en) * | 2004-09-23 | 2006-03-30 | Samsung Total Petrochemicals Co., Ltd. | Method of preparation of spherical support for olefin polymerization catalyst |
| WO2012060361A1 (en) | 2010-11-04 | 2012-05-10 | 東邦チタニウム株式会社 | Method for producing solid catalyst component for olefin polymerization, catalyst for olefin polymerization, and olefin polymers |
| WO2013005463A1 (en) | 2011-07-06 | 2013-01-10 | 東邦チタニウム株式会社 | Solid catalyst component for olefin polymerization, catalyst for olefin polymerization, and method for producing olefin polymer |
| WO2013027560A1 (en) | 2011-08-25 | 2013-02-28 | 東邦チタニウム株式会社 | Method for producing solid catalyst component for olefin polymerization, catalyst for olefin polymerization, and method for producing olefin polymer |
| WO2013042400A1 (en) | 2011-09-20 | 2013-03-28 | 東邦チタニウム株式会社 | Solid catalyst component for polymerization of olefin, catalyst for polymerization of olefin, and method for producing olefin polymer |
| WO2014013916A1 (en) | 2012-07-18 | 2014-01-23 | 東邦チタニウム株式会社 | Method for producing solid catalyst component for use in polymerization of olefin, catalyst for use in polymerization of olefin, and method for producing olefin polymer |
| WO2014050809A1 (en) | 2012-09-28 | 2014-04-03 | 東邦チタニウム株式会社 | Solid catalyst component for polymerization of olefins, catalyst for polymerization of olefins, and method for producing olefin polymer |
| WO2014132806A1 (en) | 2013-02-27 | 2014-09-04 | 東邦チタニウム株式会社 | Production method for solid catalyst component for polymerizing olefins, catalyst for polymerizing olefins, and production method for polymerized olefins |
| WO2014132805A1 (en) | 2013-02-27 | 2014-09-04 | 東邦チタニウム株式会社 | Production method for solid catalyst component for polymerizing olefins, catalyst for polymerizing olefins, and production method for polymerized olefins |
| WO2014132777A1 (en) | 2013-02-27 | 2014-09-04 | 東邦チタニウム株式会社 | Solid catalyst component for polymerizing olefins, catalyst for polymerizing olefins, and production method for polymerized olefins |
| WO2014132759A1 (en) | 2013-02-27 | 2014-09-04 | 東邦チタニウム株式会社 | Method for producing propylene block copolymer |
| US10113014B1 (en) | 2017-06-27 | 2018-10-30 | Toho Titanium Co., Ltd. | Method for producing solid catalyst component containing vanadium compound for olefin polymerization, olefin polymerization catalyst, and method for producing olefin polymer |
| WO2019005261A1 (en) | 2017-06-27 | 2019-01-03 | Exxonmobil Chemical Patents Inc. | High stiffness polypropylene impact copolymer |
| WO2019005262A1 (en) | 2017-06-27 | 2019-01-03 | Exxonmobil Chemical Patents Inc. | High impact polypropylene impact copolymer |
| US10246530B2 (en) | 2017-06-27 | 2019-04-02 | Toho Titanium Co., Ltd. | Method for producing solid catalyst component for olefin polymerization, catalyst for olefin polymerization and a process for propylene polymerization |
| WO2019064967A1 (en) | 2017-09-29 | 2019-04-04 | 東邦チタニウム株式会社 | CATALYST FOR OLEFIN POLYMERIZATION, METHOD FOR PRODUCING CATALYST FOR OLEFIN POLYMERIZATION, METHOD FOR PRODUCING OLEFIN POLYMER, AND PROPYLENE-α-OLEFIN COPOLYMER |
| WO2019202800A1 (en) | 2018-04-20 | 2019-10-24 | 東邦チタニウム株式会社 | Olefin polymer and method for producing olefin polymer |
| WO2021105373A1 (en) | 2019-11-29 | 2021-06-03 | Thai Polyethylene Co., Ltd. | Catalyst composition for the polymerization of olefins |
| WO2021220644A1 (en) | 2020-04-28 | 2021-11-04 | 東邦チタニウム株式会社 | Solid catalytic component for olefin polymerization and production method therefor, catalyst for olefin polymerization and production method therefor, and production method for olefin polymer |
| WO2022250034A1 (en) | 2021-05-26 | 2022-12-01 | 東邦チタニウム株式会社 | Olefin polymerization solid catalyst component, olefin polymerization catalyst, manufacturing method for olefin polymer, olefin polymer, manufacturing method for propylene-based block copolymer, and propylene-based block copolymer |
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| Publication number | Publication date |
|---|---|
| JPS634815B2 (en) | 1988-02-01 |
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