JPH0150322B2 - - Google Patents
Info
- Publication number
- JPH0150322B2 JPH0150322B2 JP4391183A JP4391183A JPH0150322B2 JP H0150322 B2 JPH0150322 B2 JP H0150322B2 JP 4391183 A JP4391183 A JP 4391183A JP 4391183 A JP4391183 A JP 4391183A JP H0150322 B2 JPH0150322 B2 JP H0150322B2
- Authority
- JP
- Japan
- Prior art keywords
- polymerization
- stage
- weight
- vinyl chloride
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 238000006116 polymerization reaction Methods 0.000 claims description 48
- 239000000178 monomer Substances 0.000 claims description 22
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 claims description 21
- 239000011347 resin Substances 0.000 claims description 12
- 229920005989 resin Polymers 0.000 claims description 12
- 229920000642 polymer Polymers 0.000 claims description 11
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 230000005484 gravity Effects 0.000 claims description 9
- 238000000034 method Methods 0.000 claims description 9
- 239000002270 dispersing agent Substances 0.000 claims description 8
- 229920002689 polyvinyl acetate Polymers 0.000 claims description 5
- 239000011118 polyvinyl acetate Substances 0.000 claims description 5
- 239000003505 polymerization initiator Substances 0.000 claims description 4
- 238000007127 saponification reaction Methods 0.000 claims description 4
- 239000012736 aqueous medium Substances 0.000 claims description 2
- 230000000379 polymerizing effect Effects 0.000 claims 1
- 230000000704 physical effect Effects 0.000 description 9
- 229920000915 polyvinyl chloride Polymers 0.000 description 8
- 239000004800 polyvinyl chloride Substances 0.000 description 8
- 238000001125 extrusion Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 229920001577 copolymer Polymers 0.000 description 2
- 238000007872 degassing Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- HGXJDMCMYLEZMJ-UHFFFAOYSA-N (2-methylpropan-2-yl)oxy 2,2-dimethylpropaneperoxoate Chemical compound CC(C)(C)OOOC(=O)C(C)(C)C HGXJDMCMYLEZMJ-UHFFFAOYSA-N 0.000 description 1
- BEQKKZICTDFVMG-UHFFFAOYSA-N 1,2,3,4,6-pentaoxepane-5,7-dione Chemical compound O=C1OOOOC(=O)O1 BEQKKZICTDFVMG-UHFFFAOYSA-N 0.000 description 1
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 1
- AFTPEBDOGXRMNQ-UHFFFAOYSA-N 2,2,4-Trimethylhexane Chemical compound CCC(C)CC(C)(C)C AFTPEBDOGXRMNQ-UHFFFAOYSA-N 0.000 description 1
- OEPOKWHJYJXUGD-UHFFFAOYSA-N 2-(3-phenylmethoxyphenyl)-1,3-thiazole-4-carbaldehyde Chemical compound O=CC1=CSC(C=2C=C(OCC=3C=CC=CC=3)C=CC=2)=N1 OEPOKWHJYJXUGD-UHFFFAOYSA-N 0.000 description 1
- RPBWMJBZQXCSFW-UHFFFAOYSA-N 2-methylpropanoyl 2-methylpropaneperoxoate Chemical compound CC(C)C(=O)OOC(=O)C(C)C RPBWMJBZQXCSFW-UHFFFAOYSA-N 0.000 description 1
- CARSMBZECAABMO-UHFFFAOYSA-N 3-chloro-2,6-dimethylbenzoic acid Chemical compound CC1=CC=C(Cl)C(C)=C1C(O)=O CARSMBZECAABMO-UHFFFAOYSA-N 0.000 description 1
- RTANHMOFHGSZQO-UHFFFAOYSA-N 4-methoxy-2,4-dimethylpentanenitrile Chemical compound COC(C)(C)CC(C)C#N RTANHMOFHGSZQO-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- YIVJZNGAASQVEM-UHFFFAOYSA-N Lauroyl peroxide Chemical compound CCCCCCCCCCCC(=O)OOC(=O)CCCCCCCCCCC YIVJZNGAASQVEM-UHFFFAOYSA-N 0.000 description 1
- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 description 1
- -1 acrylic ester Chemical class 0.000 description 1
- 239000003963 antioxidant agent Substances 0.000 description 1
- NSGQRLUGQNBHLD-UHFFFAOYSA-N butan-2-yl butan-2-yloxycarbonyloxy carbonate Chemical compound CCC(C)OC(=O)OOC(=O)OC(C)CC NSGQRLUGQNBHLD-UHFFFAOYSA-N 0.000 description 1
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- BSVQJWUUZCXSOL-UHFFFAOYSA-N cyclohexylsulfonyl ethaneperoxoate Chemical compound CC(=O)OOS(=O)(=O)C1CCCCC1 BSVQJWUUZCXSOL-UHFFFAOYSA-N 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- 239000003999 initiator Substances 0.000 description 1
- QYZFTMMPKCOTAN-UHFFFAOYSA-N n-[2-(2-hydroxyethylamino)ethyl]-2-[[1-[2-(2-hydroxyethylamino)ethylamino]-2-methyl-1-oxopropan-2-yl]diazenyl]-2-methylpropanamide Chemical compound OCCNCCNC(=O)C(C)(C)N=NC(C)(C)C(=O)NCCNCCO QYZFTMMPKCOTAN-UHFFFAOYSA-N 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Polymerisation Methods In General (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Description
本発明は、加工生産性に優れたポリ塩化ビニル
系樹脂の製造法に関するものである。詳しくは、
嵩比重が高く、かつ物性が良好な押出成形に適し
たポリ塩化ビニル系樹脂の製造法である。
従来、ポリ塩化ビニル樹脂の嵩比重を上げれば
押出吐出量がアツプし、加えて生産性が向上する
ことは知られていた。ポリ塩化ビニル樹脂の嵩比
重アツプを図る方法として、転化率70％前後で塩
化ビニルモノマーを途中追加する方法が知られて
いる。しかし、該方法で得た樹脂は通常のポリ塩
化ビニル系樹脂と同等な加工条件下で成形すれば
物性が悪く残存モノマーも抜けにくいことが知ら
れていた。
本発明はかかる欠点を改良した加工生産性がよ
く、物性も良好で、かつ残存モノマーが抜け易い
ポリ塩化ビニル系樹脂の製造法に関するものであ
る。詳しくは、重合の第１段階として水媒体、油
溶性重合開始剤、分散剤の存在下塩化ビニル系モ
ノマーを重合し、重合転化率50重量％以下、好ま
しくは20〜40重量％まで重合し、次いで重合の第
２段階として重合温度を第１段階重合温度より５
℃以上高い重合温度に変更し、重合を続け、第２
段階重合で缶内圧力が降下開始以前に、塩化ビニ
ル系モノマーを追加し、重合を続け、反応を終了
させ、第１段階での重合体重量をW1とし、最終
の重合体重量をW2とすれば（W2−W1）／W1が
1.0以上になることを特徴とするものである。
重合温度を変更する時のモノマー、ポリマーの
転化率が20重量％未満では、ポリ塩化ビニル系樹
脂中の残留モノマーが抜け難くなり、また50重量
％を越えると嵩比重が上がりにくくなる。
第１段階の重合温度は30℃〜55℃がよい。第２
段階の重合温度は第１段階の重合温度より５℃以
上、好ましくは10℃以上高い温度で重合するのが
よい。５℃以下では嵩比重アツプの効果が少な
い。ちなみに第１段階、第２段階とも、その最高
温度と最低温度の差は５℃未満である。なお第１
段階の温度と第２段階の温度の差は、それぞれの
平均温度同士で比較する。
第２段階の重合で、塩化ビニル系モノマーの追
加時期は、缶内圧力が降下する以前が良い。これ
は缶内圧力が降下してからモノマーを追加して
も、嵩比重アツプの効果が少ないためである。
本発明では第１段階重合終了時の重合体重量を
W1とし、第２段階重合終了時の重合体重量をW2
とすると（W2−W1）／W1が1.0以上好ましくは1.5以上
が良い。これは該比が1.0未満であれば良い物性
が発現しがたいためである。従つて、第２段階で
追加する塩化ビニル系モノマー量は上記の比を満
足する様な量を追加すべきである。別に上記比を
大巾に越す量を追加し、残分を回収してもよい
が、これは生産性上好ましくない。また塩化ビニ
ルの追加法は、一度に追加してもよいし、連続的
或は断続的に追加してもよい。
本発明で使用する油溶性重合開始剤は公知のも
のでよい。しかし、重合温度を途中で変化するた
め、その温度に適した分解温度を有する開始剤を
組み合すのがよい。また、第２段階重合時に重合
開始剤を追加してもよい。具体的にはアセチルシ
クロヘキシルスルホニルパーオキサイド、イソブ
チロイルパーオキサイド、２，2′−アゾビス（４
−メトキシ−２，４−ジメチルバレロニトリル、
ジ−２−エチルヘキシルパーオキシジカーボネー
ト、ジ−sec−ブチルパーオキシジカーボネート、
クミルパーオキシネオデカネート、tert−ブチル
パーオキシピバレート、２，2′−アゾビス−２，
４−ジメチルバレロニトリル、ラウロイルパーオ
キサイド、tert−ブチルパーオキシ３，５，５−
トリメチルヘキサノエイト等が好適に使用され
る。これらの使用量は塩化ビニル系モノマーに対
し0.01〜1.0重量％である。
本発明で使用する分散剤としては、セルロース
誘導体、部分鹸化ポリ酢酸ビニル、無水マレイン
酸−ビニルエーテル共重合体、酸化エチレン−酸
化プロピレン共重合等の公知の分散剤がある。し
かし、鹸化度65〜75％の低鹸化度の部分鹸化ポリ
酢酸ビニルを用いるのが物性上好適であることが
判つた。この原因は明白でないが、樹脂との相溶
性が増すためであろうと考えられる。これら分散
剤の使用量は塩化ビニル系モノマーに対し0.01〜
1.0重量％である。
本発明で使用する塩化ビニル系モノマーとは、
塩化ビニル単独あるいは塩化ビニルを主体とし、
これと共重合可能な単量体との混合物をいう。塩
化ビニルと共重合可能な単量体としては、塩化ビ
ニリデン、エチレン、ブテン、プロピレン、酢酸
ビニル、アクリル酸エステル等が挙げられる。こ
れらの量は塩化ビニルに対して10重量％以内が良
い。
本発明では連鎖移動剤や抗酸化剤等を適宜使用
しても何ら支障はない。
以下に、本発明の実施態様を示すが、これらは
何ら本発明を限定するものでない。
なお実施例記載の物性評価は下記の方法に従つ
た。
重合度：JIS Ｋ−6721に従つた。
嵩比重：JIS Ｋ−6721に従つた。
残存モノマー量：ウエツトケーキ約10ｇをシヤ
ーレに採取し、55℃で60分間乾燥。乾燥し
た樹脂中の残存モノマ定量する。残存モノ
マー量は乾燥レジン当りのppmとして表示
した。
抽出量：表ーイの配合物を二軸押出機で３イン
チのパイプとして押出した。この時の時間
当りのパイプ重量を押出量とした。
伸び：３インチパイプからダンベル型試験片を
切出し、JIS K6742に従つて伸び率（％）
を測定した。
The present invention relates to a method for producing polyvinyl chloride resin with excellent processing productivity. For more information,
This is a method for producing a polyvinyl chloride resin that has a high bulk density and good physical properties and is suitable for extrusion molding. Conventionally, it has been known that increasing the bulk specific gravity of polyvinyl chloride resin increases the extrusion output and, in addition, improves productivity. A known method for increasing the bulk specific gravity of polyvinyl chloride resin is to add vinyl chloride monomer midway through the process at a conversion rate of around 70%. However, it has been known that the resin obtained by this method has poor physical properties and is difficult to remove residual monomers when molded under the same processing conditions as ordinary polyvinyl chloride resins. The present invention relates to a method for producing a polyvinyl chloride resin which overcomes these drawbacks and has good processing productivity, good physical properties, and easy removal of residual monomers. Specifically, as the first step of polymerization, a vinyl chloride monomer is polymerized in the presence of an aqueous medium, an oil-soluble polymerization initiator, and a dispersant, and polymerization is performed to a polymerization conversion of 50% by weight or less, preferably 20 to 40% by weight, Then, in the second stage of polymerization, the polymerization temperature was lowered by 5% from the first stage polymerization temperature.
Change the polymerization temperature to a temperature higher than ℃ and continue polymerization.
Before the pressure inside the reactor starts to drop during stepwise polymerization, vinyl chloride monomer is added, polymerization continues, and the reaction is terminated.The polymer weight in the first stage is set to W 1 , and the final polymer weight is set to W 2 . Then, (W 2 − W 1 )/W 1 is
It is characterized by a value of 1.0 or more. If the conversion rate of the monomer or polymer when changing the polymerization temperature is less than 20% by weight, the residual monomer in the polyvinyl chloride resin will be difficult to remove, and if it exceeds 50% by weight, the bulk specific gravity will be difficult to increase. The polymerization temperature in the first stage is preferably 30°C to 55°C. Second
The polymerization temperature in the step is preferably 5°C or more, preferably 10°C or more higher than the polymerization temperature in the first stage. Below 5°C, the effect of increasing bulk specific gravity is small. Incidentally, the difference between the highest and lowest temperatures in both the first and second stages is less than 5°C. Note that the first
The difference between the temperature of the stage and the temperature of the second stage is compared based on their respective average temperatures. In the second stage of polymerization, it is best to add the vinyl chloride monomer before the internal pressure drops. This is because even if monomer is added after the internal pressure has decreased, the effect of increasing bulk specific gravity is small. In the present invention, the polymer weight at the end of the first stage polymerization is
W 1 , and the polymer weight at the end of the second stage polymerization is W 2
Then, (W 2 −W 1 )/W 1 is 1.0 or more, preferably 1.5 or more. This is because if the ratio is less than 1.0, it is difficult to exhibit good physical properties. Therefore, the amount of vinyl chloride monomer added in the second step should be such that the above ratio is satisfied. Separately, an amount exceeding the above ratio may be added and the remaining amount recovered, but this is not preferable in terms of productivity. Furthermore, vinyl chloride may be added all at once, continuously or intermittently. The oil-soluble polymerization initiator used in the present invention may be any known one. However, since the polymerization temperature is changed during the course of the polymerization, it is preferable to combine an initiator with a decomposition temperature suitable for that temperature. Furthermore, a polymerization initiator may be added during the second stage polymerization. Specifically, acetylcyclohexylsulfonyl peroxide, isobutyroyl peroxide, 2,2'-azobis(4
-methoxy-2,4-dimethylvaleronitrile,
Di-2-ethylhexyl peroxydicarbonate, di-sec-butyl peroxydicarbonate,
cumyl peroxyneodecanate, tert-butylperoxypivalate, 2,2'-azobis-2,
4-dimethylvaleronitrile, lauroyl peroxide, tert-butylperoxy 3,5,5-
Trimethylhexanoate and the like are preferably used. The amount of these used is 0.01 to 1.0% by weight based on the vinyl chloride monomer. Dispersants used in the present invention include known dispersants such as cellulose derivatives, partially saponified polyvinyl acetate, maleic anhydride-vinyl ether copolymers, and ethylene oxide-propylene oxide copolymers. However, it has been found that it is preferable to use partially saponified polyvinyl acetate having a low saponification degree of 65 to 75% in terms of physical properties. The reason for this is not clear, but it is thought to be due to increased compatibility with the resin. The amount of these dispersants used is 0.01 to 0.01 to vinyl chloride monomer.
It is 1.0% by weight. The vinyl chloride monomer used in the present invention is
Vinyl chloride alone or mainly vinyl chloride,
It refers to a mixture of this and a copolymerizable monomer. Examples of monomers copolymerizable with vinyl chloride include vinylidene chloride, ethylene, butene, propylene, vinyl acetate, and acrylic ester. The amount of these is preferably within 10% by weight based on vinyl chloride. In the present invention, there is no problem in using chain transfer agents, antioxidants, etc. as appropriate. Embodiments of the present invention are shown below, but these are not intended to limit the present invention in any way. The physical properties described in the examples were evaluated according to the following method. Degree of polymerization: According to JIS K-6721. Bulk specific gravity: According to JIS K-6721. Amount of residual monomer: Collect about 10g of wet cake in a shear dish and dry at 55℃ for 60 minutes. Quantitate the remaining monomer in the dried resin. The amount of residual monomer was expressed as ppm per dry resin. Extracted amount: The formulation in Table A was extruded using a twin screw extruder as a 3-inch pipe. The pipe weight per hour at this time was defined as the extrusion amount. Elongation: Cut a dumbbell-shaped test piece from a 3-inch pipe and measure the elongation rate (%) according to JIS K6742.
was measured.
【表】【table】
【表】
実施例 １〜11
比較例 １〜７
撹拌機、ジヤケツトを有する内容積1000重合
器に、鹸化度70％の部分鹸化ポリ酢酸ビニル105
ｇ、イオン交換水500Kg、ジ−２−エチルヘキシ
ルパーオキシジカーボネート135ｇを仕込み脱気
后、塩化ビニル300Kgを仕込んだ。内温を48℃に
昇温し所定時間重合し、次いで重合温度を65℃に
上げ所定時間重合し、塩化ビニルを追加した。こ
の後、更に重合を続け最終的に重合体を得た。
この重合体の嵩比重、物性の測定結果を表−１
に一覧する。
また比較のため重合初期から最后まで同一重合
温度で重合したものを表−１に記載した。[Table] Examples 1 to 11 Comparative Examples 1 to 7 Partially saponified polyvinyl acetate 105 with a degree of saponification of 70% was placed in a 1000 volume polymerization vessel equipped with a stirrer and a jacket.
After degassing, 300 kg of vinyl chloride was charged. The internal temperature was raised to 48°C and polymerization was carried out for a predetermined time, then the polymerization temperature was raised to 65°C and polymerization was carried out for a predetermined time, and vinyl chloride was added. After this, polymerization was further continued to finally obtain a polymer. Table 1 shows the measurement results of bulk specific gravity and physical properties of this polymer.
Listed in For comparison, Table 1 shows polymers polymerized at the same polymerization temperature from the initial stage to the final stage.
【表】【table】
【表】
実施例 12〜15
撹拌機、ジヤケツトを有する内容積1500重合
器に分散剤120ｇ、イオン交換水800Kg、クミルパ
ーオキシネオデカネート80ｇ、tert.ブチルパーオ
キシ３，５，５−トリメチルヘキサノエート107
ｇを仕込み脱気后塩化ビニル400Kgを仕込んだ。
52℃重合を開始し、転化率30％で重合温度を65℃
に上げ転化率60％時に、塩化ビニルモノマーを80
Kg仕込み更に重合を続け転化率100％（重合仕込
時の塩化ビニルモノマーに対するポリ塩化ビニル
の転化率）で重合を停止した。重合体の嵩比重、
物性の測定結果を表−２に示す。[Table] Examples 12 to 15 In a 1500 volume polymerization vessel equipped with a stirrer and a jacket, 120 g of dispersant, 800 kg of ion-exchanged water, 80 g of cumyl peroxyneodecanate, and tert.butylperoxy 3,5,5-trimethylhexane were added. Noeto 107
After degassing, 400 kg of vinyl chloride was charged.
Start polymerization at 52℃ and increase the polymerization temperature to 65℃ at a conversion rate of 30%.
When the conversion rate is increased to 60%, vinyl chloride monomer is converted to 80%
Kg was charged, and the polymerization was further continued and the polymerization was stopped at a conversion rate of 100% (conversion rate of polyvinyl chloride to vinyl chloride monomer at the time of polymerization charge). bulk specific gravity of the polymer,
The measurement results of physical properties are shown in Table-2.
【表】
表−２から分散剤として鹸化度70％の部分鹸化
ポリ酢酸ビニルを使用すれば物性（伸び）が良い
ことが判る。[Table] Table 2 shows that the physical properties (elongation) are good when partially saponified polyvinyl acetate with a degree of saponification of 70% is used as a dispersant.
Claims (1)
合開始剤、水媒体の存在下に、第１段階重合とし
て、転化率50重量％以下まで重合し、ついで第２
段階重合として、第１段階の重合温度より５℃以
上高い温度で重合を続け、缶内圧力が降下開始以
前に、塩化ビニル系モノマーを追加し更に重合を
続け、第１段階重合時の重合体重量W1と最終重
合体重量W2が、（W2−W1）／W1≧1.0の関係式
を満足させるように重合して高嵩比重の塩化ビニ
ル系樹脂を得ることを特徴とする重合法。 ２ 分散剤が鹸化度65〜75％の部分鹸化ポリ酢酸
ビニルである特許請求の範囲第１項記載の重合
法。 ３ 第１段階の重合温度が30〜55℃である特許請
求の範囲第１項記載の重合法。 ４ 生成重合体重量比（W2−W1）／W1が（W2
−W1）／W1≧1.5である特許請求の範囲第１項
記載の重合法。 ５ 第１段階重合転化率が20〜40重量％である特
許請求の範囲第１項記載の重合法。[Scope of Claims] 1. A vinyl chloride monomer is polymerized in the presence of a dispersant, an oil-soluble polymerization initiator, and an aqueous medium to a conversion rate of 50% by weight or less as a first stage polymerization, and then a second stage polymerization is performed.
In step polymerization, polymerization is continued at a temperature 5°C or more higher than the polymerization temperature of the first stage, and before the pressure inside the reactor starts to drop, vinyl chloride monomer is added and polymerization is continued, resulting in the polymerization at the time of the first stage polymerization. A vinyl chloride resin with a high bulk specific gravity is obtained by polymerizing so that the weight W 1 and the final polymer weight W 2 satisfy the relational expression (W 2 − W 1 )/W 1 ≧1.0. Polymerization method. 2. The polymerization method according to claim 1, wherein the dispersant is partially saponified polyvinyl acetate having a degree of saponification of 65 to 75%. 3. The polymerization method according to claim 1, wherein the polymerization temperature in the first stage is 30 to 55°C. 4 Weight ratio of produced polymer (W 2 - W 1 )/W 1 is (W 2
-W 1 )/W 1 ≧1.5, the polymerization method according to claim 1. 5. The polymerization method according to claim 1, wherein the first stage polymerization conversion rate is 20 to 40% by weight.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4391183A JPS59168008A (en) | 1983-03-15 | 1983-03-15 | Polymerization of vinyl chloride |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4391183A JPS59168008A (en) | 1983-03-15 | 1983-03-15 | Polymerization of vinyl chloride |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS59168008A JPS59168008A (en) | 1984-09-21 |
| JPH0150322B2 true JPH0150322B2 (en) | 1989-10-30 |
Family
ID=12676894
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4391183A Granted JPS59168008A (en) | 1983-03-15 | 1983-03-15 | Polymerization of vinyl chloride |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS59168008A (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0780926B2 (en) * | 1988-08-19 | 1995-08-30 | サン・アロー化学株式会社 | Method for producing vinyl chloride resin powder |
| KR100899985B1 (en) | 2006-06-12 | 2009-05-28 | 주식회사 엘지화학 | Method for production of vinyl chloride-based polymer by suspension polymerization |
| KR100983702B1 (en) | 2006-08-22 | 2010-09-24 | 주식회사 엘지화학 | Methods of preparing a vinyl chloride polymer having superior workability |
| EP2497787B1 (en) * | 2009-11-04 | 2016-01-13 | LG Chem, Ltd. | Vinyl chloride-based polymer |
| US9334344B2 (en) | 2010-09-22 | 2016-05-10 | Vinnolit Gmbh & Co. Kg | Process for the production of a polyvinyl-chloride (PVC) resin |
-
1983
- 1983-03-15 JP JP4391183A patent/JPS59168008A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS59168008A (en) | 1984-09-21 |
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