RU97111880A - Способ получения полиэтилена - Google Patents
Способ получения полиэтиленаInfo
- Publication number
- RU97111880A RU97111880A RU97111880/04A RU97111880A RU97111880A RU 97111880 A RU97111880 A RU 97111880A RU 97111880/04 A RU97111880/04 A RU 97111880/04A RU 97111880 A RU97111880 A RU 97111880A RU 97111880 A RU97111880 A RU 97111880A
- Authority
- RU
- Russia
- Prior art keywords
- stage
- reactor
- polymerization
- circulation
- ethylene
- Prior art date
Links
- 229920000573 polyethylene Polymers 0.000 title claims 10
- -1 POLYETHYLENE Polymers 0.000 title claims 6
- 239000004698 Polyethylene (PE) Substances 0.000 title claims 6
- 238000004519 manufacturing process Methods 0.000 title 1
- 238000006116 polymerization reaction Methods 0.000 claims 17
- 238000006243 chemical reaction Methods 0.000 claims 5
- 239000012071 phase Substances 0.000 claims 5
- 239000004215 Carbon black (E152) Substances 0.000 claims 4
- 239000005977 Ethylene Substances 0.000 claims 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims 4
- 150000002430 hydrocarbons Chemical class 0.000 claims 4
- 239000001257 hydrogen Substances 0.000 claims 4
- 229910052739 hydrogen Inorganic materials 0.000 claims 4
- 239000000155 melt Substances 0.000 claims 4
- 239000003054 catalyst Substances 0.000 claims 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims 3
- 229920000642 polymer Polymers 0.000 claims 3
- 239000007789 gas Substances 0.000 claims 2
- 239000000203 mixture Substances 0.000 claims 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims 2
- 239000001294 propane Substances 0.000 claims 2
- 239000011541 reaction mixture Substances 0.000 claims 2
- 239000004711 α-olefin Substances 0.000 claims 2
- LIKMAJRDDDTEIG-UHFFFAOYSA-N 1-Hexene Chemical compound CCCCC=C LIKMAJRDDDTEIG-UHFFFAOYSA-N 0.000 claims 1
- WSSSPWUEQFSQQG-UHFFFAOYSA-N 4-Methyl-1-pentene Chemical compound CC(C)CC=C WSSSPWUEQFSQQG-UHFFFAOYSA-N 0.000 claims 1
- XWJMQJGSSGDJSY-UHFFFAOYSA-N 4-methyloct-1-ene Chemical compound CCCCC(C)CC=C XWJMQJGSSGDJSY-UHFFFAOYSA-N 0.000 claims 1
- 238000009835 boiling Methods 0.000 claims 1
- 230000003197 catalytic Effects 0.000 claims 1
- 239000012295 chemical reaction liquid Substances 0.000 claims 1
- 239000007795 chemical reaction product Substances 0.000 claims 1
- 239000012467 final product Substances 0.000 claims 1
- 150000002431 hydrogen Chemical class 0.000 claims 1
- 239000007788 liquid Substances 0.000 claims 1
- 239000007791 liquid phase Substances 0.000 claims 1
- 239000000178 monomer Substances 0.000 claims 1
- 238000003541 multi-stage reaction Methods 0.000 claims 1
- 239000002491 polymer binding agent Substances 0.000 claims 1
- 230000000379 polymerizing Effects 0.000 claims 1
- 239000000047 product Substances 0.000 claims 1
- 239000012429 reaction media Substances 0.000 claims 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 claims 1
Claims (13)
1. Способ получения полиэтиленовых композиций в присутствии каталитической системы из этиленполимеризующих катализатора и сокатализатора в многостадийной реакционной последовательности, состоящей из последовательных жидкофазной и газофазной полимеризации, отличающийся тем, что способ содержит по крайней мере одну непрерывную реакционную последовательность, в которой на первой стадии этилен и, необязательно, водород и сомономер полимеризуются в реакторе с циркуляцией в среде низкокипящего углеводорода в присутствии этиленполимеризующих катализатора и сокатализатора, причем время пребывания и реакционная температура являются такими, что пропорция полимера этилена, полученного в реакторе, от конечного продукта способа составляет 1 - 20 мас. %, реакционная смесь, выведенная с первой стадии, поступает на вторую стадию, где полимеризация продолжается в реакторе с циркуляцией при добавлении этилена, водорода и, необязательно, инертного углеводорода, сомономеров и сокатализаторов, причем время пребывания составляет не менее 10 мин, реакционная смесь выводится из реактора с циркуляцией, по крайней мере значительная часть реакционной среды удаляется, и полимер поступает на третью стадию, где полимеризация осуществляется в газофазном реакторе в присутствии добавленных этилена и, необязательно, водорода, сомономеров и сокатализаторов.
2. Способ по п. 1, отличающийся тем, что катализатор подается только на указанную первую стадию полимеризации, а сокатализатор подается на указанную первую стадию полимеризации и, необязательно, в реактор с циркуляцией второй и/или третьей стадии и/или газофазный реактор.
3. Способ по п. 1 или 2, отличающийся тем, что в реакторе с циркуляцией указанной первой стадии полимеризации индекс расплава полученного полимера является ниже индекса расплава полимера, полученного в реакторе с циркуляцией последней стадии полимеризации.
4. Способ по п. 3, отличающийся тем, что на первой стадии полимеризации условия полимеризации выбираются так, что индекс расплава I2 полученного полимера этилена составляет 0,01 - 50, а на второй стадии полимеризации условия выбираются так, что индекс расплава I2 полиэтиленовой фракции составляет 10 - 2000.
5. Способ по пп. 1-4, отличающийся тем, что отношение молекулярной массы полимера этилена, полученного на первой стадии полимеризации, к молекулярной массе конечного продукта, выводимого с указанной третьей стадии полимеризации, составляет 0,25 - 5.
6. Способ по пп. 1-5, отличающийся тем, что реакционная температура в реакторе с циркуляцией указанной первой стадии полимеризации составляет 20 - 100oС, предпочтительно 40 - 80oС, а время пребывания составляет 10 мин - 2 ч.
7. Способ по пп. 1-6, отличающийся тем, что в реакторе с циркуляцией в качестве инертного углеводорода используется пропан, и реакционное давление и реакционная температура в реакторе с циркуляцией второй стадии выбираются так, что реакционная жидкость, образованная инертным углеводородом, мономером и водородом, находится в сверхкритическом состоянии.
8. Способ по пп. 1-7, отличающийся тем, что в реакторе с циркуляцией первой стадии полимеризации получается полиэтилен, имеющий молекулярную массу 150000 - 600000 и плотность 940 - 970 кг/м3, и тем, что в реакторе с циркуляцией второй стадии полимеризации получается полиэтилен, имеющий молекулярную массу 500 - 50000 и плотность между 950 - 980 кг/м3.
9. Способ по п. 3, отличающийся тем, что в реакторе с циркуляцией первой стадии полимеризации получается полиэтилен, имеющий молекулярную массу менее 400000.
10. Способ по пп. 1-7, отличающийся тем, что на первой стадии полимеризации в реакторе с циркуляцией подается в качестве сомономера такое количество С4-8-альфа-олефинов, что плотность продукта, полученного в реакторе, составляет 910 - 950 кг/м3.
11. Способ по п. 10, отличающийся тем, что сомономер выбирается из группы, состоящей из 1-бутена, 1-гексена, 4-метил-1-пентена, 1-октена или их смесей.
12. Способ по пп. 1-11, отличающийся тем, что С4-8-альфа-олефины подаются в качестве сомономера в газофазный реактор третьей стадии полимеризации.
13. Способ по пп. 1-12, отличающийся тем, что пропан подается в газофазный реактор через смеситель либо в жидком, либо в газообразном состоянии, либо в том и другом.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FI945926 | 1994-12-16 | ||
FI945926A FI96216C (fi) | 1994-12-16 | 1994-12-16 | Prosessi polyeteenin valmistamiseksi |
Publications (2)
Publication Number | Publication Date |
---|---|
RU97111880A true RU97111880A (ru) | 1999-06-10 |
RU2161625C2 RU2161625C2 (ru) | 2001-01-10 |
Family
ID=8541997
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
RU97111880/04A RU2161625C2 (ru) | 1994-12-16 | 1995-12-08 | Способ получения полимеров этилена |
Country Status (20)
Country | Link |
---|---|
US (1) | US5684097A (ru) |
EP (1) | EP0797599B1 (ru) |
JP (1) | JP3743847B2 (ru) |
KR (1) | KR100411381B1 (ru) |
CN (1) | CN1093863C (ru) |
AR (1) | AR000359A1 (ru) |
AT (1) | ATE177437T1 (ru) |
AU (1) | AU706963B2 (ru) |
BR (1) | BR9510034A (ru) |
CA (1) | CA2207910C (ru) |
CZ (1) | CZ290644B6 (ru) |
DE (1) | DE69508277T2 (ru) |
ES (1) | ES2129878T3 (ru) |
FI (1) | FI96216C (ru) |
GR (1) | GR3029896T3 (ru) |
IL (1) | IL116315A (ru) |
MY (1) | MY112607A (ru) |
RU (1) | RU2161625C2 (ru) |
WO (1) | WO1996018662A1 (ru) |
ZA (1) | ZA9510501B (ru) |
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DE2803281C2 (de) * | 1978-01-26 | 1982-12-02 | Chemische Werke Hüls AG, 4370 Marl | Verfahren zur mehrstufigen Polymerisation von Äthylen, allein oder zusammen mit anderen Olefinen |
JPS5910724B2 (ja) * | 1979-08-24 | 1984-03-10 | 旭化成株式会社 | エチレンの連続重合法 |
JPS5928573B2 (ja) * | 1980-02-05 | 1984-07-13 | チッソ株式会社 | α−オレフイン重合体の製造方法 |
JPS6023764B2 (ja) * | 1980-02-27 | 1985-06-10 | チッソ株式会社 | α−オレフイン重合体を製造する方法 |
CA1162700A (en) * | 1981-01-30 | 1984-02-21 | Kiyoshi Kawai | Process for producing ethylene polymers |
US4740550A (en) * | 1986-06-18 | 1988-04-26 | Shell Oil Company | Multistage copolymerization process |
FR2659338B1 (fr) * | 1990-03-09 | 1993-05-07 | Bp Chemicals Snc | Procedes et dispositifs de polymerisation catalytique d'alpha-olefines en phase gazeuse. |
FI86867C (fi) * | 1990-12-28 | 1992-10-26 | Neste Oy | Flerstegsprocess foer framstaellning av polyeten |
EP0580930B1 (en) * | 1992-07-31 | 1996-11-20 | Fina Research S.A. | Process for producing polyethylene having a broad molecular weight distribution |
FI98819C (fi) * | 1993-03-26 | 1997-08-25 | Borealis Polymers Oy | Prosessi olefiinipolymeerien valmistamiseksi ja prosessilla valmistetut tuotteet |
FI96745C (fi) * | 1993-07-05 | 1996-08-26 | Borealis Polymers Oy | Menetelmä olefiinien polymeroimiseksi leijupetipolymerointireaktorissa |
-
1994
- 1994-12-16 FI FI945926A patent/FI96216C/fi active
-
1995
- 1995-06-07 US US08/475,842 patent/US5684097A/en not_active Expired - Lifetime
- 1995-12-08 EP EP95939301A patent/EP0797599B1/en not_active Expired - Lifetime
- 1995-12-08 DE DE69508277T patent/DE69508277T2/de not_active Expired - Lifetime
- 1995-12-08 CZ CZ19971840A patent/CZ290644B6/cs not_active IP Right Cessation
- 1995-12-08 JP JP51830596A patent/JP3743847B2/ja not_active Expired - Lifetime
- 1995-12-08 AU AU41183/96A patent/AU706963B2/en not_active Expired
- 1995-12-08 AT AT95939301T patent/ATE177437T1/de not_active IP Right Cessation
- 1995-12-08 WO PCT/FI1995/000670 patent/WO1996018662A1/en active IP Right Grant
- 1995-12-08 ES ES95939301T patent/ES2129878T3/es not_active Expired - Lifetime
- 1995-12-08 RU RU97111880/04A patent/RU2161625C2/ru active
- 1995-12-08 CN CN95197319A patent/CN1093863C/zh not_active Expired - Lifetime
- 1995-12-08 CA CA002207910A patent/CA2207910C/en not_active Expired - Lifetime
- 1995-12-08 BR BR9510034A patent/BR9510034A/pt not_active IP Right Cessation
- 1995-12-10 IL IL11631595A patent/IL116315A/xx not_active IP Right Cessation
- 1995-12-11 ZA ZA9510501A patent/ZA9510501B/xx unknown
- 1995-12-14 MY MYPI95003872A patent/MY112607A/en unknown
- 1995-12-15 AR AR33463995A patent/AR000359A1/es unknown
- 1995-12-15 KR KR1019950050380A patent/KR100411381B1/ko not_active IP Right Cessation
-
1999
- 1999-04-07 GR GR990400987T patent/GR3029896T3/el unknown
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