JPS6244004B2 - - Google Patents
Info
- Publication number
- JPS6244004B2 JPS6244004B2 JP5854884A JP5854884A JPS6244004B2 JP S6244004 B2 JPS6244004 B2 JP S6244004B2 JP 5854884 A JP5854884 A JP 5854884A JP 5854884 A JP5854884 A JP 5854884A JP S6244004 B2 JPS6244004 B2 JP S6244004B2
- Authority
- JP
- Japan
- Prior art keywords
- ethylene
- precursor composition
- olefin
- carbon atoms
- mol
- 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
- 239000000203 mixture Substances 0.000 claims description 99
- 239000002243 precursor Substances 0.000 claims description 60
- 150000001875 compounds Chemical class 0.000 claims description 42
- 238000000034 method Methods 0.000 claims description 41
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 40
- 239000005977 Ethylene Substances 0.000 claims description 40
- 239000007789 gas Substances 0.000 claims description 34
- 239000004711 α-olefin Substances 0.000 claims description 33
- 125000004432 carbon atom Chemical group C* 0.000 claims description 31
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 claims description 26
- 239000010936 titanium Substances 0.000 claims description 23
- 238000006243 chemical reaction Methods 0.000 claims description 19
- 239000002245 particle Substances 0.000 claims description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 18
- 229920001038 ethylene copolymer Polymers 0.000 claims description 17
- 239000012876 carrier material Substances 0.000 claims description 16
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 15
- 229910052719 titanium Inorganic materials 0.000 claims description 15
- 238000005054 agglomeration Methods 0.000 claims description 14
- 230000002776 aggregation Effects 0.000 claims description 14
- 239000003085 diluting agent Substances 0.000 claims description 14
- -1 aliphatic ethers Chemical class 0.000 claims description 13
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 13
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 13
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 claims description 13
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 12
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 12
- 229910052782 aluminium Inorganic materials 0.000 claims description 12
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 claims description 11
- 150000001993 dienes Chemical class 0.000 claims description 10
- 229910052739 hydrogen Inorganic materials 0.000 claims description 10
- 125000001931 aliphatic group Chemical group 0.000 claims description 9
- 239000001257 hydrogen Substances 0.000 claims description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 8
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 8
- 125000002029 aromatic hydrocarbon group Chemical group 0.000 claims description 6
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 6
- 239000000377 silicon dioxide Substances 0.000 claims description 6
- OJOWICOBYCXEKR-KRXBUXKQSA-N (5e)-5-ethylidenebicyclo[2.2.1]hept-2-ene Chemical group C1C2C(=C/C)/CC1C=C2 OJOWICOBYCXEKR-KRXBUXKQSA-N 0.000 claims description 5
- 239000011777 magnesium Substances 0.000 claims description 5
- 125000005907 alkyl ester group Chemical group 0.000 claims description 4
- 150000004292 cyclic ethers Chemical class 0.000 claims description 4
- 150000002430 hydrocarbons Chemical group 0.000 claims description 4
- 150000001338 aliphatic hydrocarbons Chemical group 0.000 claims description 3
- 238000010924 continuous production Methods 0.000 claims description 3
- 238000007334 copolymerization reaction Methods 0.000 claims description 3
- 229930195734 saturated hydrocarbon Natural products 0.000 claims description 3
- YONPGGFAJWQGJC-UHFFFAOYSA-K titanium(iii) chloride Chemical compound Cl[Ti](Cl)Cl YONPGGFAJWQGJC-UHFFFAOYSA-K 0.000 claims description 3
- 159000000032 aromatic acids Chemical class 0.000 claims 2
- XJDNKRIXUMDJCW-UHFFFAOYSA-J titanium tetrachloride Chemical compound Cl[Ti](Cl)(Cl)Cl XJDNKRIXUMDJCW-UHFFFAOYSA-J 0.000 claims 2
- 238000006116 polymerization reaction Methods 0.000 description 39
- 229920000642 polymer Polymers 0.000 description 33
- 239000003054 catalyst Substances 0.000 description 29
- 229920001577 copolymer Polymers 0.000 description 23
- 239000011541 reaction mixture Substances 0.000 description 21
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 18
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 14
- 150000001336 alkenes Chemical class 0.000 description 13
- 230000004913 activation Effects 0.000 description 12
- 239000000243 solution Substances 0.000 description 12
- 230000003213 activating effect Effects 0.000 description 11
- 150000002681 magnesium compounds Chemical class 0.000 description 11
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 10
- 150000003609 titanium compounds Chemical class 0.000 description 10
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 7
- 229920000573 polyethylene Polymers 0.000 description 7
- 238000007865 diluting Methods 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- 239000000155 melt Substances 0.000 description 6
- 238000001035 drying Methods 0.000 description 5
- 239000000178 monomer Substances 0.000 description 5
- 239000002904 solvent Substances 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- YNLAOSYQHBDIKW-UHFFFAOYSA-M diethylaluminium chloride Chemical compound CC[Al](Cl)CC YNLAOSYQHBDIKW-UHFFFAOYSA-M 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000000284 extract Substances 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- VOITXYVAKOUIBA-UHFFFAOYSA-N triethylaluminium Chemical compound CC[Al](CC)CC VOITXYVAKOUIBA-UHFFFAOYSA-N 0.000 description 4
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- 238000011109 contamination Methods 0.000 description 3
- 238000005470 impregnation Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000011236 particulate material Substances 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 238000010926 purge Methods 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- ORYGRKHDLWYTKX-UHFFFAOYSA-N trihexylalumane Chemical compound CCCCCC[Al](CCCCCC)CCCCCC ORYGRKHDLWYTKX-UHFFFAOYSA-N 0.000 description 3
- LIKMAJRDDDTEIG-UHFFFAOYSA-N 1-hexene Chemical compound CCCCC=C LIKMAJRDDDTEIG-UHFFFAOYSA-N 0.000 description 2
- WSSSPWUEQFSQQG-UHFFFAOYSA-N 4-methyl-1-pentene Chemical compound CC(C)CC=C WSSSPWUEQFSQQG-UHFFFAOYSA-N 0.000 description 2
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000002035 hexane extract Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- TZIHFWKZFHZASV-UHFFFAOYSA-N methyl formate Chemical compound COC=O TZIHFWKZFHZASV-UHFFFAOYSA-N 0.000 description 2
- 150000002899 organoaluminium compounds Chemical class 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 230000000379 polymerizing effect Effects 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 229920001897 terpolymer Polymers 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- PRBHEGAFLDMLAL-GQCTYLIASA-N (4e)-hexa-1,4-diene Chemical compound C\C=C\CC=C PRBHEGAFLDMLAL-GQCTYLIASA-N 0.000 description 1
- RYHBNJHYFVUHQT-UHFFFAOYSA-N 1,4-Dioxane Chemical compound C1COCCO1 RYHBNJHYFVUHQT-UHFFFAOYSA-N 0.000 description 1
- PRBHEGAFLDMLAL-UHFFFAOYSA-N 1,5-Hexadiene Natural products CC=CCC=C PRBHEGAFLDMLAL-UHFFFAOYSA-N 0.000 description 1
- HECLRDQVFMWTQS-RGOKHQFPSA-N 1755-01-7 Chemical compound C1[C@H]2[C@@H]3CC=C[C@@H]3[C@@H]1C=C2 HECLRDQVFMWTQS-RGOKHQFPSA-N 0.000 description 1
- INYHZQLKOKTDAI-UHFFFAOYSA-N 5-ethenylbicyclo[2.2.1]hept-2-ene Chemical compound C1C2C(C=C)CC1C=C2 INYHZQLKOKTDAI-UHFFFAOYSA-N 0.000 description 1
- DKPFZGUDAPQIHT-UHFFFAOYSA-N Butyl acetate Natural products CCCCOC(C)=O DKPFZGUDAPQIHT-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 239000002879 Lewis base Substances 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- CYTYCFOTNPOANT-UHFFFAOYSA-N Perchloroethylene Chemical group ClC(Cl)=C(Cl)Cl CYTYCFOTNPOANT-UHFFFAOYSA-N 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 229910010062 TiCl3 Inorganic materials 0.000 description 1
- 238000002441 X-ray diffraction Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 150000007933 aliphatic carboxylic acids Chemical class 0.000 description 1
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000000498 ball milling Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000012986 chain transfer agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229940125904 compound 1 Drugs 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000001739 density measurement Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- HJXBDPDUCXORKZ-UHFFFAOYSA-N diethylalumane Chemical compound CC[AlH]CC HJXBDPDUCXORKZ-UHFFFAOYSA-N 0.000 description 1
- HQWPLXHWEZZGKY-UHFFFAOYSA-N diethylzinc Chemical compound CC[Zn]CC HQWPLXHWEZZGKY-UHFFFAOYSA-N 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 238000000921 elemental analysis Methods 0.000 description 1
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000005227 gel permeation chromatography Methods 0.000 description 1
- 150000004820 halides Chemical class 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- PYGSKMBEVAICCR-UHFFFAOYSA-N hexa-1,5-diene Chemical compound C=CCCC=C PYGSKMBEVAICCR-UHFFFAOYSA-N 0.000 description 1
- FUZZWVXGSFPDMH-UHFFFAOYSA-N hexanoic acid Chemical compound CCCCCC(O)=O FUZZWVXGSFPDMH-UHFFFAOYSA-N 0.000 description 1
- OIPWQYPOWLBLMR-UHFFFAOYSA-N hexylalumane Chemical compound CCCCCC[AlH2] OIPWQYPOWLBLMR-UHFFFAOYSA-N 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 150000007527 lewis bases Chemical class 0.000 description 1
- OTCKOJUMXQWKQG-UHFFFAOYSA-L magnesium bromide Chemical compound [Mg+2].[Br-].[Br-] OTCKOJUMXQWKQG-UHFFFAOYSA-L 0.000 description 1
- 229910001623 magnesium bromide Inorganic materials 0.000 description 1
- BLQJIBCZHWBKSL-UHFFFAOYSA-L magnesium iodide Chemical compound [Mg+2].[I-].[I-] BLQJIBCZHWBKSL-UHFFFAOYSA-L 0.000 description 1
- 229910001641 magnesium iodide Inorganic materials 0.000 description 1
- 239000003550 marker Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 125000000956 methoxy group Chemical group [H]C([H])([H])O* 0.000 description 1
- 239000002480 mineral oil Substances 0.000 description 1
- 235000010446 mineral oil Nutrition 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 150000002902 organometallic compounds Chemical class 0.000 description 1
- 125000002524 organometallic group Chemical group 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- YWAKXRMUMFPDSH-UHFFFAOYSA-N pentene Chemical compound CCCC=C YWAKXRMUMFPDSH-UHFFFAOYSA-N 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 230000001568 sexual effect Effects 0.000 description 1
- 238000005029 sieve analysis Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 229950011008 tetrachloroethylene Drugs 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 150000003682 vanadium compounds Chemical class 0.000 description 1
Landscapes
- Polymerisation Methods In General (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
Description
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The present invention relates to a method for producing extremely low density and low modulus ethylene copolymers in a fluidized bed. More specifically, the present invention provides 0.91
The present invention relates to a process for the fluidized bed production of ethylene copolymers having a density of less than g/cm 3 and a 1% secant modulus of less than 140,000 KPa. Ethylene copolymers with densities between 0.91 g/cm 3 and 0.96 g/cm 3 are described in U.S. Pat.
As described in Japanese Patent No. 4302566, ethylene is converted into one or more higher α
It can be prepared in a fluidized bed by sequential copolymerization with olefin monomers, where the catalyst composition is prepared by (1) forming a precursor composition from a magnesium compound, a titanium compound, and an electron donating compound; 2) diluting the precursor composition with an inert carrier material; and (3) activating the precursor composition with an organoaluminum compound. The copolymers made according to these patents are relatively high modulus, stiff materials and are generally useful in making films and injection molded articles. However, these patents do not describe how low modulus copolymers with densities below 0.91 g/cm 3 can be prepared. Low modulus copolymers of this type are useful in tube and hose manufacturing and other applications where flexibility and toughness are desired. Attempts have been made to modify the process of said US patent to produce low modulus ethylene copolymers with densities less than 0.91 g/ cm3 , for example by increasing the concentration of higher alpha olefin comonomers in the reactor. However, it was found that sticky and rubbery polymer particles were produced. Due to their sticky nature, particles of this type tend to stick together and form large agglomerates. After a short period of time, these coagulums reach too large a size and cannot maintain fluidity in the reactor bed. As a result, reactor contamination caused by these large coagulums causes polymerization to stop after only a small amount of the desired copolymer has been produced. British Patent No. 2033910A, No. 2034336A, No.
No. 2034723A and No. 2066274A disclose the production of ethylene copolymers and terpolymers by polymerizing monomeric olefin mixtures in the gas phase in the presence of catalyst compositions; The catalyst composition includes (1) an organoaluminium compound and (2) a solid material containing a magnesium-containing compound and a titanium compound and/or a vanadium compound. However, these references suggest that if polymers with densities below 0.91 g/ cm3 are to be produced in a fluidized bed, the polymerization should be carried out continuously to avoid contamination of the reactor caused by particle agglomeration and to achieve high polymer production. The conditions necessary for sexual progression have not been reported. Furthermore, these references do not indicate how the polymerization can be carried out without subjecting the catalysts used to lengthy ball milling. British Patent Nos. 2006232A, 2053246A and
No. 2053935A discloses the production of ethylene copolymers and terpolymers by polymerizing monomeric olefin mixtures in a fluidized bed in the presence of a catalyst composition, where the catalyst composition is ( Contains 1) an organometallic component and (2) a titanium-containing component. However, these references also suggest that when attempting to produce polymers with densities below 0.91 g/ cm3 , it is necessary to avoid particle agglomeration and to maintain polymerization continuously and with high polymer productivity. Not reporting required conditions. Furthermore, these references do not indicate how the polymerization can be carried out without first producing a prepolymer. With the present invention, we now have a density of less than 0.91 g/ cm3 .
It has now been found that ethylene copolymers with a 1% secant modulus of less than 140 000 KPa can be produced continuously by a fluidized bed polymerization process, where (a )0.35:1~
A gas mixture containing ethylene and at least one higher alpha olefin in a higher alpha olefin to ethylene molar ratio of 8.0:1 and (b) 33 to 95 mole percent diluent gas is continuously contacted with the catalyst composition. ,
The catalyst composition comprises forming a precursor composition from a magnesium compound, a titanium compound, and an electron donating compound, diluting the precursor composition with an inert carrier, and activating the diluted precursor composition with an organoaluminum compound. Manufactured by Fluidized bed reactors suitable for continuous production of ethylene copolymers have been previously disclosed and are well known in the art. Fluidized bed reactors useful for this purpose include:
For example, it is described in US Pat. No. 4,302,565 and US Pat. No. 4,302,566, the disclosures of which are hereby incorporated by reference. These patents also disclose catalyst compositions suitable for producing copolymers of this type. To produce an ethylene copolymer with a density of less than 0.91 g/cm 3 by the fluidized bed process, the amount of ethylene used to produce a copolymer with a density greater than 0.91 g/cm 3 is used. It is necessary to use a gaseous reaction mixture containing a higher amount of higher alpha olefin comonomer than the amount of the higher alpha olefin comonomer. By adding successively increasing amounts of higher olefins of this type to the mixture, copolymers with progressively decreasing densities are obtained at any given melt index. The amount of higher olefin required to obtain a copolymer of a given density varies from olefin to olefin under the same conditions, and as the number of carbon atoms in the olefin decreases, more of this type of higher olefin is required. . Generally, to produce copolymers with densities less than 0.91 g/cm 3 at least
It is necessary to use a reaction mixture containing higher olefins and ethylene at a higher olefin to ethylene molar ratio of 0.35:1. Usually 0.35:1~
A mixture containing higher olefins and ethylene in a molar ratio of 8.0:1 was used for this purpose and 0.6:
A molar ratio of 1 to 7.0:1 is preferred. The higher alpha olefins that can be polymerized with ethylene to produce the low density and low modulus copolymers of this invention can have from 3 to 8 carbon atoms. These alpha olefins must not contain branching at any carbon atom closer than the two carbon atoms removed from the double bond. Suitable α-olefins are propylene, butene-1, pentene-1
1, hexene-1, 4-methylpentene-1, heptene-1 and octene-1. Preferred alpha-olefins are propylene, butene-1, hexene-1, 4-methylpentene-1 and octene-1.
It is 1. If desired, one or more dienes, conjugated or unconjugated, can also be present in the reaction mixture. Dienes of this type can be used in amounts of 0.1 mol % to 10 mol %, preferably 0.1 mol % to 8 mol % of the total gas mixture fed to the fluidized bed. Dienes of this type include, for example, butadiene, 1,4-hexadiene, 1,5-hexadiene, vinylnorbornene, ethylidenenorbornene and dicyclopentadiene. Preventing the formation of polymer coagulum when using reaction mixtures with high ratios of ethylene to higher alpha olefin comonomers required to produce the desired copolymers with densities below 0.91 g/ cm3 . It has also been found that in order to maintain the polymerization continuously it is necessary to dilute the reaction mixture with a large amount of diluent gas. Diluting the reaction mixture with diluent gas in this manner helps reduce the stickiness of the resulting polymer, which is a major cause of agglomeration. Typically, the diluent gas should constitute 33 mol% to 95 mol% of the total gas mixture fed to the fluidized bed to prevent agglomeration. Preferably, the gas mixture contains 40 mol% to 70 mol% of such gases. The term "diluent" gas refers to a gas that is non-reactive under the conditions used in the polymerization reactor, i.e., does not decompose under the polymerization conditions used in the reactor or decomposes the polymerizable monomers and catalyst composition. It means a gas that does not react with the components or terminate the chain growth of the polymer. Furthermore, such gases should be insoluble in the resulting polymer so that they do not contribute to the tackiness of the polymer. Such gases include nitrogen, argon, helium, methane, and ethane. Hydrogen can also be used as diluent gas. In this case, the dilution not only dilutes the reaction mixture and prevents agglomeration of the polymer, but also acts as a chain transfer agent to adjust the melt index of the copolymer produced by this method. Generally, the reaction mixture contains sufficient hydrogen to provide a hydrogen to ethylene molar ratio of 0.01:1 to 0.5:1. In addition to hydrogen, other chain transfer agents can also be used to adjust the melt index of the copolymer. Of course, the gaseous reaction mixture may include, for example, water, oxygen,
It must be substantially free of catalyst poisons such as carbon monoxide, carbon dioxide, acetylene, etc. In addition to diluting the reaction mixture with a diluent gas, it has also been found necessary to maintain relatively low temperatures in the reactor to prevent polymer agglomeration and to maintain continuous polymerization. The temperatures that can be used vary directly with the concentration of diluent gas present in such mixtures, with higher concentrations of diluent gas allowing slightly higher temperatures to be used without adverse effects. Similarly, the lower the concentration of higher alpha olefin comonomer in the reaction mixture relative to the concentration of ethylene, ie, the higher the density and modulus of the copolymer produced, the higher the temperature that can be used. However, generally
To continuously produce copolymers with densities less than 0.91 g/cm 3 and 1% secant modulus less than 140000 KPa while preventing polymer agglomeration, the temperature
Do not allow the temperature to rise above 80°C. On the other hand, the operating temperature must be sufficiently high to prevent substantial condensation of the reaction mixture, including the diluent gas, to a liquid state. This type of condensation causes the resulting polymer particles to stick together and exacerbates the polymer condensation problem. Generally, this difficulty is associated with the use of alpha olefins having 5 or more carbon atoms and having relatively high dew points. A certain degree of low condensation can be tolerated, but beyond this it inhibits the reaction. in general,
Density of 0.86g/ cm3 ~0.90g/ cm3 and 600KPa~
Temperatures between 10° C. and 60° C. are used to produce copolymers with a secant modulus of 100,000 KPa. Usually with a density of 0.90g/cm 3 to 0.91g/cm 3
Higher temperatures of 60<0>C to 80<0>C are used to produce copolymers with 1% secant moduli of 100,000 KPa to 140,000 KPa. Figure 2 shows the highest polymerization temperature that can be used to produce an ethylene copolymer with a given secant modulus without polymer agglomeration when the reaction mixture is diluted with 50 mole percent diluent gas. . The area above the line is the operable area, and the area below the line is the inoperable area. Pressures up to 7000 KPa can be used in this method, but pressures between 70 KPa and 2500 KPa are preferred. To maintain a usable fluidized bed, the surface gas velocity of the gaseous reaction mixture passing through the bed must exceed the minimum flow rate required for fluidization, and is preferably at least 0.2 feet per second higher than the minimum flow rate. It is. Generally, the surface gas velocity should not exceed 5.0 feet per second, and in particular, 2.5 feet per second or less is generally sufficient. The catalyst composition used in the process of the present invention comprises forming a precursor composition from a magnesium compound, a titanium compound, and an electron donating compound, diluting this precursor composition with an inert carrier, and diluting this precursor composition with an inert carrier. is produced by activating it with an organoaluminium compound. The precursor composition is made by dissolving at least one titanium compound and at least one magnesium compound in at least one electron donating compound at a temperature from about 20° C. to the boiling point of the electron donating compound. . The titanium compound can be added to the electron donor compound before, after, or simultaneously with the addition of the magnesium compound. Dissolution of the titanium and magnesium compounds can be facilitated by stirring these two compounds in an electron donating compound or, in some cases, by refluxing them. After the titanium compound and the magnesium compound are dissolved, the precursor composition is isolated by crystallization or by precipitation with an aliphatic or aromatic hydrocarbon having 5 to 8 carbon atoms, such as hexane, isopentane or benzene. can be released. The crystallized or precipitated precursor composition can be isolated as fine free-flowing particles having an average particle size of 10Ό to 100Ό after drying at temperatures up to 60°C. To prepare the precursor composition, titanium compound 1
0.5 to 56 mol per mol, preferably 1 mol to 10 mol of magnesium compound are used. The titanium compound used in preparing the precursor composition has the structural formula: Ti(OR) a X b [where R is an aliphatic or aromatic hydrocarbon group having 1 to 14 carbon atoms or COR' , where R' is an aliphatic or aromatic hydrocarbon group having 1 to 14 carbon atoms, and X is
selected from the group consisting of Cl, Br, I and mixtures thereof, a is 0, 1 or 2, b is 1-4, a
+b=3 or 4]. Suitable titanium compounds are TiCl 3 , TiCl 4 , Ti
( OCH3 ) Cl3 ,Ti( OC6H5 ) Cl3 , Ti
( OCOCH3 ) Cl3 and Ti ( OCOC6H5 ) Cl3 . TiCl3 is preferred. This is because catalysts containing this material exhibit high activity at the low temperatures and low monomer concentrations used in the process of the invention. The magnesium compound used in preparing the precursor composition has the structural formula: MgX 2 where X is selected from the group consisting of Cl, Br, I, and mixtures thereof. Suitable magnesium compounds include MgCl2 , MgBr2 and MgI2 . Anhydrous MgCl2 is particularly preferred. The electron donating compound used in preparing the precursor composition is an organic compound that is liquid at 25° C. and in which the titanium and magnesium compounds are soluble. Electron donating compounds are known per se or as Lewis bases. Suitable electron donating compounds include alkyl esters of aliphatic or aromatic carboxylic acids, aliphatic ethers, cyclic ethers and aliphatic ketones.
Among these electron donating compounds, preferable ones are 1-
Alkyl esters of saturated aliphatic carboxylic acids with 4 carbon atoms, alkyl esters of aromatic carboxylic acids with 7-8 carbon atoms, 2-8
aliphatic ethers with 4 to 5 carbon atoms, preferably 4 to 5 carbon atoms, cyclic ethers with 4 to 5 carbon atoms, preferably mono- or di-ethers with 4 carbon atoms and 3 to 6 carbon atoms. carbon atoms, preferably 3 to 4 carbon atoms. Particularly preferred of these electron donating compounds include methyl formate, ethyl acetate, butyl acetate, ethyl ether, tetrahydrofuran, dioxane, acetone and methyl ethyl ketone. After the precursor composition is prepared, it is diluted with an inert carrier material by (1) mechanical mixing or (2) impregnation of the composition into the carrier material. Mechanical mixing of the inert carrier and the precursor composition is accomplished by combining the materials by conventional techniques. The combined mixture preferably contains from 3% to 50% by weight of the precursor composition. Impregnation of the inert carrier material with the precursor composition is carried out by dissolving the precursor composition in an electron donating compound and then mixing the dissolved precursor composition with the support to impregnate the support. Can be done. The solvent is then removed by drying at a temperature of up to 85°C. Alternatively, by adding the support to a solution of the chemical raw materials used to make the precursor composition in an electron-donating compound, the precursor composition can be supported without isolating the precursor composition from this solution. It is also possible to impregnate the body. Excess electron donor compound is then removed by drying at temperatures up to 85°C. When prepared as described above, the mixed or impregnated precursor composition has the formula: Mg n Ti (OR) o X p [ED] q where R is an aliphatic group having 1 to 14 carbon atoms or an aromatic hydrocarbon group or COR', where R' is also an aliphatic or aromatic hydrocarbon group having 1 to 14 carbon atoms, and X is
selected from the group consisting of Cl, Br, I and mixtures thereof, ED is an electron donating compound, m is 0.5-56, preferably 1.5-5, n is 0, 1 or 2, p is 2 -116, preferably 6-14, and q is 2-85, preferably 3-10]. Preferably, the impregnated carrier material contains from 3% by weight.
Contains 50% by weight, preferably 10% to 30% by weight of the precursor composition. The carrier material used to dilute the precursor composition is a solid, particulate, porous material that is inert to the other components of the catalyst composition and to the other active components of the reaction system. These carrier materials are
For example, inorganic materials such as oxides of silicon and/or aluminum are included. Carrier material is 10
It is used as a dry powder with an average particle size of Ό to 250Ό, preferably 20Ό to 150Ό. moreover,
These materials are porous and have a surface area of at least 3 m 2 per gram, preferably at least 50 m 2 per gram. The catalyst activity or productivity is at least
A clear improvement can be achieved by using silica supports with an average pore size of 80 Ã
units, preferably at least 100 Ã
units. The carrier material must be dry, ie it must not contain absorbed water. The drying of the carrier material can be, for example, at least as long as silica is used as the support.
This can be done by heating at a temperature of 600°C. Alternatively, if silica is used, this is at least
It can be dried at a temperature of 200 DEG C. and treated with 1% to 8% by weight of one or more aluminum activating compounds as described below. By modifying the support with an aluminum compound in this way, a catalyst composition with improved activity can be obtained, and the morphology of the polymer particles of the resulting ethylene copolymer can also be improved. Additionally, other organometallic compounds can be used to modify the support, such as diethylzinc. To be useful in making ethylene copolymers, the precursor composition must be a compound capable of converting titanium atoms in the precursor composition to a state where ethylene is effectively copolymerized with higher alpha-olefins. We must revitalize it. Such activation can be achieved by following the structural formula : Al ( Râ³) d This is carried out using an organoaluminum compound having a saturated hydrocarbon group which may or may not be present, e is 0 to 1.5, f is 0 or 1, and d+e+f=3. Activation compounds of this type can be used individually or in combination, for example Al(C 2 H 5 ) 3 , Al
(C 2 H 5 ) 2 Cl, Al 2 (C 2 H 5 ) 3 Cl 3 , Al (C 2 H 5 ) 2 H, Al
(C 2 H 5 ) 2 (OC 2 H 5 ), Al(i-C 4 H 9 ) 3 , Al(i-
Includes compounds such as C4H9 ) 2H , Al ( C6H12 ) 3 and Al ( C8H17 ) 3 . If desired, the precursor composition can be partially activated before it is introduced into the polymerization reactor. However, activation performed outside the polymerization reactor should be limited to the addition of an amount of activating compound that does not raise the molar ratio of activating compound to electron donor in the precursor composition higher than 1.4:1. It is. Preferably, when the activation is carried out in this way outside the reactor, the activating compound is present in a ratio of 0.1:1 to
An amount is used to provide the precursor composition with a 1.0:1 molar ratio of activating compound to electron donor. Such partial activation is carried out in a hydrocarbon solvent slurry and the resulting mixture is then dried to remove the solvent at 20°C to 80°C, preferably 50°C to 70°C. The resulting product is a free-flowing, solid, particulate material that can be easily fed to a polymerization reactor where activation is completed with additional activating compound, which may be the same or different. Alternatively, if an impregnated precursor composition is used, this can be used as described in European Patent Publication No.
It is also possible to carry out complete activation in the polymerization reactor without prior activation outside the reactor as described in Publication No. 12148. The partially activated or not fully activated precursor composition and the required amount of activation compound necessary to complete activation of the precursor composition preferably have separate supply routes. is fed to the reactor via The activating compound can be, for example, isopentane,
It can be sprayed into the reactor as a solution thereof in a hydrocarbon solvent such as hexane or mineral oil. This solution generally contains 2% to 30% by weight of activated compound. The activation compound is present in the reactor at a concentration of 10:1 to 400:1, preferably 25:1 to 60:1.
is added to the reactor in an amount to give a total aluminum to titanium molar ratio of . In the continuous gas phase fluidized bed process disclosed herein, individual portions of a partially activated or not fully activated precursor composition are is continuously fed to the reactor as the polymerization process continues, along with the individual portions of activating compound needed to complete the activation of the unactivated precursor composition. , replenishing the active catalyst sites consumed during the course of the reaction. By operating under the polymerization conditions described herein, ethylene is synthesized in a fluidized bed into one or more higher α
Continuously polymerize with olefin and optionally one or more dienes to produce 0.91 g/
Ethylene polymers can be produced with densities less than cm 3 and 1% secant modulus less than 140000 KPa. As used herein, the term "continuously polymerized" refers to polymerization over several weeks at a time, i.e., at least 168 hours, without contamination of the reactor by the formation of large aggregates of polymer.
Usually refers to the ability of uninterrupted polymerization for more than 1000 hours. The copolymers produced by the method of the invention generally have a density of 0.86 g/cm to 0.90 g/cm and a density of 600 KPa to 600 KPa.
It has a 1% secant modulus of 100000KPa. Copolymers of this type contain up to 94 mole percent polymerized ethylene, at least 6 mole percent polymerized alpha-olefins having from 3 to 8 carbon atoms, and optionally polymerized dienes. If a polymerized diene is present, the polymer contains 0.01 mol% to 10 mol% of at least one such diene and 6 mol% to 55 mol% of at least one polymerized diene having 3 to 8 carbon atoms. It contains α-olefin and 35 mol% to 94 mol% of polymerized ethylene. The molar ratio of propylene to ethylene that must be used in the reaction mixture to produce a copolymer with a given propylene content is shown in Table 1 below. When using alpha-olefins higher than propylene, similar results can be obtained with a lower ratio of such higher alpha-olefins to ethylene in the reaction mixture.
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ãèŠçŽããŠããã[Table] The ethylene polymer produced by the method of the present invention has a
It preferably has a standard or normal load melt index of 0.2 g/10 min to 4.0 g/10 min. Polymers of this type have a high load melt index (HLMI) of greater than 0 g/10 min and up to 1000 g/10 min. The melt index of a polymer varies inversely with its molecular weight and is a function of the polymerization temperature of the reaction, the density of the polymer, and the hydrogen/monomer ratio in the reaction system. For example, the melt index is increased by increasing the polymerization temperature and/or by increasing the ratio of higher alpha olefins to ethylene in the reaction system and/or by increasing the hydrogen/monomer ratio. . The ethylene polymer produced by the method of the invention has a melt flow rate (MFR) of 22-40, preferably 26-35. Melt flow rate is another measure of the molecular weight distribution (Mw/Mn) of a polymer. twenty two~
A MFR in the range 40 corresponds to a Mw/Mn of 2.7 to 6.5, and a MFR in the range 26 to 35 corresponds to a Mw/Mn of 2.9 to 4.8.
Corresponds to Mn. Ethylene polymers produced by the process of the present invention have a residual catalyst content of less than 10 ppm at a productivity level of at least 100,000 pounds of polymer per pound of titanium as ppm of titanium metal.
The copolymer is made of titanium 1 by this type of catalyst composition.
Easily manufactured with productivity up to 500,000 pounds per pound of polymer. The ethylene polymers produced by the process of the present invention are particulate materials having average particle sizes on the order of 0.01 to 0.07 inches (0.25 to 1.8 mm), generally 0.02 to 0.05 inches (0.5 to 1.3 mm) in diameter. This particle size is important for the purpose of facilitating fluidization of the polymer particles in a fluidized bed reactor. Additionally, these particulate materials contain no more than 4.0% of fine particles having a diameter of less than 0.005 inches (0.13 mm). Ethylene polymers produced by the process of the present invention range from 16 pounds per square foot to 31 pounds per square foot (0.26 pounds per square foot).
It has a bulk density of ~0.50 g/cm 3 ). The following examples illustrate the method of the invention, but the scope of the invention is not limited thereto. The properties of the polymers produced in these examples were determined by the following test method: Density ASTM D-1505. Create a black and
Condition for 1 hour at 100°C to reach equilibrium crystallinity. Density measurements are then carried out on a density gradient column and density values are recorded as g/cm 3 . Melt Index (MI) ASTM D-1238, Condition E. Measure at 190°C and record as grams per 10 minutes. Flow Index (HLMI) ASTM D-1238, Condition F. Measure 10 times the weight used in the melt index test above. Melt Flow Ratio (MFR) The ratio of flow index to melt index. Productivity A sample of the resin product is incinerated and the weight percent ash content is determined. Since the ash consists essentially of catalyst, productivity corresponds to the number of pounds of polymer produced per pound of total catalyst consumed.
The amount of Ti, Mg and halides in the ash is determined by elemental analysis. Bulk Density ASTM D-1895, Method B. Pour the resin through a 3/8 inch (9.5 mm) diameter funnel into a 400 ml graduated cylinder to the 400 ml line without shaking the cylinder and determine the weight by difference. ASTM D-1921, Method A using a sample with an average particle size of 500 g.
Calculated from sieve analysis data measured according to The calculation is based on the weight fraction retained on the sieve. n-hexane extract (FDA tested for use in polyethylene films intended for food contact applications). A 200 in 2 (1290 cm 2 ) sample of 1.5 mil (0.038 mm) sized film is cut into 1 inch x 6 inch (25.4 mm x 152.4 mm) sized strips and weighed to the nearest 0.1 mg. Place these strips in a container and add 300ml of n-
Extract with hexane for 2 hours at 50±1°C. The extract is then decanted into a tared culture dish. After drying the extract in a vacuum desiccator, the culture dishes are weighed to the nearest 0.1 mg. The extract normalized to the initial weight of the sample is then recorded as the weight fraction of n-hexane extract. Molecular weight distribution, Mw/Mn gel permeation chromatography. Styrogel column packing: (The packing order of pore size is 10 7 , 10 5 ,
10 4 , 10 3 , 60 Ã
). The solvent is perchlorethylene at 117°C. Detection: Infrared at 3.45Ό. Melting point, °C Melting point was measured using a DuPont differential thermal analyzer, model 990.
The mold was used to measure film samples 5-6 mils (0.13-0.15 mm) thick. The sample was rapidly heated under nitrogen to 150°C, held isothermally at this temperature for 5 minutes, cooled at a rate of 10°C/min. to 50°C, and then cooled to a softening point at a rate of 10°C/min. Reheated until it reached . Crystallinity % Crystallinity was measured by X-ray diffraction using a Norelco XRG-500 X-ray refractometer under copper K irradiation. Crystallinity was calculated from the integrated intensity of (020) reflection. 1% secant modulus ASTM D-638. 10 inches x 0.5 inches (254mm
x 12.7mm) film strip to 5 inches (127mm)
Clamp at length and 0.2in./min. (5.1mm/
Deform at a Jio separation speed of 1 minute). Measure the force-extension trace. The secant modulus is 1 from the origin.
It is the slope of the line drawn to the load at % deformation.
Deformation is determined by crosshead position. Record the secant modulus as KPa, normalized by the undeformed cross-sectional area of the sample. Tensile strength and elongation ASTM D-638. 1 inch x 5 inch (25.4 mm
x 127mm) film strip to 2 inches (50.8mm)
Clamp at length and 20in/min. (508mm/
Deform at a Jio separation speed of 1 minute). Tensile strength is the engineering stress that occurs at break. Elongation at break is measured by tracking the deformation of a 1 inch gauge marker placed over the film sample and is reported as a %. Example 1 Impregnation of a support with a precursor (a) into 12 flasks equipped with a mechanical stirrer 41.8
g (0.439 mol) of anhydrous MgCl 2 and 2.5 grams of tetrahydrofuran (THF). To this mixture was added 27.7 g (0.146 mol) of TiCl 4 dropwise over a period of 30 minutes. The mixture was then heated at 60° C. for an additional 30 minutes to completely dissolve the material. 500 g of silica was dehydrated by heating at a temperature of 600° C. and slurried in 3 isopentane. While stirring this slurry, add 20% of triethylaluminum in hexane.
186 ml of the wt% solution was added over 15 minutes. The resulting mixture was then dried at 60° C. for about 4 hours under a nitrogen purge to obtain a dry, free-flowing powder containing 5.5% by weight aluminum alkyl. The treated silica was then added to the solution prepared above. The resulting slurry was stirred for 15 minutes and then dried at 60° C. for about 4 hours under a nitrogen purge to yield an impregnated free-flowing dry powder. (b) 29.0 g (0.146 mol) of TiCl 4
The procedure was repeated using TiCl3.0.33AlCl3 . Example 2 Preparation of Partially Activated Precursor (a) A silica-impregnated precursor composition prepared according to Example 1(a) was slurried in anhydrous isopentane of 3 and chlorinated in anhydrous hexane with stirring. A 20% by weight solution of diethylaluminium was added over 15 minutes. A solution of diethylaluminum chloride was used in an amount sufficient to provide 0.4 moles of this compound per mole of tetrahydrofuran in the precursor. After completing the addition of diethylaluminum chloride, add the trichloride in anhydrous hexane with stirring continued for an additional 15 to 30 minutes.
A 20% by weight solution of n-hexylaluminum was added in an amount sufficient to provide 0.6 moles of this compound per mole of tetrahydrofuran in the precursor. This mixture was then heated under a nitrogen purge for 65 min.
It was dried at a temperature of ±10° C. for about 4 hours to obtain a free-flowing dry powder. This material was stored under dry nitrogen until needed. (b) The silica-impregnated precursor composition prepared according to Example 1(b) was partially activated with diethylaluminum chloride and tri-n-hexylaluminum by the same procedure as in 2(a), but However, tri-n-hexylaluminum was used in an amount sufficient to provide 0.4 moles of this compound per mole of tetrahydrofuran in the precursor. (c) The silica-impregnated precursor composition prepared according to Example 1(b) was partially activated with diethylaluminum chloride and tri-n-hexylaluminum by the same procedure as in 2(a), but However, each compound has 1 tetrahydrofuran in the precursor.
Sufficient amount was used to give 0.3 moles of this compound per mole. Examples 3-4 Ethylene was copolymerized with butene-1 under various reaction conditions in a fluid bed reaction system similar to that described and exemplified in U.S. Pat. Nos. 4,302,565 and 4,302,566. The polymerization reactor had a lower section 10 feet (3.05 m) high and 13.5 inches (0.343 m) in diameter and an upper section 16 feet (4.88 m) high and 23.5 inches (0.597 m) in diameter. In each polymerization, prepared according to Example 1(a),
The silica-impregnated precursor composition, and partially activated according to Example 2(a), was fed to a polymerization reactor with a 5% solution of triethylaluminum in isopentane to give a ratio of 15:1 to 55:1. A fully activated catalyst having a molar ratio of aluminum to titanium was provided in the reactor. Table 2 below summarizes the reaction conditions used for each polymerization, the properties of the polymer produced in this polymerization, and the productivity of the catalyst system used, expressed as residual titanium in the copolymer.
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ãŠãããIt is noted that when the reaction temperature in Example 4 was increased to 65° C., fouling of the reactor occurred due to particle agglomeration, stopping the polymerization. Examples 5-6 Ethylene was copolymerized with propylene under various reaction conditions using the same fluidized bed reactor system and catalyst system used in Examples 3-4. Table 3 below summarizes the reaction conditions used for each polymerization and the properties of the polymer produced by this polymerization.
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It is noted that when using a reaction temperature of , particle agglomeration resulted in fouling of the reactor and terminated the polymerization. Examples 7-8 Ethylene was copolymerized with propylene under various reaction conditions using the same fluidized bed reactor system used in Examples 3-4. In each polymerization, a silica-impregnated precursor composition prepared according to Example 1(b) and partially activated according to Example 2(b) was co-polymerized with a 5% solution of triethylaluminum in isopentane. The reactor was fed with fully activated catalyst having an aluminum to titanium molar ratio of 40:1 to 55:1. Table 4 below summarizes the reaction conditions used for each polymerization, the properties of the polymers produced by these polymerizations, and the productivity of the catalyst system used, expressed as residual titanium in the copolymer.
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948TABLE It is noted that under the conditions used in Example 8, ethylene and butylene cannot be copolymerized. The reason for this is that the dew point of the reaction mixture exceeds the temperature of the bed. Furthermore, it is noted that increasing the propylene to ethylene ratio in Example 8 to 1.9 causes fouling of the reactor due to particle agglomeration, stopping the polymerization. Example 9 Ethylene was copolymerized with propylene and ethylidene norbornene using the same fluidized bed reactor system used in Examples 3-4. In this polymerization, a silica-impregnated precursor composition prepared according to Example 1(b) and partially activated according to Example 2(c) is copolymerized with a 5% solution of triethylaluminum in isopentane. to provide fully activated catalyst with an aluminum to titanium molar ratio of 24:1 into the reactor. Table 5 below summarizes the reaction conditions used for the polymerization and the properties of the polymer produced by this polymerization. Table 5 Example 9 Polymerization conditions Temperature, °C 50 Pressure, KPa 2075 Gas velocity, ft/sec 1.5 (m/sec) (0.46) Space-time yield (lb/hr./ft 3 ) 1.5 (Kg/hr./ m 3 ) (24) Propylene/ethylene molar ratio 0.91 Hydrogen/ethylene molar ratio 0.23 N 2 mol % in the reaction mixture 55.7 H 2 mol % in the reaction mixture 4.7 mol % ethylidene norbornene in the reaction mixture 4.3 Property density of the polymer , g/cm 3 0.902 Ethylidene norbornene content, mole % 2.3 Melt index, g/10min. 2.0 Flow index, g/10min. 74 Melt flow rate 37 Bulk density, lb/ft 3 19.4 (g/cm 3 ) (0.310 ) Average particle size, inch 0.02 (mm) (0.51) 1% secant modulus, KPa 93772 Tensile strength, KPa 5026 Elongation, % 948
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FIG. 1 is a flowchart showing the steps for preparing a catalyst composition used in the production of the ethylene copolymer of the present invention. Figure 2 shows the ratio of low modulus ethylene copolymers to reaction temperatures used to copolymerize ethylene with higher alpha olefins, such as propylene or butene, by a fluidized bed process using the catalyst composition of the present invention. % secant modulus graph for producing an ethylene copolymer with a given secant modulus without polymer agglomeration using a gas mixture containing 50 mole % diluent gas and a reactor pressure of 2000 KPa. indicates an operable polymerization temperature that can be used for
The area above the line is an operable area, and the area below the line is an inoperable area.
Claims (1)
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æ³ã[Scope of Claims] 1. 94 mol% or less of polymerized ethylene and at least 6
mol% of polymerized alpha-olefins having 3 to 8 carbon atoms, and with a density of less than 0.91 g/ cm3.
When producing an ethylene copolymer having a 1% secant modulus of less than 140000 KPa in a fluidized bed without particle agglomeration, a temperature of 10° to 80°C in the fluidized bed reaction zone and
At pressures below 7000KPa, (a) 0.35:1 to 8.0:1
ethylene and at least one having 3 to 8 carbon atoms in a molar ratio of higher alpha olefins to ethylene of
A gas mixture containing a higher α-olefin of species and (b) 33 to 95 mol % of at least one diluent gas is expressed by the formula: Mg n Ti (OR) o X p [ED] q [where R is an aliphatic or aromatic hydrocarbon radical having 1 to 14 carbon atoms or COR', where R' is an aliphatic or aromatic hydrocarbon radical having 1 to 14 carbon atoms; X is
ED is an organic electron donating compound selected from the group consisting of Cl, Br, I and mixtures thereof, and ED is selected from the group consisting of alkyl esters of aliphatic or aromatic acids, aliphatic ethers, cyclic ethers and aliphatic ketones. , m is 0.5 to 56, n is 0.1 or 2, p is 2 to 116, and q is 2 to 85]. the precursor composition is diluted with an inert carrier material and the formula: Al(Râ³) d Xâ² e H f [where Xâ² is Cl or OR, Râ³ and R is a saturated hydrocarbon having 1 to 14 carbon atoms, e is 0 to 1.5, f is 0 or 1, and d + e + f = 3. The molar ratio of aluminum to titanium is
A continuous production method for ethylene copolymerization, characterized in that it is completely activated using an amount of 10:1 to 400:1. 2. The method of claim 1, wherein the precursor composition is mechanically mixed with an inert carrier material and the blended mixture contains from 3% to 50% by weight of the precursor composition. 3. impregnating an inert carrier material with a precursor composition and having an impregnated carrier material of 3% to 50% by weight.
% of the precursor composition by weight. 4. A method according to any one of claims 1 to 3, wherein the inert carrier material is silica. 5. A method according to any of claims 1 to 4, wherein the gas mixture contains sufficient hydrogen to provide a hydrogen to ethylene molar ratio of 0.01:1 to 0.5:1. 6 High-grade α-olefin and ethylene in a ratio of 0.6:1 to
6. A method according to any of claims 1 to 5, wherein a molar ratio of higher alpha olefin to ethylene of 7.0:1 is present in the mixture. 7. A patent claim in which X and X' are Cl, [ED] is tetrahydrofuran, n is 0, m is 1.5 to 5, p is 6 to 14, and q is 3 to 10 The method according to any one of items 1 to 6. 8. The method according to any one of claims 1 to 7, wherein the precursor composition comprises magnesium chloride, titanium trichloride, and tetrahydrofuran. 9. The method according to any one of claims 1 to 7, wherein the precursor composition comprises magnesium chloride, titanium tetrachloride, and tetrahydrofuran. 10. The method according to any one of claims 1 to 9, wherein the higher α-olefin is propylene. 11. The method according to any one of claims 1 to 9, wherein the higher α-olefin is butene-1. 12. A method according to any one of claims 1 to 11, wherein the gas mixture contains nitrogen. 13 Containing not more than 94 mol % of polymerized ethylene and at least 6 mol % of polymerized α-olefin having 3 to 8 carbon atoms, and having a density of less than 0.91 g/cm 3
When producing an ethylene copolymer having a 1% secant modulus of less than 140000 KPa in a fluidized bed without particle agglomeration, a temperature of 10° to 80°C in the fluidized bed reaction zone and
At pressures below 7000KPa, (a) 0.35:1 to 8.0:1
ethylene and at least one having 3 to 8 carbon atoms in a molar ratio of higher alpha olefins to ethylene of
A gas mixture containing a higher α-olefin of species, (b) 33 to 95 mol % of at least one diluent gas, and (c) 0.1 mol % to 10 mol % of at least one diene is defined by the formula: Mg n Ti (OR) o X p [ED] q [wherein R is an aliphatic or aromatic hydrocarbon group having 1 to 14 carbon atoms or COR'; is an aliphatic or aromatic hydrocarbon group having 4 carbon atoms, and X is
ED is an organic electron donating compound selected from the group consisting of Cl, Br, I and mixtures thereof, and ED is selected from the group consisting of alkyl esters of aliphatic or aromatic acids, aliphatic ethers, cyclic ethers and aliphatic ketones. , m is 0.5 to 56, n is 0.1 or 2, p is 2 to 116, and q is 2 to 85]. the precursor composition is diluted with an inert carrier material and has the formula: Al(Râ³) d Xâ² e H f , where Xâ² is Cl or OR, Râ³ and R is a saturated hydrocarbon group having 1 to 14 carbon atoms, e is 0 to 1.5, f is 0 or 1, and d+e+f=3. The total aluminum to titanium molar ratio in
A continuous production method for ethylene copolymerization, characterized in that it is completely activated using an amount of 10:1 to 400:1. 14 Higher α-olefin and ethylene at 0.6:1
Claim 1 wherein a molar ratio of higher alpha olefin to ethylene is present in the mixture of ~7.0:1.
The method described in Section 3. 15. The method according to any one of claims 13 to 14, wherein the diene is ethylidene norbornene. 16 A patent claim in which X and X' are Cl, [ED] is tetrahydrofuran, n is 0, m is 1.5 to 5, p is 6 to 14, and q is 3 to 10 The method according to any one of items 13 to 15. 17. The method according to any one of claims 13 to 16, wherein the precursor composition consists of magnesium chloride, titanium trichloride, and tetrahydrofuran. 18. The method according to any one of claims 13 to 16, wherein the precursor composition consists of magnesium chloride, titanium tetrachloride, and tetrahydrofuran. 19. The method according to any one of claims 13 to 18, wherein the higher α-olefin is propylene. 20. The method according to any one of claims 13 to 18, wherein the higher α-olefin is butene-1. 21. A method according to any of claims 13 to 20, wherein the gas mixture contains nitrogen.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US48029683A | 1983-03-29 | 1983-03-29 | |
US480296 | 1983-03-29 | ||
US587005 | 1984-03-13 |
Publications (2)
Publication Number | Publication Date |
---|---|
JPS59230011A JPS59230011A (en) | 1984-12-24 |
JPS6244004B2 true JPS6244004B2 (en) | 1987-09-17 |
Family
ID=23907417
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP5854884A Granted JPS59230011A (en) | 1983-03-29 | 1984-03-28 | Manufacture of low density and low modulus ethylene copolymer in fluidized bed |
Country Status (2)
Country | Link |
---|---|
JP (1) | JPS59230011A (en) |
ZA (1) | ZA842306B (en) |
Families Citing this family (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS61213238A (en) * | 1985-03-19 | 1986-09-22 | Nippon Yunikaa Kk | Flame-retardant polyolefin composition |
JP2584610B2 (en) * | 1985-04-17 | 1997-02-26 | æ¥æ¬ãŠãã«ãŒ æ ªåŒäŒç€Ÿ | Electric wires and cables |
JPS61284439A (en) * | 1985-06-11 | 1986-12-15 | å矜ååŠå·¥æ¥æ ªåŒäŒç€Ÿ | Heat-resistant laminate |
JPH072798B2 (en) * | 1987-10-28 | 1995-01-18 | äœåååŠå·¥æ¥æ ªåŒäŒç€Ÿ | Solid catalyst component for olefin polymerization |
JPH02206548A (en) * | 1989-02-07 | 1990-08-16 | Nippon Unicar Co Ltd | Wrap film |
JPH0376645A (en) * | 1989-08-21 | 1991-04-02 | Nippon Unicar Co Ltd | Wrapping film |
JP2568127B2 (en) * | 1990-03-09 | 1996-12-25 | æ¥æ¬ãŠãã«ãŒæ ªåŒäŒç€Ÿ | Stretch wrap film |
FR2800379A1 (en) * | 1999-10-29 | 2001-05-04 | Bp Chemicals Snc | PROCESS OF GAS-PHASE COPOLYMERIZATION OF AT LEAST TWO ALPHA-OLEFINS HAVING 2 TO 12 CARBON ATOMS |
-
1984
- 1984-03-28 ZA ZA842306A patent/ZA842306B/en unknown
- 1984-03-28 JP JP5854884A patent/JPS59230011A/en active Granted
Also Published As
Publication number | Publication date |
---|---|
ZA842306B (en) | 1984-11-28 |
JPS59230011A (en) | 1984-12-24 |
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