CA2277294A1 - Metal halide solid acids and supported metal halides as catalysts for the preparation of hydrocarbon resins - Google Patents
Metal halide solid acids and supported metal halides as catalysts for the preparation of hydrocarbon resins Download PDFInfo
- Publication number
- CA2277294A1 CA2277294A1 CA002277294A CA2277294A CA2277294A1 CA 2277294 A1 CA2277294 A1 CA 2277294A1 CA 002277294 A CA002277294 A CA 002277294A CA 2277294 A CA2277294 A CA 2277294A CA 2277294 A1 CA2277294 A1 CA 2277294A1
- Authority
- CA
- Canada
- Prior art keywords
- metal halide
- monomers
- catalyst
- feed stream
- molecular weight
- 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.)
- Abandoned
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 265
- 229910001507 metal halide Inorganic materials 0.000 title claims abstract description 106
- 150000005309 metal halides Chemical class 0.000 title claims abstract description 106
- 239000011973 solid acid Substances 0.000 title claims abstract description 71
- 239000013032 Hydrocarbon resin Substances 0.000 title claims abstract description 53
- 229920006270 hydrocarbon resin Polymers 0.000 title claims abstract description 53
- 238000002360 preparation method Methods 0.000 title description 18
- 239000000178 monomer Substances 0.000 claims abstract description 208
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 76
- 238000006243 chemical reaction Methods 0.000 claims description 110
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 90
- 239000002904 solvent Substances 0.000 claims description 66
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 claims description 60
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 claims description 56
- 238000000034 method Methods 0.000 claims description 46
- 239000002841 Lewis acid Substances 0.000 claims description 45
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 45
- 150000007517 lewis acids Chemical class 0.000 claims description 42
- 239000000377 silicon dioxide Substances 0.000 claims description 42
- 239000011592 zinc chloride Substances 0.000 claims description 38
- 235000005074 zinc chloride Nutrition 0.000 claims description 38
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 35
- WTEOIRVLGSZEPR-UHFFFAOYSA-N boron trifluoride Chemical compound FB(F)F WTEOIRVLGSZEPR-UHFFFAOYSA-N 0.000 claims description 31
- -1 lanthanide halides Chemical class 0.000 claims description 29
- PMJHHCWVYXUKFD-SNAWJCMRSA-N (E)-1,3-pentadiene Chemical compound C\C=C\C=C PMJHHCWVYXUKFD-SNAWJCMRSA-N 0.000 claims description 27
- PMJHHCWVYXUKFD-UHFFFAOYSA-N piperylene Natural products CC=CC=C PMJHHCWVYXUKFD-UHFFFAOYSA-N 0.000 claims description 27
- 239000002002 slurry Substances 0.000 claims description 26
- DUNKXUFBGCUVQW-UHFFFAOYSA-J zirconium tetrachloride Chemical compound Cl[Zr](Cl)(Cl)Cl DUNKXUFBGCUVQW-UHFFFAOYSA-J 0.000 claims description 25
- 229910007932 ZrCl4 Inorganic materials 0.000 claims description 24
- 238000001542 size-exclusion chromatography Methods 0.000 claims description 23
- 229920000642 polymer Polymers 0.000 claims description 19
- BKOOMYPCSUNDGP-UHFFFAOYSA-N 2-methylbut-2-ene Chemical compound CC=C(C)C BKOOMYPCSUNDGP-UHFFFAOYSA-N 0.000 claims description 18
- 229910015900 BF3 Inorganic materials 0.000 claims description 18
- 239000004927 clay Substances 0.000 claims description 16
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 15
- XYLMUPLGERFSHI-UHFFFAOYSA-N alpha-Methylstyrene Chemical compound CC(=C)C1=CC=CC=C1 XYLMUPLGERFSHI-UHFFFAOYSA-N 0.000 claims description 15
- 229910052747 lanthanoid Inorganic materials 0.000 claims description 15
- 229910003865 HfCl4 Inorganic materials 0.000 claims description 14
- ZSWFCLXCOIISFI-UHFFFAOYSA-N cyclopentadiene Chemical compound C1C=CC=C1 ZSWFCLXCOIISFI-UHFFFAOYSA-N 0.000 claims description 14
- 239000010457 zeolite Substances 0.000 claims description 14
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 13
- YBYIRNPNPLQARY-UHFFFAOYSA-N 1H-indene Chemical compound C1=CC=C2CC=CC2=C1 YBYIRNPNPLQARY-UHFFFAOYSA-N 0.000 claims description 12
- 229910021627 Tin(IV) chloride Inorganic materials 0.000 claims description 12
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 12
- 229910021536 Zeolite Inorganic materials 0.000 claims description 11
- PDPJQWYGJJBYLF-UHFFFAOYSA-J hafnium tetrachloride Chemical compound Cl[Hf](Cl)(Cl)Cl PDPJQWYGJJBYLF-UHFFFAOYSA-J 0.000 claims description 11
- HJWLCRVIBGQPNF-UHFFFAOYSA-N prop-2-enylbenzene Chemical compound C=CCC1=CC=CC=C1 HJWLCRVIBGQPNF-UHFFFAOYSA-N 0.000 claims description 11
- 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 claims description 10
- JMMZCWZIJXAGKW-UHFFFAOYSA-N 2-methylpent-2-ene Chemical compound CCC=C(C)C JMMZCWZIJXAGKW-UHFFFAOYSA-N 0.000 claims description 10
- RRHGJUQNOFWUDK-UHFFFAOYSA-N Isoprene Chemical compound CC(=C)C=C RRHGJUQNOFWUDK-UHFFFAOYSA-N 0.000 claims description 10
- 229910003074 TiCl4 Inorganic materials 0.000 claims description 10
- JHXKRIRFYBPWGE-UHFFFAOYSA-K bismuth chloride Chemical compound Cl[Bi](Cl)Cl JHXKRIRFYBPWGE-UHFFFAOYSA-K 0.000 claims description 10
- 238000001354 calcination Methods 0.000 claims description 10
- LPIQUOYDBNQMRZ-UHFFFAOYSA-N cyclopentene Chemical compound C1CC=CC1 LPIQUOYDBNQMRZ-UHFFFAOYSA-N 0.000 claims description 10
- HPGGPRDJHPYFRM-UHFFFAOYSA-J tin(iv) chloride Chemical compound Cl[Sn](Cl)(Cl)Cl HPGGPRDJHPYFRM-UHFFFAOYSA-J 0.000 claims description 10
- XJDNKRIXUMDJCW-UHFFFAOYSA-J titanium tetrachloride Chemical compound Cl[Ti](Cl)(Cl)Cl XJDNKRIXUMDJCW-UHFFFAOYSA-J 0.000 claims description 10
- RGSFGYAAUTVSQA-UHFFFAOYSA-N pentamethylene Natural products C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 claims description 9
- HGCIXCUEYOPUTN-UHFFFAOYSA-N cyclohexene Chemical compound C1CCC=CC1 HGCIXCUEYOPUTN-UHFFFAOYSA-N 0.000 claims description 8
- QMMOXUPEWRXHJS-UHFFFAOYSA-N pentene-2 Natural products CCC=CC QMMOXUPEWRXHJS-UHFFFAOYSA-N 0.000 claims description 8
- WWUVJRULCWHUSA-UHFFFAOYSA-N 2-methyl-1-pentene Chemical compound CCCC(C)=C WWUVJRULCWHUSA-UHFFFAOYSA-N 0.000 claims description 6
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 claims description 6
- PQLAYKMGZDUDLQ-UHFFFAOYSA-K aluminium bromide Chemical compound Br[Al](Br)Br PQLAYKMGZDUDLQ-UHFFFAOYSA-K 0.000 claims description 6
- JLBJTVDPSNHSKJ-UHFFFAOYSA-N 4-Methylstyrene Chemical compound CC1=CC=C(C=C)C=C1 JLBJTVDPSNHSKJ-UHFFFAOYSA-N 0.000 claims description 5
- YWAKXRMUMFPDSH-UHFFFAOYSA-N pentene Chemical compound CCCC=C YWAKXRMUMFPDSH-UHFFFAOYSA-N 0.000 claims description 5
- QROGIFZRVHSFLM-QHHAFSJGSA-N [(e)-prop-1-enyl]benzene Chemical compound C\C=C\C1=CC=CC=C1 QROGIFZRVHSFLM-QHHAFSJGSA-N 0.000 claims description 4
- 229910052782 aluminium Inorganic materials 0.000 claims description 4
- 230000000379 polymerizing effect Effects 0.000 claims description 4
- PRBHEGAFLDMLAL-GQCTYLIASA-N (4e)-hexa-1,4-diene Chemical compound C\C=C\CC=C PRBHEGAFLDMLAL-GQCTYLIASA-N 0.000 claims description 3
- 239000012013 faujasite Substances 0.000 claims description 3
- 239000003456 ion exchange resin Substances 0.000 claims description 3
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 3
- 229910052680 mordenite Inorganic materials 0.000 claims description 3
- QYZLKGVUSQXAMU-UHFFFAOYSA-N penta-1,4-diene Chemical compound C=CCC=C QYZLKGVUSQXAMU-UHFFFAOYSA-N 0.000 claims description 3
- AHAREKHAZNPPMI-AATRIKPKSA-N (3e)-hexa-1,3-diene Chemical compound CC\C=C\C=C AHAREKHAZNPPMI-AATRIKPKSA-N 0.000 claims description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 2
- 229910015844 BCl3 Inorganic materials 0.000 claims 7
- FAQYAMRNWDIXMY-UHFFFAOYSA-N trichloroborane Chemical compound ClB(Cl)Cl FAQYAMRNWDIXMY-UHFFFAOYSA-N 0.000 claims 7
- 229920005989 resin Polymers 0.000 abstract description 117
- 239000011347 resin Substances 0.000 abstract description 117
- 238000006116 polymerization reaction Methods 0.000 abstract description 50
- 239000000047 product Substances 0.000 abstract description 23
- 239000007787 solid Substances 0.000 abstract description 22
- 239000002253 acid Substances 0.000 abstract description 16
- 238000005727 Friedel-Crafts reaction Methods 0.000 abstract description 10
- 239000002685 polymerization catalyst Substances 0.000 abstract description 5
- 238000011109 contamination Methods 0.000 abstract description 2
- 239000006227 byproduct Substances 0.000 abstract 1
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 108
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 76
- 239000000243 solution Substances 0.000 description 67
- 238000010926 purge Methods 0.000 description 61
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 51
- 229910052757 nitrogen Inorganic materials 0.000 description 38
- 239000003153 chemical reaction reagent Substances 0.000 description 30
- 230000035484 reaction time Effects 0.000 description 23
- 239000012141 concentrate Substances 0.000 description 22
- 239000000463 material Substances 0.000 description 19
- 239000003208 petroleum Substances 0.000 description 16
- 150000001336 alkenes Chemical class 0.000 description 15
- 238000011068 loading method Methods 0.000 description 15
- 239000002808 molecular sieve Substances 0.000 description 15
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 15
- 238000004821 distillation Methods 0.000 description 14
- 230000000694 effects Effects 0.000 description 14
- 239000000203 mixture Substances 0.000 description 14
- 238000001914 filtration Methods 0.000 description 13
- 239000007789 gas Substances 0.000 description 13
- 125000003118 aryl group Chemical group 0.000 description 12
- 238000010438 heat treatment Methods 0.000 description 12
- 238000010992 reflux Methods 0.000 description 12
- 230000009969 flowable effect Effects 0.000 description 11
- 239000000126 substance Substances 0.000 description 11
- 239000012298 atmosphere Substances 0.000 description 10
- 239000000843 powder Substances 0.000 description 10
- 238000010791 quenching Methods 0.000 description 10
- 150000003839 salts Chemical group 0.000 description 9
- 238000001816 cooling Methods 0.000 description 8
- 230000000171 quenching effect Effects 0.000 description 8
- 238000010538 cationic polymerization reaction Methods 0.000 description 7
- 239000003795 chemical substances by application Substances 0.000 description 7
- 239000000539 dimer Substances 0.000 description 7
- 150000003505 terpenes Chemical class 0.000 description 7
- 235000007586 terpenes Nutrition 0.000 description 7
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 6
- 239000003849 aromatic solvent Substances 0.000 description 6
- FKOASGGZYSYPBI-UHFFFAOYSA-K bis(trifluoromethylsulfonyloxy)alumanyl trifluoromethanesulfonate Chemical compound [Al+3].[O-]S(=O)(=O)C(F)(F)F.[O-]S(=O)(=O)C(F)(F)F.[O-]S(=O)(=O)C(F)(F)F FKOASGGZYSYPBI-UHFFFAOYSA-K 0.000 description 6
- 239000012986 chain transfer agent Substances 0.000 description 6
- 239000012065 filter cake Substances 0.000 description 6
- 239000011968 lewis acid catalyst Substances 0.000 description 6
- 241000894007 species Species 0.000 description 6
- 238000012546 transfer Methods 0.000 description 6
- 238000003828 vacuum filtration Methods 0.000 description 6
- NLZUEZXRPGMBCV-UHFFFAOYSA-N Butylhydroxytoluene Chemical compound CC1=CC(C(C)(C)C)=C(O)C(C(C)(C)C)=C1 NLZUEZXRPGMBCV-UHFFFAOYSA-N 0.000 description 5
- 238000009835 boiling Methods 0.000 description 5
- 235000010354 butylated hydroxytoluene Nutrition 0.000 description 5
- 150000001875 compounds Chemical class 0.000 description 5
- 238000003756 stirring Methods 0.000 description 5
- 239000008096 xylene Substances 0.000 description 5
- 239000004322 Butylated hydroxytoluene Substances 0.000 description 4
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 125000000217 alkyl group Chemical group 0.000 description 4
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 4
- GUJOJGAPFQRJSV-UHFFFAOYSA-N dialuminum;dioxosilane;oxygen(2-);hydrate Chemical compound O.[O-2].[O-2].[O-2].[Al+3].[Al+3].O=[Si]=O.O=[Si]=O.O=[Si]=O.O=[Si]=O GUJOJGAPFQRJSV-UHFFFAOYSA-N 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 239000003209 petroleum derivative Substances 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000011949 solid catalyst Substances 0.000 description 4
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 4
- 150000003738 xylenes Chemical class 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 229910017974 NH40H Inorganic materials 0.000 description 3
- 125000001931 aliphatic group Chemical group 0.000 description 3
- 125000005234 alkyl aluminium group Chemical group 0.000 description 3
- 229920006272 aromatic hydrocarbon resin Polymers 0.000 description 3
- 238000010923 batch production Methods 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 150000001993 dienes Chemical class 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 238000010828 elution Methods 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 229910001510 metal chloride Inorganic materials 0.000 description 3
- 229910052901 montmorillonite Inorganic materials 0.000 description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 3
- 239000003348 petrochemical agent Substances 0.000 description 3
- XMGQYMWWDOXHJM-JTQLQIEISA-N (+)-α-limonene Chemical compound CC(=C)[C@@H]1CCC(C)=CC1 XMGQYMWWDOXHJM-JTQLQIEISA-N 0.000 description 2
- MYRTYDVEIRVNKP-UHFFFAOYSA-N 1,2-Divinylbenzene Chemical compound C=CC1=CC=CC=C1C=C MYRTYDVEIRVNKP-UHFFFAOYSA-N 0.000 description 2
- FIPKSKMDTAQBDJ-UHFFFAOYSA-N 1-methyl-2,3-dihydro-1h-indene Chemical compound C1=CC=C2C(C)CCC2=C1 FIPKSKMDTAQBDJ-UHFFFAOYSA-N 0.000 description 2
- AFABGHUZZDYHJO-UHFFFAOYSA-N 2-Methylpentane Chemical compound CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 2
- MHNNAWXXUZQSNM-UHFFFAOYSA-N 2-methylbut-1-ene Chemical compound CCC(C)=C MHNNAWXXUZQSNM-UHFFFAOYSA-N 0.000 description 2
- 229910052684 Cerium Inorganic materials 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 239000004793 Polystyrene Substances 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 239000000853 adhesive Substances 0.000 description 2
- 230000001070 adhesive effect Effects 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 229960000892 attapulgite Drugs 0.000 description 2
- 229910000278 bentonite Inorganic materials 0.000 description 2
- 239000000440 bentonite Substances 0.000 description 2
- SVPXDRXYRYOSEX-UHFFFAOYSA-N bentoquatam Chemical compound O.O=[Si]=O.O=[Al]O[Al]=O SVPXDRXYRYOSEX-UHFFFAOYSA-N 0.000 description 2
- VNSBYDPZHCQWNB-UHFFFAOYSA-N calcium;aluminum;dioxido(oxo)silane;sodium;hydrate Chemical compound O.[Na].[Al].[Ca+2].[O-][Si]([O-])=O VNSBYDPZHCQWNB-UHFFFAOYSA-N 0.000 description 2
- 238000011088 calibration curve Methods 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 description 2
- 239000002734 clay mineral Substances 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- GDVKFRBCXAPAQJ-UHFFFAOYSA-A dialuminum;hexamagnesium;carbonate;hexadecahydroxide Chemical compound [OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Al+3].[Al+3].[O-]C([O-])=O GDVKFRBCXAPAQJ-UHFFFAOYSA-A 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000009408 flooring Methods 0.000 description 2
- 150000004820 halides Chemical group 0.000 description 2
- 229910000271 hectorite Inorganic materials 0.000 description 2
- KWLMIXQRALPRBC-UHFFFAOYSA-L hectorite Chemical compound [Li+].[OH-].[OH-].[Na+].[Mg+2].O1[Si]2([O-])O[Si]1([O-])O[Si]([O-])(O1)O[Si]1([O-])O2 KWLMIXQRALPRBC-UHFFFAOYSA-L 0.000 description 2
- DMEGYFMYUHOHGS-UHFFFAOYSA-N heptamethylene Natural products C1CCCCCC1 DMEGYFMYUHOHGS-UHFFFAOYSA-N 0.000 description 2
- 229910001701 hydrotalcite Inorganic materials 0.000 description 2
- 229960001545 hydrotalcite Drugs 0.000 description 2
- PQNFLJBBNBOBRQ-UHFFFAOYSA-N indane Chemical compound C1=CC=C2CCCC2=C1 PQNFLJBBNBOBRQ-UHFFFAOYSA-N 0.000 description 2
- 239000000976 ink Substances 0.000 description 2
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 2
- 229910052622 kaolinite Inorganic materials 0.000 description 2
- XMGQYMWWDOXHJM-UHFFFAOYSA-N limonene Chemical compound CC(=C)C1CCC(C)=CC1 XMGQYMWWDOXHJM-UHFFFAOYSA-N 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 239000003607 modifier Substances 0.000 description 2
- 230000007935 neutral effect Effects 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 2
- 229910052625 palygorskite Inorganic materials 0.000 description 2
- 229920002223 polystyrene Polymers 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- GRWFGVWFFZKLTI-UHFFFAOYSA-N rac-alpha-Pinene Natural products CC1=CCC2C(C)(C)C1C2 GRWFGVWFFZKLTI-UHFFFAOYSA-N 0.000 description 2
- 238000000611 regression analysis Methods 0.000 description 2
- 229910000275 saponite Inorganic materials 0.000 description 2
- 229930195734 saturated hydrocarbon Natural products 0.000 description 2
- 229910052814 silicon oxide Inorganic materials 0.000 description 2
- 238000007655 standard test method Methods 0.000 description 2
- 150000003440 styrenes Chemical class 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- JZHBGUMBONMHQS-UHFFFAOYSA-F tetrachlorotitanium;zirconium(4+);tetrachloride Chemical compound [Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Ti+4].[Zr+4] JZHBGUMBONMHQS-UHFFFAOYSA-F 0.000 description 2
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 2
- 239000003643 water by type Substances 0.000 description 2
- WTARULDDTDQWMU-RKDXNWHRSA-N (+)-β-pinene Chemical compound C1[C@H]2C(C)(C)[C@@H]1CCC2=C WTARULDDTDQWMU-RKDXNWHRSA-N 0.000 description 1
- WTARULDDTDQWMU-IUCAKERBSA-N (-)-Nopinene Natural products C1[C@@H]2C(C)(C)[C@H]1CCC2=C WTARULDDTDQWMU-IUCAKERBSA-N 0.000 description 1
- HYFLWBNQFMXCPA-UHFFFAOYSA-N 1-ethyl-2-methylbenzene Chemical compound CCC1=CC=CC=C1C HYFLWBNQFMXCPA-UHFFFAOYSA-N 0.000 description 1
- GRWFGVWFFZKLTI-IUCAKERBSA-N 1S,5S-(-)-alpha-Pinene Natural products CC1=CC[C@@H]2C(C)(C)[C@H]1C2 GRWFGVWFFZKLTI-IUCAKERBSA-N 0.000 description 1
- DXIJHCSGLOHNES-UHFFFAOYSA-N 3,3-dimethylbut-1-enylbenzene Chemical compound CC(C)(C)C=CC1=CC=CC=C1 DXIJHCSGLOHNES-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 229910004664 Cerium(III) chloride Inorganic materials 0.000 description 1
- ZQISRDCJNBUVMM-YFKPBYRVSA-N L-histidinol Chemical compound OC[C@@H](N)CC1=CNC=N1 ZQISRDCJNBUVMM-YFKPBYRVSA-N 0.000 description 1
- NIPNSKYNPDTRPC-UHFFFAOYSA-N N-[2-oxo-2-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)ethyl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(CNC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 NIPNSKYNPDTRPC-UHFFFAOYSA-N 0.000 description 1
- 229910017544 NdCl3 Inorganic materials 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 229910019328 PrCl3 Inorganic materials 0.000 description 1
- WTARULDDTDQWMU-UHFFFAOYSA-N Pseudopinene Natural products C1C2C(C)(C)C1CCC2=C WTARULDDTDQWMU-UHFFFAOYSA-N 0.000 description 1
- 241000779819 Syncarpia glomulifera Species 0.000 description 1
- 239000004809 Teflon Substances 0.000 description 1
- 229920006362 Teflon® Polymers 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- 239000003377 acid catalyst Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- XCPQUQHBVVXMRQ-UHFFFAOYSA-N alpha-Fenchene Natural products C1CC2C(=C)CC1C2(C)C XCPQUQHBVVXMRQ-UHFFFAOYSA-N 0.000 description 1
- MVNCAPSFBDBCGF-UHFFFAOYSA-N alpha-pinene Natural products CC1=CCC23C1CC2C3(C)C MVNCAPSFBDBCGF-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229930006722 beta-pinene Natural products 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229940095259 butylated hydroxytoluene Drugs 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- VYLVYHXQOHJDJL-UHFFFAOYSA-K cerium trichloride Chemical compound Cl[Ce](Cl)Cl VYLVYHXQOHJDJL-UHFFFAOYSA-K 0.000 description 1
- PHSMPGGNMIPKTH-UHFFFAOYSA-K cerium(3+);trifluoromethanesulfonate Chemical compound [Ce+3].[O-]S(=O)(=O)C(F)(F)F.[O-]S(=O)(=O)C(F)(F)F.[O-]S(=O)(=O)C(F)(F)F PHSMPGGNMIPKTH-UHFFFAOYSA-K 0.000 description 1
- 239000003086 colorant Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 150000001925 cycloalkenes Chemical class 0.000 description 1
- 238000005108 dry cleaning Methods 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- LCWMKIHBLJLORW-UHFFFAOYSA-N gamma-carene Natural products C1CC(=C)CC2C(C)(C)C21 LCWMKIHBLJLORW-UHFFFAOYSA-N 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 239000000383 hazardous chemical Substances 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
- 238000007757 hot melt coating Methods 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- FBAFATDZDUQKNH-UHFFFAOYSA-M iron chloride Chemical compound [Cl-].[Fe] FBAFATDZDUQKNH-UHFFFAOYSA-M 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- AEDROEGYZIARPU-UHFFFAOYSA-K lutetium(iii) chloride Chemical compound Cl[Lu](Cl)Cl AEDROEGYZIARPU-UHFFFAOYSA-K 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- NFWSQSCIDYBUOU-UHFFFAOYSA-N methylcyclopentadiene Chemical compound CC1=CC=CC1 NFWSQSCIDYBUOU-UHFFFAOYSA-N 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229930014626 natural product Natural products 0.000 description 1
- ATINCSYRHURBSP-UHFFFAOYSA-K neodymium(iii) chloride Chemical compound Cl[Nd](Cl)Cl ATINCSYRHURBSP-UHFFFAOYSA-K 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 238000006384 oligomerization reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 239000001739 pinus spp. Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 1
- 239000004810 polytetrafluoroethylene Substances 0.000 description 1
- LHBNLZDGIPPZLL-UHFFFAOYSA-K praseodymium(iii) chloride Chemical compound Cl[Pr](Cl)Cl LHBNLZDGIPPZLL-UHFFFAOYSA-K 0.000 description 1
- 239000011253 protective coating Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000002390 rotary evaporation Methods 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- BHXBZLPMVFUQBQ-UHFFFAOYSA-K samarium(iii) chloride Chemical compound Cl[Sm](Cl)Cl BHXBZLPMVFUQBQ-UHFFFAOYSA-K 0.000 description 1
- 239000000565 sealant Substances 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- PJANXHGTPQOBST-UHFFFAOYSA-N stilbene Chemical compound C=1C=CC=CC=1C=CC1=CC=CC=C1 PJANXHGTPQOBST-UHFFFAOYSA-N 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 229910002029 synthetic silica gel Inorganic materials 0.000 description 1
- GFISHBQNVWAVFU-UHFFFAOYSA-K terbium(iii) chloride Chemical compound Cl[Tb](Cl)Cl GFISHBQNVWAVFU-UHFFFAOYSA-K 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- BFKJFAAPBSQJPD-UHFFFAOYSA-N tetrafluoroethene Chemical compound FC(F)=C(F)F BFKJFAAPBSQJPD-UHFFFAOYSA-N 0.000 description 1
- 238000007669 thermal treatment Methods 0.000 description 1
- 229920001169 thermoplastic Polymers 0.000 description 1
- 239000012815 thermoplastic material Substances 0.000 description 1
- 229940036248 turpentine Drugs 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
- 239000004711 α-olefin Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F4/00—Polymerisation catalysts
- C08F4/06—Metallic compounds other than hydrides and other than metallo-organic compounds; Boron halide or aluminium halide complexes with organic compounds containing oxygen
- C08F4/12—Metallic compounds other than hydrides and other than metallo-organic compounds; Boron halide or aluminium halide complexes with organic compounds containing oxygen of boron, aluminium, gallium, indium, thallium or rare earths
- C08F4/14—Boron halides or aluminium halides; Complexes thereof with organic compounds containing oxygen
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F240/00—Copolymers of hydrocarbons and mineral oils, e.g. petroleum resins
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F12/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring
- C08F12/02—Monomers containing only one unsaturated aliphatic radical
- C08F12/04—Monomers containing only one unsaturated aliphatic radical containing one ring
Landscapes
- Chemical & Material Sciences (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Polymerization Catalysts (AREA)
- Catalysts (AREA)
Abstract
Supported metal halides and metal halide solid acids are used as catalysts for the polymerization of a feed stream containing at least one of pure monomer, C5 monomers, and C9 monomers to produce hydrocarbon resins. Freely-associated water may be removed from the solid acid catalyst prior to use. Resins with softening points (Ring and Ball) in the range of about 5 ~C to 170 ~C can be prepared. These catalysts offer advantages over the traditional Friedel-Crafts polymerization catalysts since the acid sites are an integral part of the solid. The solid acid catalysts are relatively nonhazardous, reusable catalysts which eliminate or at least reduce contamination of the resulting resin products with acid residues or by-products.
Description
METAL HALIDE SOLID ACIDS AND SUPPORTED METAL HALIDES AS
CATALYSTS FOR THE PREPARATION OF HYDROCARBON RESINS
CROSS-REFERENCE OF RELATED APPLICATIONS
The present application claims the priority under 35 U.S.C. ~ 119(e) of U.S.
Provisional Application No. 60/035,217, filed January 8, 1997; U.S.
Provisional Application No. 60/034,579, filed on January 9, 1997; and U.S. Provisional Application No.
60/035,797, filed on January 10, 1997; the disclosures of which are herein expressly incorporated by reference in their entirety.
BACKGROUND OF THE INVENTION
1.Field of the Invention This invention relates to supported metal halides and metal halide solid acids useful as catalysts for the polymerization of a feed stream containing at least one of pure monomer.
I S CS monomers, and C9 monomers to produce a hydrocarbon resin, to processes of preparing hydrocarbon resins using at least one of supported metal halides and metal halide solid acid catalysts, and to hydrocarbon resins produced by such processes.
''. Discussion of Back rg ound Hydrocarbon resins are low molecular weight, thermoplastic materials prepared via thermal or catalytic polymerization. The resins may be derived from several different sources of monomers. The monomer sources include cracked petroleum distillate from oil refining, turpentine fractions (c.g.) terpenes from natural product distillation), paper mill bv-product streams, coal tar, and a variety of pure olefinic monomers.
The resulting hydrocarbon resins can range from viscous liquids to hard, brittle solids with colors ranging from water white to pale yellow, amber, or dark brown depending on the monomers used and the specific reaction conditions. Typically, pure monomer resins tend to be water white, C9 monomer resins tend to be brown, and CS monomer resins tend to be yellow.
Hydrocarbon resins are used extensively as modifiers in adhesives, rubber, hot-melt coatings, printing inks, paint, flooring, and other applications. The resins are usually used to modify other materials.
Pure monomer hydrocarbon resins can be prepared by cationic polymerization of _2_ styrene-based monomers such as styrene, alpha-methyl styrene, vinyl toluene, and other alkyl substituted styrenes using Friedel-Crafts polymerization catalysts such as unsupported Lewis acids (e.g., boron trifluoride (BF3), complexes of boron trifluoride, aluminum trichloride (A1C13), alkyl aluminum chlorides).
Similarly, aliphatic CS hydrocarbon resins can be prepared by cationic polymerization of a cracked petroleum feed containing CS and C6 paraffins, olefins, and diolefins also referred to as "CS monomers". These monomer streams are comprised of canonically polymerizable monomers such as 1,3-pentadiene which is the primary reactive component along with cyclopentene, pentenc, 2-methyl-2-butene, 2-methyl-2-pentene, cyclopentadiene, and dicyclopentadiene. The polymcrizations are catalyzed using Friedel-Crafts polymerization catalysts such as unsupported Lewis acids (e.g., boron trifluoride (BF3), complexes of boron trifluoride, aluminum trichloride (AIC13), or alkyl aluminum chlorides). 1n addition to the reactive components, nonpolymerizable components in the feed include saturated hydrocarbons which can be codistilled with the unsaturated components such as pentane, cyclopentane, or 2-methylpentane. This monomer feed can be copolymerized with C4 or CS olefins or dimers as chain transfer agents.
Also, aromatic C9 hydrocarbon resins can be prepared by cationic polymerization of aromatic C8, C9, and/or C10 unsaturated monomers derived from petroleum distillates resulting from naphtha cracking and are referred to as "C9 monomers". These monomer streams arc comprised of canonically polymerizable monomers such as styrene, alpha-methyl styrene, beta-methyl styrene, vinyl toluene, indene, dicyclopentadiene, divinylbenzene, and other alkyl substituted derivatives of these components.
The polymcrizations are catalyzed using Friedel-Crafts polymerization catalysts such as unsupported Lewis acids (e.g., boron trifluoride (BF3), complexes of boron trifluoride, aluminum trichloride (A1C13), alkyl aluminum chlorides). In addition to the reactive components, nonpolymerizable components include aromatic hydrocarbons such as xylene, ethyl benzene, cumene, ethyl toluene, indane, methylindane, naphthalene and other similar species. These nonpolymerizable components of the feed stream can be incorporated into the resins via alkylation reactions.
Although unsupported Lewis acids are effective catalysts for the cationic polymerization reactions to produce hydrocarbon resins, they have several disadvantages.
Conventional unsupported Lewis acids are single use catalysts which require processing steps to quench the reactions and neutralize the acids.
Further, conventional unsupported Lewis acids also require removal of catalyst salt residues from the resulting resin products. Once the salt residues generated from the catalyst neutralization are removed, the disposal of these residues presents an additional cost.
Therefore, it is of particular interest to reduce the amount of catalyst residues, particularly halogen-containing species generated in these reactions.
Another problem involved in using conventional unsupported Lewis acid catalysts, such as A1C13 and BF3, is that they are hazardous materials. These conventional Lewis acid catalysts generate highly corrosive acid gases on exposure to moisture, (e.g., HF, HC1).
In addition to the traditional Lewis acids, work has been done with certain solid acid catalysts. BITTLES et al., "Clay-Catalyzed Reactions of Olefins. I.
Polymerization of Styrene", Iournal of Polymer Science: Part A, Vol. 2, pp. 1221-31 (1964) and BITTLES et al., "Clay-Catalyzed Reactions of Olefins. II. Catalyst Acidity and Measurement", .lournal of Polymer Science: Part A, Vol. 2, pp. 1847-62 (1964), the disclosures of which are herein incorporated by reference in their entireties, together disclose polymerization of styrene with acid clay catalysts to obtain polymers having molecular weights between 440 and 2000 as determined by freezing point depression of benzene solutions. These documents disclose that the catalyst was prepared for polymerization by heating under vacuum) and that i f the catalyst adsorbed moisture, the activity of the catalyst could be restored by rcheating under vacuum.
SALT, "The Use of Activated Clays as Catalysts in Polymerisation Processes, with Particular Reference to Polymers of Alpha Methyl Styrene", ClakMinerals Bulletin, Vol.
CATALYSTS FOR THE PREPARATION OF HYDROCARBON RESINS
CROSS-REFERENCE OF RELATED APPLICATIONS
The present application claims the priority under 35 U.S.C. ~ 119(e) of U.S.
Provisional Application No. 60/035,217, filed January 8, 1997; U.S.
Provisional Application No. 60/034,579, filed on January 9, 1997; and U.S. Provisional Application No.
60/035,797, filed on January 10, 1997; the disclosures of which are herein expressly incorporated by reference in their entirety.
BACKGROUND OF THE INVENTION
1.Field of the Invention This invention relates to supported metal halides and metal halide solid acids useful as catalysts for the polymerization of a feed stream containing at least one of pure monomer.
I S CS monomers, and C9 monomers to produce a hydrocarbon resin, to processes of preparing hydrocarbon resins using at least one of supported metal halides and metal halide solid acid catalysts, and to hydrocarbon resins produced by such processes.
''. Discussion of Back rg ound Hydrocarbon resins are low molecular weight, thermoplastic materials prepared via thermal or catalytic polymerization. The resins may be derived from several different sources of monomers. The monomer sources include cracked petroleum distillate from oil refining, turpentine fractions (c.g.) terpenes from natural product distillation), paper mill bv-product streams, coal tar, and a variety of pure olefinic monomers.
The resulting hydrocarbon resins can range from viscous liquids to hard, brittle solids with colors ranging from water white to pale yellow, amber, or dark brown depending on the monomers used and the specific reaction conditions. Typically, pure monomer resins tend to be water white, C9 monomer resins tend to be brown, and CS monomer resins tend to be yellow.
Hydrocarbon resins are used extensively as modifiers in adhesives, rubber, hot-melt coatings, printing inks, paint, flooring, and other applications. The resins are usually used to modify other materials.
Pure monomer hydrocarbon resins can be prepared by cationic polymerization of _2_ styrene-based monomers such as styrene, alpha-methyl styrene, vinyl toluene, and other alkyl substituted styrenes using Friedel-Crafts polymerization catalysts such as unsupported Lewis acids (e.g., boron trifluoride (BF3), complexes of boron trifluoride, aluminum trichloride (A1C13), alkyl aluminum chlorides).
Similarly, aliphatic CS hydrocarbon resins can be prepared by cationic polymerization of a cracked petroleum feed containing CS and C6 paraffins, olefins, and diolefins also referred to as "CS monomers". These monomer streams are comprised of canonically polymerizable monomers such as 1,3-pentadiene which is the primary reactive component along with cyclopentene, pentenc, 2-methyl-2-butene, 2-methyl-2-pentene, cyclopentadiene, and dicyclopentadiene. The polymcrizations are catalyzed using Friedel-Crafts polymerization catalysts such as unsupported Lewis acids (e.g., boron trifluoride (BF3), complexes of boron trifluoride, aluminum trichloride (AIC13), or alkyl aluminum chlorides). 1n addition to the reactive components, nonpolymerizable components in the feed include saturated hydrocarbons which can be codistilled with the unsaturated components such as pentane, cyclopentane, or 2-methylpentane. This monomer feed can be copolymerized with C4 or CS olefins or dimers as chain transfer agents.
Also, aromatic C9 hydrocarbon resins can be prepared by cationic polymerization of aromatic C8, C9, and/or C10 unsaturated monomers derived from petroleum distillates resulting from naphtha cracking and are referred to as "C9 monomers". These monomer streams arc comprised of canonically polymerizable monomers such as styrene, alpha-methyl styrene, beta-methyl styrene, vinyl toluene, indene, dicyclopentadiene, divinylbenzene, and other alkyl substituted derivatives of these components.
The polymcrizations are catalyzed using Friedel-Crafts polymerization catalysts such as unsupported Lewis acids (e.g., boron trifluoride (BF3), complexes of boron trifluoride, aluminum trichloride (A1C13), alkyl aluminum chlorides). In addition to the reactive components, nonpolymerizable components include aromatic hydrocarbons such as xylene, ethyl benzene, cumene, ethyl toluene, indane, methylindane, naphthalene and other similar species. These nonpolymerizable components of the feed stream can be incorporated into the resins via alkylation reactions.
Although unsupported Lewis acids are effective catalysts for the cationic polymerization reactions to produce hydrocarbon resins, they have several disadvantages.
Conventional unsupported Lewis acids are single use catalysts which require processing steps to quench the reactions and neutralize the acids.
Further, conventional unsupported Lewis acids also require removal of catalyst salt residues from the resulting resin products. Once the salt residues generated from the catalyst neutralization are removed, the disposal of these residues presents an additional cost.
Therefore, it is of particular interest to reduce the amount of catalyst residues, particularly halogen-containing species generated in these reactions.
Another problem involved in using conventional unsupported Lewis acid catalysts, such as A1C13 and BF3, is that they are hazardous materials. These conventional Lewis acid catalysts generate highly corrosive acid gases on exposure to moisture, (e.g., HF, HC1).
In addition to the traditional Lewis acids, work has been done with certain solid acid catalysts. BITTLES et al., "Clay-Catalyzed Reactions of Olefins. I.
Polymerization of Styrene", Iournal of Polymer Science: Part A, Vol. 2, pp. 1221-31 (1964) and BITTLES et al., "Clay-Catalyzed Reactions of Olefins. II. Catalyst Acidity and Measurement", .lournal of Polymer Science: Part A, Vol. 2, pp. 1847-62 (1964), the disclosures of which are herein incorporated by reference in their entireties, together disclose polymerization of styrene with acid clay catalysts to obtain polymers having molecular weights between 440 and 2000 as determined by freezing point depression of benzene solutions. These documents disclose that the catalyst was prepared for polymerization by heating under vacuum) and that i f the catalyst adsorbed moisture, the activity of the catalyst could be restored by rcheating under vacuum.
SALT, "The Use of Activated Clays as Catalysts in Polymerisation Processes, with Particular Reference to Polymers of Alpha Methyl Styrene", ClakMinerals Bulletin, Vol.
2, pp. 55-58 ( 1948), the disclosure of which is herein incorporated by reference in its entirety, discloses polymerization of styrene and/or alpha-methyl styrene by using a clay catalyst to obtain polymers that range from dimers to molecular weights of about 3000.
U.S. Patent No. 5,561,095 to CHEN et al., the disclosure of which is herein incorporated by reference in its entirety, discloses a supported Lewis acid catalyst for polymerization of olefins, including C3-C23 alpha-olefins, to obtain polymers having number average molecular weights (Mn) ranging from about 300 to 300,000.
Exemplary Lewis acid supports include silica, silica-alumina, zeolites, and clays.
Example 1 of CHEN
et al. discloses that a Lewis acid supported on silica is heated under vacuum.
U.S. Patent No. 3,799,913 to WHEELER et al., the disclosure of which is herein incorporated by reference in its entirety, discloses Friedel-Crafts catalysts for polymerization of polymerizable constituents, including alpha-methyl styrene, indene, vinyl toluene and styrene, to obtain polymers having a number average molecular weight (Mn) ranging from about 350 to 1200. Zinc chloride is disclosed as one of the Friedel-Crafts catalysts.
U.S. Patent No. 3,652,707 to SAINES, the disclosure of which is herein incorporated by reference in its entirety, discloses Friedel-Crafts metal halide catalysts for polymerization of olefin hydrocarbons, including pentene, styrene and methylstyrene, to obtain polymers having a molecular weight of from about 700 to about 2500. Zinc chloride is disclosed as one of the Friedel-Crafts metal halide catalysts.
PENG et al., "Electrophilic Polymerization of 1,3-Pentadiene Initiated by Aluminum Triflate", Eur. Pol~nn. (T, Vol. 30, No. 1, pp. 69-77 ( 1994), the disclosure of which is herein incorporated by reference in its entirety, discloses aluminum triflate for polymerization of piperylene to obtain polymers having varying number average molecular weights.
European Patent Application 0 352 856 A 1, the disclosure of which is herein incorporated by reference in its entirety, discloses use of aluminum triflate, cerium triflate, e.g., for oligomerization of C3 to C6 olefins to obtain oligomers having 6 to 24 carbon atoms.
GANDINI et al., "The Heterogeneous Cationic Polymerization of Aromatic Monomers by Aluminum Triflate", Polymer Pr~rints, American Chemical Society) pp. 359-360 ( 1996), the disclosure of which is herein incorporated by reference in its entirety, discloses use of aluminum triflate for polymerization of C9 related monomers to obtain a polymer having a number average molecular weight (Mn) around 3000. This document also discloses that aluminum triflate could be useful for the direct "resinification" of mixtures of aromatic monomers and solvents arising from specific petroleum cuts.
Other documents, the disclosures of which are herein incorporated by reference in their entireties, which generally disclose the use of solid acid catalysts to polymerize monomers for the preparation of resins include U.S. Patent No. 4,068,062 to LEPERT, U.S.
Patent No. 4,130,701 to LEPERT, U.S. Patent No. 4,245,075 to LEPERT, and U.S.
Patent No. 4,824,921 to LUVINH.
_5_ SUMMARY OF THE INVENTION
The present invention involves the preparation of hydrocarbon resins. More particularly, the present invention involves the use of at least one of supported metal halides and metal halide solid acid catalysts to polymerize a feed of hydrocarbon monomers.
Hydrocarbon resins are prepared from at least one of pure monomer, CS
monomers, and C9 monomers using relatively environmentally benign, recyclable, at least one of supported metal halides and metal halide solid acid catalysts in which freely-associated water may have been removed. In the present invention, hydrocarbon resins are prepared by a cationic polymerization (e.g., Friedel-Crafts) wherein a feed stream containing at least one of pure monomer, CS monomers, and C9 monomers is preferably treated with at least one of supported metal halides and metal halide solid acid catalyst.
Before use, the solid acid catalysts and/or supports may be treated to remove freely-associated water associated with the solids to maximize catalyst acidity and activity toward the polymerization. For example, prior to use, the catalyst and/or support may be calcined for a sufficient time to remove freely-associated water and/or the catalyst and/or support can be exposed to reduced atmospheric pressure. For instance, the calcining may be at a temperature up to about 700°C, preferably at a temperature between about 50°C and 500°C.
The calcining may be under reduced atmospheric pressure for up to about 8 hours, preferably between about 1 hour to 4 hours.
2p In accordance with one aspect, the present invention is directed to a process for making a hydrocarbon resin, including polymerizing a feed stream comprising at least one member selected from the group consisting of pure monomer, CS monomers, and C9 monomers in the presence of a supported metal halide solid acid catalyst to produce a hydrocarbon resin, wherein substantially all freely-associated water has been removed from the supported metal halide solid acid catalyst.
In accordance with another aspect, the present invention is directed to a process for making a hydrocarbon resin, including polymerizing a feed stream comprising at least one member selected from the group consisting of pure monomer, CS monomers, and C9 monomers in the presence of ZrCl4 to produce a hydrocarbon resin.
The supported metal halide solid acid catalyst may comprise Lewis acid on clay, silica, silica-alumina, mesoporous silica, mesoporous silica-alumina, ion exchange resin, zeolite. The Lewis acid may include at least one member selected from the group consisting _6_ of ZnClz, A1C1~, AlBr3, BFj, BC13, FeCl3, SnCl4, TiCl4, ZrCl4, HfCl4, BiCl3, and lanthanide halides.
The clay supports may include naturally occurring clay mineral such as at least one member selected from the group consisting of kaolinite, bentonite, attapulgite, montmorillonite, clarit, Fuller's earth, hectorite, and beidellite; synthetic clay such as at least one member selected from the group consisting of saponite and hydrotalcite;
montmorillonite clay treated with at least one member selected from the group consisting of sulfuric acid and hydrochloric acid; and modified clay including at least one member selected from the group consisting of aluminum oxide pillared clay, cerium modified alumina pillared clay, and metal oxide pillared clay.
The zeolite support may include at least one member selected from the group consisting of zeolite Y, zeolite Vii, MFI, MEL, NaX, NaY, faujasite, and mordenite.
In another feature of the present invention, the supported metal halide solid acid catalyst includes polymer grafted aluminum halide.
1n accordance with another feature of the invention, the feed stream includes between about 20 wt'% and 80 wt% monomers and about 80 wt% to 20 wt% of solvent.
Preferably, the feed stream includes about 30 wt% to 70 wt% monomers and about 70 wt'ro to 30 wrt%
of solvent. More preferably, the feed stream includes about SO wt% to 70 wt°,~o monomers and about 50 wt'% to 30 wt% of solvent. The solvent may include an aromatic solvent. The aromatic solvent may include at least one member selected from the group consisting of toluene, xylenes, and aromatic petroleum solvents. The solvent may include an aliphatic solvent. The invention may further include recycling the solvent.
In accordance with a feature of the invention, the feed stream includes at least CS
monomers. The feed stream may include at least CS monomers, wherein cyclopentadiene and methylcyclopentadienc components are removed from the feed stream by heating at a temperature between about 100°C and 160°C and fractionating by distillation. The CS
monomers may include at least one member selected from the group consisting of isobutylene, 2-methyl-2-butene, 1-pentene, 2-methyl-1-pentene, 2-methyl-2-pentene, 2-pentene, cyclopentene, cyclohexene, 1,3-pentadiene, 1,4-pentadiene, isoprene, 1,3-hexadiene, 1,4-hexadiene, cyclopentadiene, and dicyclopentadiene. The feed stream may include at least CS monomers, wherein the feed stream includes at least about 70 wt% of polymerizable monomers with at least about 50 wt% 1,3-pentadiene. The feed stream may contain low levels of isoprene, generally contains a portion of 2-methyl-2-butene, and may contain one or more cyclodiolefins.
The feed stream may include at least CS monomers, wherein the feed stream further includes up to about 40 wt% of chain transfer agent, preferably up to about 20 wt% of chain transfer agent. The chain transfer agent may include at least one member selected fi~om the group consisting of C4 olefins, CS olefins, dimers of C4 olefins, and dimers of CS olefins.
The chain transfer agent may include at least one member selected from the group consisting of isobutylene, 2-methyl-1-butene, 2-methyl-2-butene, dimers thereof, and oligomers thereo f.
In accordance with a feature of the invention, the feed stream includes about 30 wt%
to 95 wt% of CS monomers and about 70 wt% to S wt% of a cofeed including at (cast one member selected from the group consisting of pure monomer, C9 monomers, and terpenes.
Preferably, the feed stream includes about 50 wt% to 85 wt% of CS monomers and about 50 wt% to 15 wt% of a cofeed including at least one member selected from the group consisting of pure monomer, C9 monomers, and tcrpencs.
In accordance with another feature of the invention, the feed stream includes at least C9 monomers. The C9 monomers may include at least one member selected from the group consisting of styrene, vinyl toluene, indene, dicyclopentadiene, and alkylated derivatives thereof. The C9 monomers may include at least about 20 wt% polymerizable unsaturated hydrocarbons. The C9 monomers may include about 30 wt°a to 75 wt'%
polymerizable unsawrated hydrocarbons. The C9 monomers may include about 35 wt°r~ to 7O wt'~a polymerizable unsaturated hydrocarbons.
In accordance with a feature of the invention, the feed stream includes about 3U wt'%
to 95 wt% of the C9 monomers and about 70 wt% to 5 wt% of a cofeed including at least one member selected from the group consisting of pure monomer, CS monomers, and terpenes. Preferably, the feed stream includes about 50 wt% to 85 wt°/<. of the C9 monomers and about 50 wt% to 15 wt% of a cofeed including at least one member selected from the group consisting of pure monomer, CS monomers, and terpenes.
Many of the supported metal halides and metal halide solid acid catalysts function -g_ most effectively in the presence of a controlled amount of water in the monomer feed stream. In accordance with this feature of the invention, the feed stream should include less than about 500 ppm water, preferably less than about 200 ppm water, more preferably less than about 100 ppm water, and most preferably less than about 50 ppm water.
S In accordance with yet another feature of the invention, the feed stream is contacted with about 0.5 wt% to 30 wt%, preferably about 1 wt% to 20 wt%, more preferably about 3 wt% to 15 wt%, and most preferably 0.5 wt% to 5 wt% of the catalyst based on monomer weight in a batch reactor.
In accordance with yet another feature of the invention, the catalyst is added to the feed stream.
In accordance with another feature of the invention, the feed stream is added to a slurry of the catalyst in solvent. The feed stream may be passed over a fixed bed of the catalyst.
In accordance with yet another feature of the invention, the feed stream is cofed with 1 S a slurry of the catalyst into a reactor.
In accordance with a feature of the invention, the polymerization is carried out as a continuous process or as a batch process. A reaction time in the batch process is about 30 minutes to 8 hours, preferably about 1 hour to 4 hours at reaction temperature.
In accordance with a feature of the invention, the feed stream is polymerized at a reaction temperature between about -50°C and 1 SO°C, preferably between about -20°C and 100°C, and more preferably between about 0°C and 70°C.
In accordance with another feature of the invention, the polymerization is stopped by removing the catalyst from the hydrocarbon resin. The catalyst may be removed from the hydrocarbon resin by filtration. The hydrocarbon resin may be removed from a fixed bed reactor which includes the catalyst.
In accordance with a feature of the invention, the hydrocarbon resin is stripped to remove unreacted monomers, solvents, and low molecular weight oligomers. The unreacted monomers, solvents, and low molecular weight oligomers may be recycled.
In accordance with a feature of the invention, the hydrocarbon resin is separated from a hydrocarbon resin solution.
In accordance with a feature of the invention, the hydrocarbon resin has a softening point as measured by ASTM-E28 "Standard Test Method for Softening Point by Ring and Ball Apparatus", between about 5°C and 170°C. The feed stream may include at least CS
monomers, wherein the softening point of the resulting hydrocarbon resin is between about 50°C and 150°C. The feed stream may include at least C9 monomers, wherein the softening point of the resulting hydrocarbon resin is between about 70°C and 160°C.
In accordance with a feature of the invention, the feed stream includes at least pure monomer, wherein the resulting hydrocarbon resin has a number average molecular weight (Mn) ranging from about 400 to 2000, a weight average molecular weight (Mw) ranging from about S00 to 5000, a Z average molecular weight (Mz) ranging from about 500 to 10,000, and a polydispersity (PD) as measured by Mw/Mn between about 1.2 and 3.5, where Mn, Mw, and Mz are determined by size exclusion chromatography (SEC).
In accordance with a feature of the invention, the feed stream includes at least CS
monomers, wherein the resulting hydrocarbon resin has a number average molecular weight (Mn) of about 400 to 2000, a weight average molecular weight (Mw) of about 500 to 3500, a Z average molecular weight (Mz) of about 700 to 15,000, and a polydispcrsity (PD) as measured by Mw/Mn between about 1.2 and 5, where Mn, Mw, and Mz are determined by size exclusion chromatography (SEC).
In accordance with another feature of the invention, the feed stream includes at least C9 monomers, wherein the resulting hydrocarbon resin has a number average molecular weight (Mn) of about 400 to 1200, a weight average molecular weight (Mw) of about 500 to 2000, a Z average molecular weight (Mz) of about 700 to 6000, and a polydispcrsity (PD) as measured by Mw/Mn between about 1.2 and 3.5, preferably 1.2 and 2.5, where Mn, Mw, and Mz are determined by size exclusion chromatography (SEC).
In accordance with another feature of the invention, the hydrocarbon resin is hydrogenated.
BRIEF DESCRIPTION OF THE DRAWINGS
The present invention is further described in the detailed description which follows, in reference to the noted plurality of non-limiting drawings, and wherein:
Figures 1-4 depict contour plots generated from regression analysis of various pure monomer resin polymerizations.
DETAILED DESCRIPTION OF THE INVENTION
The particulars shown herein are by way of example and for purposes of illustrative discussion of the various embodiments of the present invention only and are presented in the cause of providing what is believed to be the most useful and readily understood description of the principles and conceptual aspects of the invention. In this regard, no attempt is made to show details of the invention in more detail than is necessary for a fundamental understanding of the invention, the description making apparent to those skilled in the art how the several forms of the invention may be embodied in practice.
All percent measurements in this application, unless otherwise stated, are measured by weight based upon 100% of a given sample weight. Thus, for example, 30%
represents 30 weight parts out of every 100 weight parts of the sample.
Unless otherwise stated, a reference to a compound or component includes the compound or component by itself, as well as in combination with other compounds and components, such as mixtures of compounds.
Before further discussion, a definition of the following terms will aid in the understanding of the present invention.
SOLID ACID: a solid which changes the color of a basic Hammett indicator with apK~<0.
METAL HALIDE SOLID ACID: a solid acid comprising metal covalently bonded to halide.
SUPPORTED METAL HALIDE SOLID ACID: a solid catalyst comprising a support) e.g., silica, silica-alumina, clay, zcolite, associated with a compound comprising metal covalently bonded to halide.
HYDROCARBON RESIN: a low molecular weight (i.e., a number average molecular weight of about 200 to less than about 3000 as determined by size exclusion chromatography (SEC)) thermoplastic polymer synthesized via thermal or catalytic polymerization of cracked petroleum distillates, terpenes, coal tar fractions, or pure olefmic monomers, wherein one of the monomers is at least a CS or higher.
PURE MONOMER: a composition comprising synthetically generated or highly purified monomer species, e.g., styrene from ethyl benzene or alpha methyl styrene from cumene.
WO 98/30587 PCT/US98l00012 PURE MONOMER FEED STREAM: a composition comprising any number of pure monomer species.
CS MONOMERS: a composition derived from petroleum processing, e.g., cracking, containing unsaturated hydrocarbons comprising CS and/or C6 olefin species boiling in the range from about 20°C to 100°C at atmospheric pressure.
C9 MONOMERS: a composition derived from petroleum processing, e.g., cracking, containing unsaturated aromatic C8, C9, and/or C10 olefin species with a boiling range of about 100°C to 300°C at atmospheric pressure.
FREELY-ASSOCIATED WATER: water associated with a solid acid catalyst or support where the water is chemisorbed and/or physisorbed.
As a general overview of the present invention, hydrocarbon resins are produced by using at least one of supported metal halides and metal halide solid acids as catalysts for the cationic polymerization of a feed stream containing at least one of pure monomer (e.g..
styrene based monomers), CS monomers, and C9 monomers. Resins with softening points (Ring and Ball) preferably in the range of about 5°C to 170°C, more preferably about 30°C
to 1 SO°C, can be prepared. These catalysts offer advantages over the traditional unsupported Lewis acid polymerization catalysts since the acid sites are an integral part of the solid or a Lewis acid is supported on a solid. Further, for the supported Lewis acids, the Lewis acid is supported on a solid and therefore can be removed from the reaction solution.
Looking at the present invention in more detail, hydrocarbon resins are prepared through a polymerization reaction wherein a feed stream containing at least one of pure monomer, CS monomers) and C9 monomers are contacted with a at least one of a supported metal halides and metal halide solid acid catalyst. Supported metal halides and metal halide solid acid catalysts which are useful in the current invention include, but are not limited to, the following.
Lewis acids on clays The Lewis acids on clays including, for example ZnCl2 AlCl3 AlBr3 FeCl3 SnCl4 TiCl4 ZrCl4 HfCl4 BiCl3 Lanthanide halides The clays supporting the Lewis acids including, for example Naturally occurring clay minerals, for example Kaolinite Bentonite Attapulgite Montmorillonite Clarit Fuller's Earth Hectorite Beidellite Synthetic clays, for example Saponite Hydrotalcite Montmorillonite clays treated with sulfuric or hydrochloric acid Modified clays (i.e., clays modified by backbone element replacement), e.g.
Aluminum oxide pillared clays Cerium modified alumina pillared clays Metal oxide pillared clays Lewis acids on silica or silica-alumina, for example ZnClz AICI, AlBr3 FeCl3 SnCla TiCl4 ZrCI~
HfCl4 BCI
BiCl3 Lanthanide halides Lewis acids on mesoporous silica or silica-alumina, for example ZnCl2 AlBr3 FeCl3 SnCl4 TiCl4 ZrCl4 HfCl4 BiCl3 Lanthanide halides Lewis acids on ion exchange resins, for example ZnClz AlCl3 AlBr3 FeCI
SnCl4 TiCl4 ZrCl4 HfCI~
BiCl3 Lanthanide halides Lewis acids on natural or synthetic zeolites The Lewis acids on zeolites including, for example ZnCl2 A1C1;
AlBr3 BC1~
FeClz SnCl4 TiCl4 ZrCl4 HfCl4 BiCI, Lanthanide halides The zcolites supporting Lewis acids including, for example Zeolite Y
Zeolite (3 (i.e., BEA) MFI (e.g., "Zeolite Sacony Mobil-5" ("ZSM-5")) MEL (e.g., "Zeolite Sacony Mobil-11" ("ZSM-11")) NaX
NaY
Faujasite (i.e., FAU) Mordenite (i.e., MOR) Polymer grafted aluminum halides Solid Inorganic Acids ZrCl4 HfCl4 Lanthanide halides As mentioned previously, the above list of supported metal halides and metal halide solid acid catalysts is not intended to be an exhaustive list. In selecting other supported metal halides and metal halide solid acid catalysts which may be useful in the present invention, it is generally true that the supported metal halides and metal halide solid acid catalyst should be more acidic than about -3 on the Hammett scale.
Examples of the lanthanide halides mentioned in the above list include ScCI,, YC1,, LaCI;, YbCI,, CeCl3) PrCl3, NdCl3, NdBr;, SmCl3, EuCI,, GdCI~, TbCl3, DyCI~, HoCI,, HoBr~, ErCI,, TmCI~, and LuCl3.
1 S Concerning the zeolites, the names BEA, MFI, MEL, FAU, and MOR are the framework structure type IUPAC definitions of the listed species.
Examples of polymer grafted aluminum halides mentioned in the above list arc found in U.S. Patent No. 5,414,177 to CHUNG et al. and U.S. Patent No. 5,409,873 to CHUNG
et al., the disclosures of which are herein incorporated by reference in their entireties.
Before use) the solid acid catalysts and/or supports may be treated to remove Creeiy-associated water to maximize the catalyst acidity and activity toward the polymcriration.
The freely-associated water may be removed by various techniques, including thermal treatment, reduced pressure treatment, dry atmosphere treatment such as nitrogen or air, or a combination thereof While not wishing to be bound by theory, removing freely-associated water maximizes the acid strength of the Lewis acid catalyst and makes the polymerizations more reproducible.
The freely-associated water may be removed from the solid acid catalyst and/or support by calcining which generally means heating the metal halide solid acid and/or support to high temperature without fusing the catalyst. The metal halide solid acid and/or support may be calcined under an inert atmosphere, such as nitrogen or dry air, or under reduced pressure. The calcining is performed for preferably up to about 8 hours or more, more preferably about 1 hour to 4 hours, preferably at temperatures up to about 700°C, more preferably about 100°C to 400°C.
The freely-associated water removed from the metal halide solid acid catalyst and/or support may have been derived from water (physisorbed water) or hydroxyl groups (chemisorbed water) associated with the metal halide solid acid catalyst andlor support. By removal of substantially all freely-associated water is meant removing all or essentially all physisorbed water and removing at least a majority of chemisorbed water.
For the supported metal halide acid catalysts, the solid acid catalyst may consist essentially of a single type of a metal halide, e.g., a Lewis acid, on a single type of support.
However, the supported metal halide solid acid catalyst may involve any combination of a single type or plurality of types of a metal halide on a single type or plurality of types of supports.
Before the support and the metal halide are combined, the support may be calcined.
The importance of calcining the support before the support and metal halide are combined varies depending upon the metal halide. For instance, calcination is critical for supported A1C1,, AlBr3, BFI, TiCl4, HfCl4, FeCI~, and BCI;. Calcination is important for supported ZrCl4 and BiCI~. In contrast, supported FeCI~ and ZnCI, may be used with or without pre-1 S calcination of the support.
It is expected that by controlling the conditions under which the at least one of supported metal halides and metal halide solid acid catalyst is calcined, such as controlling the temperature or time under which the calcination step takes place, tailoring of the physical properties of the resultant resin, such as its softening point or its molecular weight, may be achieved.
Many of the supported metal halides and metal halide solid acid catalysts of the present invention are most effective in the presence of a controlled amount of water in the feed stream. For instance, the feed stream may include less than about 500 ppm water, preferably less than about 200 ppm water, more preferably less than about 100 ppm water, and most preferably less than about SO ppm water.
Pure monomer feed streams may contain relatively pure styrene-based monomers such as styrene, alpha-methyl styrene, beta-methyl styrene, 4-methyl styrene, and vinyl toluene fractions. The monomers can be used as pure components or as blends of two or more monomer feeds to give desired resin properties. Preferred blends include about 20 wt% to 90 wt% alpha-methyl styrene with about 80 wt% to 10 wt% of one or more comonomers, preferably styrene, vinyl toluene, 4-methyl styrene or blends of these components. In addition, other alkylated styrenes can be used as monomers in this invention such as t-butyl styrene or phenyl styrene. Feed streams can be dried, if desired, and preferably contain less than about 200 ppm water, more preferably less than about 100 ppm water, and most preferably less than about 50 ppm water.
In the case of CS resins, the petroleum feed streams contain unsaturated CS
andlor S C6 olefins and diolefins boiling in the range from about 20°C to 100°C, preferably about 30°C to 70°C. In some cases, cyclopentadiene and methylcyclopentadiene components are removed from the feed by heat soaking at temperatures preferably between about 100°C and 160°C, and fractionating by distillation. Monomers found in these feedstocks may include but are not limited to olefins such as isobutylene, 2-methyl-2-butene, I -pentene, 2-methyl-1-pentene, 2-methyl-2-pentene, as well as 2-pentene, cycloolefins such as cyclopentene, and cyclohexene, diolefins such as 1,3-pentadiene, 1,4-pentadiene, isoprene, 1,3-hexadienc, and 1,4-hexadiene, cyclodiolefins such as cyclopentadiene, dicyclopentadiene, and alkyl substituted derivatives and codimers of these cyclodiolefins. Commercial samples of this type of feed include, but are not limited to "Naphtha Petroleum 3 Pipcrylencs"
from Lyondell Petrochemical Company, Houston, TX, regular "Piperylcne Concentrate"
or "Super Piperylene Concentrate" both from Shell Nederland Chemie B.V., Hoogvilet, the Netherlands. The CS feed streams generally contain at least about 70 wt%
polymerizablc monomers with at least about SO wt% 1,3-pentadiene. The CS feed stream may contain low levels of isoprene, generally contains 2-methyl-2-butene, and may contain one or more cyclodiolefins.
Also concerning CS monomer feed streams, in addition to the reactive components, nonpolymerizable components in the feed may include saturated hydrocarbons which can be codistilled with the unsaturated components such as pentane, cyclopentane, or 2-mcthylpentane. This monomer feed can be copolymerized with C4 or CS olefins or dimers as chain transfer agents. Chain transfer agents may be added to obtain resins with lower and narrower molecular weight distributions than can be prepared from using monomers alone.
Chain transfer agents stop the propagation of a growing polymer chain by terminating the chain in a way which regenerates a polymer initiation site. Components which behave as chain transfer agents in these reactions include but are not limited to isobutylene, 2-methyl-1-butene, 2-methyl-2-butene or dimers or oligomers of these species. The chain transfer agent can be added to the reaction in pure form or diluted in a solvent. Feed streams can be dried if desired and preferably contain less than about 500 ppm water, more preferably less WO 98/30587 PCTlUS98/00012 than about 200 ppm water, and most preferably less than about SO ppm water.
In the case of C9 monomer resins, the feed streams contain unsaturated aromatic C8, C9, and/or CI O monomers with a boiling range of about 100°C to 300°C at atmospheric pressure. Aromatic C8-C 10 feed streams (also referred to as C9 feed streams) can be derived fiom steam cracking of petroleum distillates. Monomers found in these feed stocks may include but are not limited to styrene, vinyl toluene, indene, dicyclopentadiene, and alkylated derivatives of these components. Commercial samples of this type of feed include but are not limited to "LRO-90" from Lyondell Petrochemical Company, Houston, TX, "DSM C9 Resinfeed Classic" from DSM, Geleen, the Netherlands, "RO-60" and "RO-80"
from Dow Chemical Company of Midland, Michigan, and "Dow Resin Oil 60-L" from the Dow Chemical Company of Terneuzen, the Netherlands. The C9 feed stream generally contains at least about 20% by weight, preferably about 30% to 75% by weight, and most preferably about 35% to 70% by weight polymerizable unsaturated hydrocarbons.
The remainder is generally alkyl substituted aromatics which can be incorporated into the resins by alkyiation reactions. Feed streams can be dried if desired and preferably contain less than about 500 ppm water, more preferably less than about 200 ppm water, and most preferably less than about 50 ppm water.
The feed streams may be limited to pure monomer, CS monomers, or C9 monomers.
Alternatively, cofeed streams can be used in combination with main feed streams of pure monomer, CS monomers, or C9 monomers. Depending upon the main feed stream, pure monomer, CS monomers, C9 monomers, or even terpenes, and any combination thereof, may serve as a cofeed stream. Terpene feed stocks include but are not limited to d-limonene, alpha- and beta-pinene, as well as dipentene. Resins from blends of main feed streams with cofeed streams may be prepared in the range of about 30 wt% to 95 wt°/~ rnain feed with about 70 wt% to 5 wt% of a cofeed, preferably about SO-85 wt% main feed and about 50 wt% to 1 S wt% cofeed.
The polymerization feed stream preferably contains between about 20 wt% and 80 wt% monomers, more preferably about 30 wt% to 70 wt%, and most preferably about 40 wt% to 70 wt%. In the case of CS resins, the feed may contain up to about 40 wt% of a chain transfer agent, more preferably up to about 20 wt%, chain transfer agents as discussed above. The feed stream also contains about 80 wt% to 20 wt% of a solvent such as toluene, octane, higher boiling aromatic solvent, aliphatic solvent, or solvent blend.
-lg_ Regarding the solvents, for pure monomer polymerization, the preferred solvents are aromatic solvents. Typically toluene, xylenes, or light aromatic petroleum solvents such as "Aromatic 100" from Exxon Chemical Company, Houston, TX, "HiSol 10" from Ashland Chemical Incorporated, Columbus, OH, and "Cyclosol 53" from Shell Chemical Company, S Houston, TX can be used. These solvents can be used fresh or recycled from the process.
The solvents generally contain less than about 200 ppm water, preferably less than about 100 ppm water, and most preferably less than about 50 ppm water.
For C5 polymerization, the preferred solvents are aromatic solvents.
Generally, unreacted resin oil components are recycled through the process as solvent. In addition to the recycled solvents, toluene, xylenes, or aromatic petroleum solvents such as "Solvesso 100" from Exxon Chemical Company, Houston, TX and "Shellsol A" from Shell Chemical Company, Houston, TX can be used. These solvents can be used fresh or recycled from the process. The solvents generally contain less than about 500 ppm water, preferably less than about 200 ppm water, and most preferably less than about 50 ppm water.
For C9 polymerization, the preferred solvents are aromatic solvents.
Generally, unreacted resin oil components are recycled through the process as solvent. In addition to the recycled solvents, toluene, xylenes, or aromatic petroleum solvents such as "Solvesso 100" from Exxon Chemical Company, Houston, TX and "Shcllsol A" from Shell Chemical Company, Houston, TX can be used. These solvents can be used fresh or recycled from the process. The solvents generally contain less than about 200 ppm water, preferably less than about 100 ppm water, and most preferably less than about 50 ppm water.
Concerning the polymerization reaction conditions, a first important variable is the amount of at least one of supported metal halides and metal halide solid acid catalyst which is used. The at least one of supported metal halides and metal halide solid acids are preferably used at a level of about 0.1 wt% to 30 wt% based on the weight of the monomer.
For pure monomer resins, the at least one of supported metal halides and metal halide solid acid concentration is preferably about 0.1 to 15 wt%, more preferably about 0.5 wt% to 10 wt%, and most preferably about 0.5 wt% to 8 wt%. For C5 monomers, the at least one of supported metal halides and metal halide solid acid concentration is preferably about 0.5 wt% to 30 wt%, more preferably about 1 wt% to 20 wt%, and most preferably about 3 wt%
to 15 wt%. For C9 monomers, the at least one of supported metal halides and metal halide solid acid concentration is preferably about 0.5 wt% to 30 wt%, more preferably about 1 wt% to 20 wt%, and most preferably about 3 wt% to 15 wt%.
A second important variable in the reaction is the reaction sequence, i.e., the order and manner in which reactants are combined. In one reaction sequence, the catalyst can be added to a solution of the monomers incrementally while controlling the reaction temperature. Alternatively, in another reaction sequence, the monomer can be added incrementally to a slurry of the at least one of supported metal halides and metal halide solid acid catalyst in a solvent. For a set catalyst level and reaction temperature, substantially lower softening point resins are obtained when the monomer is added to a catalyst slurry.
As discussed in more detail in the following paragraphs, lower molecular weights and narrow polydispersity (PD), i.c., Mw/Mn, as measured by size exclusion chromatography, are obtained when the monomer is added to the catalyst solution compared with resins where the catalyst is added to the monomer.
The molecular weight averages of the resins were measured using size exclusion chromatography, SEC. The column set for the analysis consisted of four Waters I S "Ultrastyragel" columns of 500, 500, 1000, and 100 A pore size, in series, (Pan Nos. VVAT
010571, 010571, 010572, 010570 respectively) available from Waters Corporation, Milford, MA. The molecular weight calibration was calculated from the peak elution times of a standard set of narrow molecular weight distribution polystyrene polymers. The calibration set encompassed 18 standards ranging in peak molecular weight from I 62 to 43,900. The peak molecular weight of a narrow molecular weight standard is defined as equal to (MwMn)''' (ASTM test method D3536-76). The calibration curve is defined by a third degree polynomial curve fit of a plot of log MW vs. V~/V" where V~ is the elution volume of the standard and V, is the elution volume of the reference peak, oxygen, present as dissolved air in the injected solution. The columns and detector cell (Hewlett-Packard Differential Refractometer) are maintained at 40°C. The solvent (mobile phase) was tetrahydrofuran containing 250 ppm butylated hydroxytoluene (BHT, 2,6-di-tert-butyl-4-methylphenol) as a stabilizer (the tetrahydrofuran with BHT being available from Burdick and Jackson, Muskegon, MI). The mobile phase reservoir is purged with helium and is maintained at a flow rate of I milliliter per minute. Under these conditions, BHT eluted at 35.86 minutes. Samples are dissolved in THF, 0.25% wt/vol, and filtered through a 0.45 micron pore size "TEFLON" (polytetrafluoroethylene) membrane filter prior to injection (200 microliters) into the chromatograph. The reported molecular weights are the "polystyrene equivalent" molecular weights as calculated from the calibration curve.
For the pure monomer resins, the resins produced using the current invention have number average molecular weights (Mn) ranging from about 400 to 2000, weight average molecular weights (Mw) ranging from about 500 to 5000, Z average molecular weights (Mz) S ranging from about 500 to 10,000, and polydispersities (PD) as measured by Mw/Mn between about 1.2 and 3.5, typically between about 1.2 and 2.5. For the CS
hydrocarbon resins, the resins produced using the current invention have number average molecular weights (Mn) ranging from about 400 to 2000, weight average molecular weights (Mw) ranging from about 500 to 3500, Z average molecular weights (Mz) ranging from about 700 to 15,000, and polydispersities (PD) as measured by Mw/Mn between about I.2 and S, typically between about 1.2 and 3.5. For the C9 hydrocarbon resins, the resins produced using the current invention have number average molecular weights (Mn) ranging from about 400 to 1200, weight average molecular weights (Mw) ranging from about 500 to 2000, Z average molecular weights (Mz) ranging from about 700 to 6000, and polydispersities (PD) as measured by Mw/Mn between about 1.2 and 3.5, typically between about 1.2 and 2.5.
As mentioned previously, it is expected that narrower polydispcrsitics and lower molecular weights are obtained when the monomer is added to the catalyst solution than when the catalyst is added to the monomer. Taking into consideration the effect of the reaction sequence, it is expected that polydispersities more narrow than those obtained using traditional unsupported Lewis acid Friedel-Crafts catalysts can be obtained using the at least one of supported metal halides and metal halide solid acids if desired. Narrow polydispersity is important to ensure compatibility of resin with polymers in end use applications.
A third important reaction variable is the reaction temperature.
Polymerization temperatures between about -50°C and 150°C can be used in these reactions, however, more preferred reaction temperatures are between about -20°C and 100°C, most preferred temperatures are between about 0 ° C and 70 ° C. For pure monomer, the reaction temperature is preferably between about -50°C and 100°C, more preferably between about -20°C and 75°C, and most preferably between about -10°C and 60°C.
For CS monomers, the reaction temperature is preferably between about -50°C and 100°C, more preferably between about -20°C and 75°C, and most preferably between about -10°C
and 70°C. For C9 monomers, the reaction temperature is preferably between about 0°C and 150°C, more preferably between about 10°C and 120°C, and most preferably between about 20°C and 110°C.
Temperature is found to have a significant effect on the properties of the resulting resins.
Higher molecular weight and high softening point resins are prepared at lower reaction temperatures. The reaction time at reaction temperature is preferably between about 30 minutes and 8 hours, and more preferably between about 1 hour and 4 hours.
The polymerization process can be carried out as a continuous, semi-batch, or batch process in such diverse reactors as continuous, batch, semi-batch, fixed bed, fluidizcd bed, and plug flow. For instance, in continuous processes, a solution of the monomers can be passed over the catalyst in a fixed bed, or the monomers can be cofed with a catalyst slurry into a continuous reactor.
The reaction may be stopped by physically separating the at least one of supported metal halides and metal halide solid catalysts from the products. Physical separation may render the reaction solution neutral. Furthermore, physical separation can be performed by 1 S simple filtration or by separation of the resin solutions from a fixed catalyst bed. As a result, physical separation is easy and complete such that, for many the at least one of supported metal halides and metal halide solid acid catalysts, acid functionality and catalyst residue are not left in the resin product.
If leaching of acid is possible, then acid neutralization is required. This step is commonly known in the art as "quenching". For the at least one of supported metal halides and metal halide solid acid catalysts of the present invention which require quenching, less salt is generated than by traditional unsupported Lewis acid catalysts.
Thus, use of the at least one of supported metal halides and metal halide solid acid catalysts minimizes or eliminates the need for extra processing steps to quench the reactions, neutralize the catalyst, and filter the catalyst salt residues from the resulting products.
Once the at least one of supported metal halides and metal halide solid acid catalyst and resin solution are separated, the resin solution can be stripped to remove unreacted hydrocarbons, solvents, and low molecular weight oligomers which can be recycled through the process. When pure monomer is reacted, water white resins can be obtained from this invention in yields of up to about 99% based on starting monomer.
Resins obtained from this invention typically have softening points as measured by ASTM-E28 "Standard Test Method for Softening Point by Ring and Ball Apparatus"
(revised 1996), varying from preferably about 5°C to 170°C, more preferably from about 30°C to 150°C. For pure monomer, the softening points preferably range from about S°C
to 170°C, more preferably from about 50°C to 1 SO°C. For CS hydrocarbon resins, the softening point ranges from preferably about 5°C to 170°C, more preferably from about 50°C to 150°C, and most preferably about 70°C to 130°C. For C9 hydrocarbon resins, the softening point is preferably up to about 170°C, and the softening point range is most preferably from about 70°C to 160°C. Flowable resin or those that are liquids at room temperature can also be prepared if desired using proper reaction conditions.
After the resin is produced, it may be subsequently subjected to hydrogenation to reduce coloration and improve color stability. Hydrogenation of resins is well known in the art. For a discussion of hydrogenation, reference is made to U.S. Patent No.
5,491,214 to DAUGHENBAUGH et al., which is incorporated herein by reference in its entirety.
The resins of the current invention can be used as modifiers in adhesives, sealants, printing inks, protective coatings, plastics, road markings, flooring, and as dry cleaning retexturizing agents.
The at least one of supported metal halides and metal halide solid acid catalysts of the present invention offer several advantages over unsupported Lewis acids (e.g., AICI,) AIBr,, BF,, complexes of BF3, TiCla, and others which arc traditionally used for Friedcl-Crafts polymerizations). Many of these advantages are a result of the acid sites being an integral part of the solid catalysts or a Lewis acid supported on a solid.
Because the acid sites are an integral part of the solid catalyst or the Lewis acid is supported on a solid, contamination of the resin products or solvents with catalyst residues is minimal. As a result, the at least one of supported metal halides and metal halide solid acid catalysts do not impart color to the hydrocarbon resins due to catalyst residues. If pure styrene-based monomers are used, the resulting resins can be water white.
The at least one of supported metal halides and metal halide solid acid catalysts of the present invention can generally be regenerated and recycled to thereby minimize waste disposal of spent catalyst. In contrast, the unsupported Lewis acids are generally single use catalysts.
Further, the at least one of supported metal halides and metal halide solid acid catalysts of the present invention are nonhazardous when compared with traditional unsupported Lewis acid catalysts such as BF3 and AICI 3 The catalysts of the present WO 98/30587 PCT/US98l00012 invention generally do not generate corrosive or hazardous liquid or gaseous acids on exposure to moisture.
The present invention will be further illustrated by way of the following Examples.
Examples 1-17 involve pure monomer resins, Examples 18-53 involve CS resins, and $ Examples 54-76 involve C9 resins. These examples are non-limiting and do not restrict the scope of the invention.
Unless stated otherwise, all percentages, parts, etc. presented in the examples are by weight.
These examples illustrate the effect of zinc chloride supported on silica as a catalyst for the polymerization of pure monomer.
Catalyst preparation involves dissolving 20 grams of reagent grade zinc chloride in 75-100 ml methanol and adding to a slurry of synthetic amorphous silica, Grade "EP-12", Crosfield Limited, Warrington, England. The solution is stirred for 1 hour.
The solvent is slowly removed on a rotary evaporator to avoid bumping of the mixture. After the rotary evaporation, the material should be a free flowing solid. The catalyst is calcined by carefully heating the solid for 2 hours at 2 mm of Hg at 40°C, followed by 2 hours at 2 mm of Hg at 100°C, and finished at 1 hour at 2 mm of Hg at 140°C.
The catalyst is handled in a nitrogen filled glove bag prior to use.
Catalyst recycle tests were done in a jacketted one gallon reactor with a flat-bed turbine agitator, cooling coil, sample line, thermowell, bottom valve and sintered metal filters. The filters were located on the end of the sample line and in the bottom valve seat of the reactor and had a nominal rating of 7 microns. The jacket of the reactor was controlled at 0°C t 5°C. Thirty-five (35) grams of the supported zinc chloride catalyst described above and 1000 grams of toluene were added to the reactor. The catalyst/toluene mixture was cooled to 0°C.
A mixture of 866 grams of alpha-methyl styrene and 366 grams of styrene were pumped into the 1 gallon reactor at a rate such that the temperature was controlled to 0°C
~ 5°C by flowing -20°C fluid through the cooling coil. The time for pumping in the monomer was 100 minutes. The reactor was held at 0°C for an additional 3 hours. The catalyst was contained in the reactor by using the two in situ filters. One gram of catalyst was removed and one gram of fresh catalyst was added between each of the catalyst recycle tests. An aliquot of the filtered reaction mixture was rotary evaporated, with an end condition of 3 mm of Hg and 190°C to produce a resin product.
Subsequent reactions using the same catalyst were done in essentially the same manner. The yield and properties of the resins are listed in Table 1.
Ex. Catalyst Yield SofteningMolecular P Weight i t o Mn Mw Mz n (R&B) 1 ZnClz on silica 87% 135C 1176 2407 4492 2 Catalyst recycled from 76% 142C 1431 3268 6825 Example 1 3 Catalyst recycled from 59% 142C 1383 3467 7486 Example 2 The following examples illustrate the preparation of pure monomer resins using a catalyst to monomer addition scheme with styrene based monomers and a supported ZnClz on silica catalyst.
CATALYST PREPARATION
Zinc chloride (98% Aldrich, Milwaukee, WI), S.0 grams (0.037 mol), was dissolved in SO milliliters ofmethanol (reagent grade, Aldrich, Milwaukee, WI). The support material, 13.5 grams, ("EP12" silica from Crosfield Catalysts, Warrington, England which had been calcined at 1 SO°C under vacuum to remove excess water for the purpose of obtaining an accurate weight of the support) was added to the methanol solution. The slurry was stirred at room temperature for 30 minutes. The solvent was removed on a rotary evaporator at 2-S
mm Hg with mild heating to obtain a flowable powder. The catalyst was calcined at 150°C
under a dry nitrogen purge for 2 hours prior to use.
POLYMERIZATION
A S00 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, thermometer, and a dropping addition funnel. The flask was charged with 86.6 grams alpha-methyl styrene (reagent grade, Aldrich, Milwaukee, WI), 36.6 grams styrene (reagent grade, Aldrich, Milwaukee, WI), and 36.6 grams toluene (reagent grade, Aldrich, Milwaukee, WI). The monomers and solvent were dried as follows: the styrene based monomers were dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer) immediately prior to use, the toluene was dried over 3 angstrom molecular sieves prior to use.
The catalyst, 3.7 grams ZnClz/Si02 - prepared as described above, was transferred to the solid addition funnel in an inert, moisture free atmosphere. The catalyst was added to the reaction from the dropping addition funnel over 15 minutes maintaining the target reaction temperature with external cooling of the reaction flask. The reaction was stirred at temperature for a total reaction time of 1-2 hour.
After the reaction time was completed, the resulting resin solution was vacuum filtered from the catalyst at room temperature. The reaction flask and catalyst filter cake were rinsed with approximately 100 milliliters of toluene.
After catalyst filtration, the solvent was removed from the resin solution at 100°C
I S at 2-5 mm Hg. The resin oil was placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube, thermometer, and attached to a condenser and receiving flask. The resin oil was heated to 235°C with a nitrogen purge followed by a steam purge at 235-245°C to remove the light oil products. The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The resin produced has the properties listed in Table 2.
Example Reaction Yield SofteningMolecular Weight Temperature Point (R&B) Mn Mw Mz 4 0C 69% 150C 1770 4050 8250 5 25C 83% 122C 960 1470 2430 The following examples illustrate a range of resin properties available from the current invention using styrene and alpha-methyl styrene as the monomers and a calcined ZnClz on silica as the catalyst. When combined, the following examples serve to define a half factorial designed experiment with two variables. The variables in these experiments include reaction temperature and catalyst loading. Replicate points are included to estimate experimental error. The results from the following examples are used to generate a model equation for each measured response in terms of the variables studied. The responses S studied in these examples include: product yield, Ring and Ball softening point, and molecular weight distribution. as defined by number average molecular weight (Mn), weight average molecular weight (Mw), and Z average molecular weight (Mz).
CATALYST PREPARATION
Zinc chloride (98% Aldrich, Milwaukee, WI) 20.0 grams (0.15 mol) was dissolved in 300 milliliters of methanol (reagent grade, Aldrich, Milwaukee, WI). The support material, 80 grams, ("EP12" silica from Crosfield Catalysts, Warrington, England) was added to the methanol solution. The slurry was stirred at room temperature for 30 minutes.
The solvent was removed on a rotary evaporator at 2-5 mm Hg with mild heating to obtain a flowable powder. Prior to use, the catalyst was calcined for 2 hours at 40°C, 1 hour at 1 S 100°C, and 2 hours at 150°C all under vacuum.
POLYMERIZATION
A S00 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, thermometer, and a dropping addition funnel. The flask was charged with 86.6 grams alpha-methyl styrene (reagent grade, Aldrich, Milwaukee, WI), 36.6 grams styrene (reagent grade, Aldrich, Milwaukee, WI), and 36.6 grams toluene (reagent grade, Aldrich, Milwaukee, WI). Immediately prior to use, the styrene based monomers were dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer). Also prior to use, the toluene was dried over 3 angstrom molecular sieves.
The catalyst, prepared as described above, was transferred to the dropping addition funnel in an inert, moisture free atmosphere. The catalyst was added to the reaction from the dropping addition funnel over 15 minutes maintaining the target reaction temperature with external cooling of the reaction flask. The reaction solution was stirred at temperature for a total reaction time of 1 hour.
After completion of the reaction time, the resulting resin solution was vacuum filtered from the catalyst at room temperature. The reaction flask and catalyst filter cake were rinsed with approximately 100 milliliters of toluene.
After catalyst filtration, the resin oil was placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube, thermometer, and attached to a condenser and receiving flask. The resin oil was heated to 235°C
with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products.
The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The reaction conditions for each example are outlined in the Table 3 below.
The level of each variable was coded as -1, 0, or 1 for low, middle, and high, respectively. Use of coded variable values facilitates generation of the model equations for each response.
Coded values are included in parenthesis.
Ex. CatalystReaction Yield Softening Mol eculareight Point W
1 S LoadingTemp. (R&B) (wt%) Mn Mw Mz 6 3.25 25C (0) 74% 118C 910 1470 2420 (0) 7 1 (-1) 50C (I) 72% 68C 610 830 1130 8 6 (1) 25C (0) 86/~ 100C 960 I~50 2630 9 1 (-1 0C (-1 10% 142C 1240 2080 4400 ) ) 10 3.25 50C ( 1 73% 76C 660 890 1220 (0) ) I 3.25 25C (0) 77% 125C 1000 1680 2810 1 (0) 12 6 ( 50C ( 1 18% 70C 450 480 520 I ) ) 13 3.25 0C (-1) 36% 131C 1650 3100 5700 (0) 14 1 (-1) 25C (0) 64% 133C 1080 1680 2620 IS 6 (1) 0C (-1) 70% 139C 2130 5490 11780 16 3.25 25C (0) 63% 103C 790 1150 2110 (0) The data from the above tables was analyzed by regression analysis for each of the responses (steam stripped product yield, Ring and Ball softening point, Mn molecular weight, Mw molecular weight, and Mz molecular weight). The process variables, (reaction temperature (TMP) and catalyst loading (CAT), were coded to -l, 0, and 1 for the low, mid, _2g_ and high levels respectively. The following regression models were obtained based on the coded variables. The proportion of the variation in the response data that is explained by the models is listed as RZ(adj).
Equation 1 Resin Yield % - 72.8 - 29.3(CAT)(TMP) - 26.3(TMP)z Rz(adj) = 78.9%
Equation 2 R & B Softening Point - 110 - 33.0(TMP) Rz(adj) = 82.1%
Equation 3 In[Mn] - 6.86 - 0.537(TMP) - 0.214(CAT)(TMP) RZ(adj) = 93.7%
Eauation 4 In[Mw] - 7.32 - 0.780(TMP) - 0.385(CAT)(TMP) R-'(adj) = 94.0%
Equation 5 (n[Mz] - 7.81 - 1.02(TMP) - 0.45(CAT)(TMP) R'(adj) = 96.4%
The regression equations listed above can be used to predict the properties of all resins which can be obtained for a set of reaction conditions where the control variables lie within the intervals tested. Contour plots can be generated to investigate the factor effects and make comparisons of resin properties predicted to be generated using various reaction conditions. Sample contour plots are shown in Figures 1 - 4 for product yield, Mn, Mw, and Mz molecular weights versus catalyst loading and reaction temperature.
This example demonstrates the use of supported aluminum trichloride as a catalyst for the polymerization of styrene based monomers.
CATALYST PREPARATION
Aluminum chloride (- 40 mesh, Vanchlor Co., Inc., Lockport, NY), 20.0 grams (0.15 mol), was dissolved in 100 milliliters of toluene dried over 4 angstrom molecular sieves (reagent grade, Aldrich, Milwaukee, WI). The support material, 80 grams, ("EP12" silica from Crosfield Catalysts, Warrington, England) was dried prior to contacting the aluminum trichloride solution for 2 hours at 40°C, 1 hour at 100°C, and 2 hours at 150°C all under vacuum. The aluminum trichloride solution was added to the dried support material and the resulting slurry was stirred at room temperature for 30 minutes. The solvent was removed under vacuum at 2-5 mm Hg while maintaining the temperature near 40°C
to obtain a flowable powder. Prior to use, the catalyst was stored and handled in an inert atmosphere.
POLYMERIZATION
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, thermometer, and a dropping addition funnel. The flask was charged with 86.6 grams alpha-methyl styrene (reagent grade, Aldrich, Milwaukee, WI), 36.6 grams styrene (reagent grade, Aldrich. Milwaukee) WI), and 36.6 grams toluene (reagent grade, Aldrich, Milwaukee, WI). Immediately prior to use, the styrene based monomers were dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer). Prior to use, the toluene was dried over 3 angstrom molecular sieves.
The catalyst, 2.5 wt% based on monomer, was transferred to the dropping addition funnel in an inert, moisture free atmosphere. The catalyst was added to the reaction from the dropping addition funnel over 1 S minutes maintaining a 25°C
reaction temperature with external cooling of the reaction flask. The reaction solution was stirred at temperature for a total reaction time of 1 hour.
After completion of the reaction time, the resin solution was vacuum filtered from the catalyst at room temperature. The reaction flask and catalyst filter cake were rinsed with approximately 100 milliliters of toluene.
After catalyst filtration, the resin oil was placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube, thermometer, and attached to a condenser and receiving flask. The resin oil was heated to 235°C
with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products.
The steam purge was S continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The following summarizes the reaction conditions and resin properties.
Reaction temperature 25°C
Resin yield 24%
Ring and Ball Softening Point 59°C
Molecular Weight Mn 520 Mw 600 Mz 740 These examples illustrate the effect of zinc chloride supported on a variety of substrates as a catalyst for the polymerization of piperylene concentrate, a CS feed.
CATALYST PREPARATION
Zinc chloride (98% Aldrich, Milwaukee, WI) 27.3 grams (0.2 mol ) was dissolved in 300 milliliters of methanol (reagent grade, Aldrich, Milwaukee, WI). The support material, 100 grams, ("F-22" and "F-6" acid treated clays from Engelhard, Iselin, NJ, "K-10"
acid treated clay from Sud Chemie, Munich, Germany, or "EP12" silica from Crosfield Catalysts, Warrington, England) was added to the methanol solution. The slurry was stirred at room temperature for 30 minutes. The solvent was removed on a rotary evaporator at 2-5 mm Hg with mild heating to obtain a flowable powder. The catalyst was calcined at 1 SO°C
under a dry nitrogen purge for 2 hours prior to use.
POLYMERIZATION
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, a thermometer, and a dropping addition funnel. The flask was charged with 60 grams of toluene (reagent grade, Aldrich Milwaukee, WI) and 14 grams of the supported zinc chloride catalyst as prepared above. The catalyst slurry was heated to SO°C with stirring.
Piperylene concentrate (Naphtha Petroleum 3 "Piperylenes", Lyondell Petrochemical Company, Houston, TX), 140 grams, was added to the nitrogen purged reaction flask via the dropping addition funnel over 15 minutes. Immediately prior to use, the monomers and solvent were dried as follows, the solvents were dried over 4 angstrom molecular sieves and the piperylene concentrate was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams of alumina to 1 milliliter of monomer).
The reaction solution was stirred at 50°C for a total reaction time of one hour. The resulting resin solution was separated from the catalyst by vacuum filtration at room temperature. The volatile components and solvent were removed by heating the reaction solution to 50°C under vacuum (2-5 mm Hg) for 2 hours. The flask was fitted with a distillation head with an adaptor for an inlet tube and a thermometer, and attached to a condenser and receiving flask. The resin oil in the flask was then heated to 235°C with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products. The steam purge was continued until less than t ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The resins produced have the properties listed in Table 4. Examples 18-21 are in accordance with the present invention, whereas Comparative Example 22 is for comparison purposes.
Example Catalyst Yield SofteningMolecular P Weight i o nt Mn Mw Mz (R&B) 18 ZnClz on F-22 13% 40C I 520 2710 6500 Clay S 19 ZnCl2 on F-6 28% 41 C 1400 2490 6760 Clay 20 ZnCIZ on K-10 13% - 1160 2180 5160 Clay 21 ZnCl2 on EP12 64% 44C 1350 2360 4320 silica 22 ZnCh unsupported0% - - - -These examples illustrate the effect of reaction temperature on the polymerization of piperylene concentrate, a CS feed, with zinc chloride supported on silica.
Reaction procedures are similar to those listed for Examples l 8-22. The catalyst used was ZnClz on "EP12" silica prepared as described in Example 7 above. The reaction temperature was varied as described in the Table 5 below with the properties of the resulting resin also listed in Table 5.
TABLE S
Example Catalyst and Yield SofteningMolecular R P Weight ti i T
eac nt on o Mn Mw Mz emperature (R&B) 23 ZnCI,/Si02 - 50C 50'% 30C 1000 1710 3260 24 ZnCI~/SiO~ - 25C 29% 27C 1410 2300 3600 25 ZnCh/SiOz - 0C 14% 31 C 1480 2640 4360 These examples illustrate the effect of zinc chloride loading on silica and the total zinc loading in the reaction on the polymerization of piperylene concentrate, a CS feed. At a constant wt% ZnClz based on monomer, higher resin yields are obtained at lower loadings of ZnClz on the silica. For a given loading of ZnCl2 on silica, higher yields are obtained at higher loadings of catalyst with respect to monomer.
CATALYST PREPARATION
Catalyst A
Zinc chloride on silica was prepared as described in Example 21.
Catalyst B
Zinc chloride (98% Aldrich, Milwaukee, WI) 13.7 grams (0.059 mol) was dissolved in 150 grams of methanol (reagent grade, Aldrich, Milwaukee, WI). The support material, 25 grams, ("EP12" silica from Crosfield Catalysts, Warrington, England) was added to the methanol solution. The slurry was stirred at room temperature for 30 minutes.
The solvent was removed on a rotary evaporator at 2-S mm Hg with mild heating to obtain a ilowablc powder. The catalyst was calcined at 150°C under a dry nitrogen purge for 2 hours prior to use.
1 S Catalyst C, D, and E
The procedures for preparing catalysts C-E were similar to the procedures outlined for catalyst B. The zinc chloride loading for each catalyst is as follows, 20.> grams for catalyst C, 27.3 grams for catalyst D, and 34.2 grams for catalyst E using 25 grams of silica.
POLYMERIZATION
Preparation of the resins was as described for Examples 18-22. Catalysts and catalyst loadings were as described in the Table 6 and the resulting resin had the properties listed in Table 6.
ExampleCat. Loading LoadingYield SofteningMolecular Weight Cat. ZnClz Point wt% wt% (R&B) Mn Mw Mz 26 A 10 2.1 64% 44C 1350 2360 4320 27 B 3.6 1.3 23% 39C 1630 3000 5400 28 B 6.1 2.1 26% 43C 1690 3050 5390 29 B 10 3.5 39% 42C 1540 2810 4960 30 C 3.4 1.5 12% 21 C 1370 2290 4930 31 C 4.8 2.1 21% 25C 1410 2220 3750 32 C 10 4.5 34% 19C 1270 1990 3110 33 D 2.5 1.3 6% 41 C 1890 3660 6810 34 D 4.1 2.1 11% 38C 1790 3270 5820 S 35 D 10 5.2 27% 39C 1550 2970 5560 36 E 3.7 2.1 7% 25C 1520 2540 4480 These examples illustrate the effect of unsupported metal halides as catalysts for the I 0 polymerization of pipcrylene concentrate, a CS feed. In particular, these examples compare the effectiveness of the solid acid catalyst ZrCl4 with the effectiveness of the conventional Lewis acids FeCI, and A1C1~.
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, a thermometer, and a dropping addition funnel. The I S flask was charged with 30 grams toluene (reagent grade, Aldrich Milwaukee, WI) and 0.008 moles of the metal chloride catalyst, FeCl3 97%, ZrCI~ 99.9+% (all from Aldrich, Milwaukee, WI) and A1C13 (Vanchlor Co. Inc., Lockport, NY). The catalyst slurry was heated to 50°C with stirring.
Piperylene concentrate (Naphtha Petroleum 3 "Piperylenes", Lyondell Petrochemical 20 Company, Houston, TX), 100 grams, was added to the nitrogen purged reaction flask via the dropping addition funnel over 1 S minutes. Immediately prior to use, the monomers and solvent were dried as follows, the solvent was dried over 4 angstrom molecular sieves and the piperylene concentrate was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams of alumina to 1 milliliter of monomer).
25 The reaction solution was stirred at 50°C for a total reaction time of two hours.
Catalyst solids were removed from the reaction solution via filtration. After filtration, the reaction solutions were quenched with 4 milliliters of NI-I40H in 100 milliliters of water and the water removed using a separatory funnel. After quenching, the resin solution was separated from the catalyst salts formed during quenching by vacuum filtration at room 30 temperature.
The resin oil was then placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube and a thermometer, and attached to a WO 98/30587 PCT/US98/00(112 condenser and a receiving flask. The resin oil was heated to 200°C to 235°C with a nitrogen purge for all resins, followed by a steam purge at 235-245°C to remove light oil products for the AlCl3 and ZrCl4 reactions. The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was $ collected. The steam purge was followed by a nitrogen purge at 235°C
to remove water from the remaining resin.
The resins produced have the properties listed in Table 7. Examples 37 and 39 are in accordance with the invention, whereas Comparison Example 38 is for comparison purposes.
Example Catalyst Yield Softening Molecular Point Weight (R&B) Mn Mw Mz 37 FeCl3 7%' - 950 3750 16910 38 A1C1~ 52% 95C 1580 3120 6790 39 ZrCl4 52% ~ 68C I 2250 I 5730 I 15160 1. Sample was not steam stripped.
These examples illustrate the effect of supported metal halides as catalysts for the polymerization of piperylene concentrate, a CS feed.
CATALYST PREPARATION
Supported ZnCl2 and FeCl3 Zinc chloride, 98+%, or iron chloride, 97%, {both from Aldrich, Milwaukee, WI) grams was dissolved in 100 milliliters of methanol (Reagent grade, Aldrich, Milwaukee, WI). The support material, 24 grams, ("EP12" silica from Crosfield Catalysts, Warrington, England) was added to the methanol solution. The slurry was stirred at room temperature for 30 minutes. The solvent was removed on a rotary evaporator at 2-5 mm Hg with mild heating to obtain a flowable powder. The catalyst was calcined at 150°C
under a dry nitrogen purge for 2 hours prior to use.
Supported BiCl3, AICl3, and ZrCl4 The silica support material ("EP12" from Crosfield Catalysts, Warrington, England) was dried under vacuum, 2-5 mm Hg, using the following thermal cycle, 0.5 hours at room temperature, 1 hour at 35-40°C, 1.5 hours at 100°C, and 2 hours at 150°C. The dried support was added to the reaction flask under an inert atmosphere with the desired metal halide, 6 grams, (bismuth chloride or zirconium tetrachloride from Aldrich, Milwaukee, WI, or aluminum chloride from Vanchlor Chemical, Inc., Lockport, NY). Toluene, 100 ml, was added via syringe to the solids. The catalyst slurry was stirred at ambient temperature for one hour and the solvent removed under vacuum, 2-5 mm Hg, maintaining the temperature near 20°C. Drying the flowable solid continued under vacuum at ambient temperature for 3 hours.
POLYMERIZATION
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, a thermometer, and a dropping addition funnel. The flask was charged with 30-50 grams of toluene (reagent grade, Aldrich Milwaukee, W1) and 0.011 moles of the metal chloride on the catalyst support as prepared above.
The catalyst slurry was heated to 50°C with stirnng.
Piperylene concentrate (Naphtha Petroleum 3 "Piperylenes", Lyondell Petrochemical Company, Houston, TX)) 100 grams, was added to the nitrogen purged reaction flask via the dropping addition funnel over 1 S minutes. Immediately prior to use, the monomers and solvent were dried as follows, the solvent was dried over 4 angstrom molecular sieves and the piperylene concentrate was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams of alumina to 1 milliliter of monomer).
The reaction solution was stirred at 50°C for a total reaction time of two hours.
Catalyst solids were removed from the reaction solution via filtration. The reaction solutions were quenched with 4 milliliters of NH40H in 100 milliliters of water and the water removed using a separatory funnel. After quenching, the resin solution was separated from any catalyst salt residues formed during quenching by vacuum filtration at room temperature.
The resin oil was then placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube and a thermometer, and attached to a condenser and a receiving flask. The resin oil was heated to 23 $ °C
with a nitrogen purge followed by a steam purge at 23$-24$°C to remove light oil products.
The steam purge was $ continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 23$°C to remove water ftom the remaining resin.
The resins produced have the properties listed in Table 8.
Example Catalyst Yield Softening Molecular Point Weight (R&B) Mn Mw Mz 40 BiCI,/Si0211 - 1290 1900 6300 %
41 ZnCl2/SiOz37/~ 42C 1780 2990 $340 1$ 42 FeCl3/Si027% - 9$0 2360 10800 43 A1C13/SiOZ41 $4C 990 1490 2410 %
44 ZrCl4/Si02$$/> 60C 1310 2370 46$0 COMPARATIVE EXAMPLE 4$
This comparative example illustrates that the silica used as a support for the metal halide catalysts is not an effective catalyst for C$ hydrocarbon resin synthesis.
POLYMERIZATION
A $00 milliliter three neck flask was equipped with an overhead stirrer, reflux 2$ condenser, gas inlet and outlet ports, a thermometer, and a dropping addition funnel. The flask was charged with 60.0 grams of toluene (reagent grade, Aldrich, Milwaukee, WIl and 14.0 grams silica ("EP12" grade, Crosfield Catalysts, Warrington England).
Prior to use, the solvent was dried over 4 angstrom molecular sieves. The catalyst slurry was heated to $0°C with stirnng.
Piperylene concentrate (Naphtha Petroleum 3 "Piperylenes", Lyondell Petrochemical Company, Houston, TX), 140 grams, was added to the nitrogen purged flask via the dropping addition funnel over 1$ minutes. Prior to use, the piperylene concentrate was dried _3g_ by passing through a column of activated alumina (Fischer 8-I6 mesh, 0.3 grams of alumina to I milliliter of monomer). The reaction solution was stirred at 50°C
for a total reaction time of one hour.
After completion of the reaction time, the resulting resin solution was separated from the silica by vacuum filtration at room temperature. The volatile materials were removed under reduced pressure at 50°C, no product remained.
These examples serve to illustrate the reuse of a ZrCl4 supported on silica as a catalyst for the polymerization of piperylene concentrate, a CS monomer feed.
CATALYST PREPARATION
The silica support material ("EP12" silica from Crosfield Catalysts, Warrington, England) was dried under vacuum, 2-5 mm Hg, using the following thermal cycle, 0.5 hours at room temperature, 1 hour at 35-40°C, 1.5 hours at 100°C, and 2 hours at 150°C. The 1 S dried support was added to the reaction flask under an inert atmosphere with zirconium tetrachloride (Aldrich, Milwaukee, WI). Loadings for the 10% catalyst were 3 grams ZrCl4 and 27 grams silica and for the 5% catalyst were 3 grams ZrCl4 and 57 grams silica.
Toluene, 100 ml, which had been dried over 4 angstrom molecular sieves, was added via syringe to the solids. The catalyst slurry was stirred at ambient temperature for one hour and the solvent removed under vacuum, 2-S mm Hg, maintaining the temperature near 20°C.
Drying the flowable solid continued under vacuum at ambient temperature for 3 hours.
POLYMERIZATION
A S00 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, a thermometer, and a dropping addition funnel. The flask was charged with 70 grams toluene (reagent grade, Aldrich Milwaukee, WI) and catalyst as follows. Prior to use, the solvent was dried over 4 angstrom molecular sieves.
For the 10% catalyst, 25.6 grams supported catalyst prepared as described above was added.
For the 5% catalyst, 51.2 grams supported catalyst prepared as described above was added.
Thus, in each case, 2.56 grams ZrCl4, 0.011 moles of the metal chloride was added to the solution. The catalyst slurry was heated to SO°C with stirring.
Piperylene concentrate (Naphtha Petroleum 3 "Piperylenes", Lyondell Petrochemical Company, Houston, TX), 100 grams, was added to the nitrogen purged reaction flask via the dropping ftumel over 15 minutes. Prior to use, the piperylene concentrate was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer). The reaction solution was stirred at 50°C for a total reaction time of two hours.
For the recycle examples, the catalyst was allowed to settle and the reaction solution removed from the flask via syringe. The catalyst was washed with 100 milliliters of dry toluene which was also removed from the catalyst via syringe. Additional solvent and monomer was added to the catalyst as described above.
For all of the examples, after completion of the reaction time, catalyst solids were removed from the reaction solution via filtration. The reaction solutions were then quenched with 4 milliiiters of NH40H in 100 milliliters of water and the water removed using a separatory funnel. The resin solution was then separated from any catalyst salt residues formed during quenching by vacuum filtration at room temperature.
The resin oil was then placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube, thermometer, and attached to a condenser and receiving flask. The resin oil was heated to 235°C with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products. The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The resins produced have the properties listed in Table 9.
Example Catalyst Yield Softening Molecular Weight Point (R&B) Mn Mw Mz 46 10% ZrCl4/Si0243% 63C 1890 3830 8490 47 10% ZrCl4/Si0247% 56C 1940 4020 8200 recycle 48 5% Zl'Cl4/SlOz35% 57C 1450 2910 6860 49 S% ZrCl4/Si0259% 49C 1440 3170 7460 recycle These examples illustrate the use of a supported aluminum trichloride catalyst on alumina for the polymerization of piperylene concentrate, a CS monomer feed.
POLYMERIZATION
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, a thermometer, and a dropping addition funnel. The flask was charged with 40 grams toluene (reagent grade, Aldrich Milwaukee, WI) and a solid supported aluminum trichloride catalyst, "CAT-59" catalyst (UOP, Des Plains, IL) as outlined below.
Prior to use, the solvent was dried over 4 angstrom molecular sieves. Also prior to use, the catalyst was crushed to a powder. All catalyst handling was performed in a nitrogen purged atmosphere. The catalyst slurry was heated to 50°C with stirring.
Piperylene concentrate (Naphtha Petroleum 3 "Piperylenes", Lyondell Petrochemical Company, Houston, TX), 100 grams, was added to the nitrogen purged reaction flask via the dropping addition funnel over 15 minutes. Immediately prior to use, the pipcrylene concentrate was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer). The reaction solution was stirred at _SO°C for a total reaction time of one hour.
Upon completion of the reaction time, the catalyst solids were removed from the reaction solution via filtration. The reaction solutions were then quenched with 4 milliliters of NH40H in 100 milliliters of water and the water removed using a separatory funnel.
After quenching, the reaction solution was then separated from any catalyst salt residues formed by vacuum filtration at room temperature.
The resulting resin solution was then washed to neutral pH with water and dried over MgS04 (reagent grade, Aldrich, Milwaukee, WI) The resin oil was then placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube, thermometer, and attached to a condenser and receiving flask. The resin oil was heated to 235°C with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products. The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The resins produced have the properties listed in Table 10.
Ex. Catalyst Yield SofteningMolecular Weight Point (R&B) Mn Mw Mz 50 27 wt% "CAT-59" 50% 62C 1510 2900 5950 on monomer 51 13.5 wt% "CAT-59"27% 62C 1640 3320 6980 on monomer These examples demonstrate the use of a synthetic supported aluminum trichloride as a catalyst for the polymerization of piperylene concentrate, a CS monomer feed.
CATALYST PREPARATION
Aluminum chloride (- 40 mesh, Vanchlor Co., Inc., Lockport, NY) 7.5 grams (O.U6 mol) and the support material, 30 grams "EP12" silica (Crosficld Catalysts) Warrington, England), were combined with 180 milliliters of toluene dried over 4 angstrom molecular sieves (reagent grade, Aldrich, Milwaukee, WI). The support material was dried prior to contacting with the aluminum trichloride solution for 2 hours at 40°C, 1 hour at 100°C, and 2 hours at I50°C all under vacuum. The aluminum trichloride solution was added to the dried support material and the resulting slurry was stirred at room temperature for one hour.
'The solvent was removed under vacuum at 2-5 mm Hg while maintaining the temperature near 25-30°C to obtain a flowable powder. The catalyst was stored and handled under an inert atmosphere prior to use.
POLYMERIZATION
Resins were prepared by the procedures outlined for Examples 50 and 5 I above.
The resins produced have the properties listed in Table 11.
Example Catalyst Yield SofteningMolecular Weight P
i o nt (R&B) Mn Mw Mz 52 7.5 wt% A1C13/SiOz21% 54C 960 1330 2010 on monomer 53 3.75 wt% 26% 47C 1030 1540 2610 AlCl3/Si02 on monomer These examples illustrate the use of zinc chloride on a variety of support materials as solid acid catalysts for the preparation of hydrocarbon resins from C9 unsaturated aromatic hydrocarbon feed stocks.
The supported zinc chloride catalysts were prepared by dissolving 27.3 grams ZnCI, (Aldrich Milwaukee, WI) in 300 grams of methanol (reagent grade, Aldrich, Milwaukee, WI). One hundred grams of support was added to the methanol solution and stirred as a 1 S slurry for 30 minutes. The support materials used were "F-22" and "F-6"
clays (Engelhard Corporation, Iselin, NJ), "K 10" clay (Sud Chemie/Llnited Catalyst Inc., Louisville, KY), and "EP12" silica (Crosfield Catalysts, Warrington, England). The methanol was evaporated from the catalysts on a rotary evaporator under reduced pressure.
The catalysts were calcined at 150°C for 2 hours under a nitrogen purge prior to use.
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, thermometer, and a dropping addition funnel. The flask was charged with 50 grams of toluene (reagent grade, Aldrich Milwaukee, WI) and 1 S
wt°/> of the supported ZnCl2 catalysts described above.
The C9 monomer feed, 100 grams of "LRO-90" (from Lyondell Petrochemicals, Houston, TX), was added to the flask via the dropping addition funnel.
Immediately prior to use, the monomers and solvent were dried as follows: the C9 monomer feed was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams of alumina to 1 milliliter of monomer). Also immediately prior to use, the toluene was dried over 3 angstrom molecular sieves prior to use.
The reaction solution was heated to a 50°C reaction temperature. The monomer was added to the reaction flask from the dropping addition funnel at a rate to maintain the desired reaction temperature with external cooling. Monomer addition time was approximately 1 S
minutes. The reaction solution was stirred at the desired reaction temperature for a total reaction time of 2 hours.
After completion of the reaction time, the resin solution was vacuum filtered from the acid treated clay catalyst at room temperature. The reaction flask and catalyst filter cake were rinsed with approximately 100 milliliters of toluene.
After catalyst filtration, the solvent was removed from the resin solution at 100°C
at 2-5 mm Hg. Also, the resin oil was placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube and a thermometer, and attached to a condenser with a receiving flask. The resin oil was heated to 23S°C
with a nitrogen purge followed by a steam purge at 23S-24S°C to remove light oil products.
The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensatc or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
1 S The resins produced have the properties listed in Table 12. Examples S4-S7 are in accordance with the present invention, whereas Comparison Example 58 is for comparison purposes.
Example Catalyst Yield Softening ~ Mo lecular Point Weight (R&B) Mn Mw Mz 54 ZnCI,/F-2229% 121 C 680 96n 1390 SS ZnCh/K 39% 101C 540 800 1230 S6 ZnCI,/EP1238% 113C 590 8S0 2590 S7 ZnCI,/F-6 40% 124C 690 960 1410 S8 ZnCl2 0% - - - -The following examples illustrate the effect on C9 resin properties produced using a supported ZnCl2 catalyst on silica at various reaction temperatures and catalyst loadings.
CATALYST PREPARATION
Zinc chloride {98% Aldrich, Milwaukee, WI), S.0 grams (0.037 mol), was dissolved in 50 milliliters of methanol (reagent grade, Aldrich, Milwaukee, WI). The support material, 13.5 grams, ("EP12" silica from Crosfield Catalysts, Warnngton, England which had been calcined at 1 SO°C under vacuum to remove excess water for the purpose of obtaining an accurate weight of the support) was added to the methanol solution. The slurry was stirred at room temperature for 30 minutes. The solvent was removed on a rotary evaporator at 2-5 mm Hg with mild heating to obtain a flowable powder. The catalyst was calcined at 150°C
under a dry nitrogen purge for 2 hours prior to use.
POLYMERIZATION
A S00 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, thermometer, and a dropping addition funnel. The flask was charged with 50 grams of toluene (reagent grade, Aldrich Milwaukee, W1) and a supported ZnClz on Si02 prepared as described about. Prior to use, the toluene was dried over 3 angstrom molecular sieves. The catalyst level for each reaction is described in Table 13 below.
The C9 monomer feed, 100 grams ("LRO-90" from Lyondell Petrochemicals, Nouston, TX) was added to the dropping addition funnel. Immediately prior to use, the C9 monomer feed was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer). The reaction solution was heated to the reaction temperature described in Table 13 below. The monomer solution was added to the reaction flask from the dropping addition funnel at a rate to maintain the desired reaction temperature with external cooling. Monomer addition time was approximately 1 ~
minutes.
The reaction solution was stirred at the desired reaction temperature for a total reaction time of 2 hours.
Upon completion of the reaction time, the resin solution was vacuum filtered from the catalyst at room temperature. The reaction flask and catalyst filter cake were rinsed with approximately 100 milliliters of toluene.
After filtration, the resin oil was placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube and thermometer and attached to a condenser with a receiving flask. The resin oil was heated to 235°C
with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products.
The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The resins produced have the properties listed in Table 13.
Ex. Catalyst ReactionYieldSoftening M olecularWeight Loading Temp. Point (R&B) Mn Mw Mz PD
59 S wt% 100C 41% 102C 530 750 1440 1.4 60 20 wt% 60C 38% 134C 790 1220 4410 1.6 61 5 wt% 20C 7% 145C 1010 1750 3950 1.8 62 12.5 wt% 100 40% I 07 C 620 810 2040 1.3 C
63 12.5 wt% 60C 37% 132C 880 1210 2100 1.4 64 20 wt% 100C 42% 105C 620 810 2730 1.3 65 12.5 wt% 20C 1% - 790 2450 8260 3.1 66 5 wt% 60C 18% 139C 910 1230 2210 1.4 67 20 wt% 20C I% - 960 2890 8040 ?.8 68 12.5 wt% 60C 25% 122C 790 1070 1950 1.4 69 12.5 wt% 60C 17% 123C 740 960 1320 1.3 70 S wt% 136C 37% 88C 480 600 790 1.3 7l 12.5 wt% 136C 41% 62C 390 470 580 1.2 72 20 wt% 120C 35% 80C 490 580 690 1.2 I
The following examples illustrate the effect on C9 resin properties produced using a supported ZnClz catalyst on silica at various reaction temperatures and catalyst loadings.
CATALYST PREPARATION
Zinc chloride (98% Aldrich, Milwaukee, WI), 20.0 grams (0.1 S mol), was dissolved in 300 milliliters of methanol (reagent grade, Aldrich, Milwaukee, WI). The support material, 80 grams, ("EP 12" silica from Crosfield Catalysts, Warrington, England) was added to the methanol solution. The slurry was stirs ed at room temperature for 30 minutes.
The solvent was removed on a rotary evaporator at 2-5 mm Hg with mild heating to obtain a flowable powder. The catalyst was calcined for 2 hours at 40°C, 1 hour at 100°C, and 2 hours at 150°C all under vacuum prior to use.
POLYMERIZATION
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, thermometer, and a dropping addition funnel. The flask was charged with 100 grams of toluene (reagent grade, Aldrich Milwaukee, WI) and a supported ZnClz on SiOz prepared as described above. Prior to use, the toluene was dried over 3 angstrom molecular sieves. The catalyst level for each reaction is described in Table 14 below.
The C9 monomer feed, 100 grams ("LRO-90" from Lyondell Petrochemicals, Houston, TX) was added to the dropping addition funnel. Immediately prior to use, the C9 monomer feed was dried by passing through a column of activated alumina (Fischcr 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer). The reaction solution was heated to the reaction temperature described in Table 14 below. The monomer solution was added to the reaction flask from the dropping addition funnel at a rate to maintain the desired reaction temperature with external cooling. Monomer addition time was approximately 15 minutes.
The reaction solution was stirred at the desired reaction temperature for a total reaction time of 2 hours.
Upon completion of the reaction time, the resin solution was vacuum filtered from the catalyst at room temperature. The reaction flask and catalyst filter cake were rinsed with approximately 100 milliliters of toluene.
After filtration, the resin oil was placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube and thermometer and attached to a condenser with a receiving flask. The resin oil was heated to 235°C
with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products.
The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The resulting resins had the properties listed in Table 14.
WO 98130587 PCT/iJS98/00012 Ex. CatalystReactionYield SofteningMolecular I Weight LoadingTemp. Point (R&B) Mn Mw Mz PD
73 10 wt% 50C 37% 134C 830 1280 2040 1.5 74 5 wt% 50C 21% 144C 890 1380 2260 1.6 75 10 wt% 100C 28% 126C 690 920 1320 1.3 76 10 wt% 50C 35% 141 C 850 1230 1890 1.5 While the invention has been described in connection with certain preferred embodiments so that aspects thereof may be more fully understood and appreciated, it is not intended to limit the invention to these particular embodiments. On the contrary, it is intended to cover all alternatives, modifications and equivalents as may be included within the scope of the invention as defined by the appended claims.
U.S. Patent No. 5,561,095 to CHEN et al., the disclosure of which is herein incorporated by reference in its entirety, discloses a supported Lewis acid catalyst for polymerization of olefins, including C3-C23 alpha-olefins, to obtain polymers having number average molecular weights (Mn) ranging from about 300 to 300,000.
Exemplary Lewis acid supports include silica, silica-alumina, zeolites, and clays.
Example 1 of CHEN
et al. discloses that a Lewis acid supported on silica is heated under vacuum.
U.S. Patent No. 3,799,913 to WHEELER et al., the disclosure of which is herein incorporated by reference in its entirety, discloses Friedel-Crafts catalysts for polymerization of polymerizable constituents, including alpha-methyl styrene, indene, vinyl toluene and styrene, to obtain polymers having a number average molecular weight (Mn) ranging from about 350 to 1200. Zinc chloride is disclosed as one of the Friedel-Crafts catalysts.
U.S. Patent No. 3,652,707 to SAINES, the disclosure of which is herein incorporated by reference in its entirety, discloses Friedel-Crafts metal halide catalysts for polymerization of olefin hydrocarbons, including pentene, styrene and methylstyrene, to obtain polymers having a molecular weight of from about 700 to about 2500. Zinc chloride is disclosed as one of the Friedel-Crafts metal halide catalysts.
PENG et al., "Electrophilic Polymerization of 1,3-Pentadiene Initiated by Aluminum Triflate", Eur. Pol~nn. (T, Vol. 30, No. 1, pp. 69-77 ( 1994), the disclosure of which is herein incorporated by reference in its entirety, discloses aluminum triflate for polymerization of piperylene to obtain polymers having varying number average molecular weights.
European Patent Application 0 352 856 A 1, the disclosure of which is herein incorporated by reference in its entirety, discloses use of aluminum triflate, cerium triflate, e.g., for oligomerization of C3 to C6 olefins to obtain oligomers having 6 to 24 carbon atoms.
GANDINI et al., "The Heterogeneous Cationic Polymerization of Aromatic Monomers by Aluminum Triflate", Polymer Pr~rints, American Chemical Society) pp. 359-360 ( 1996), the disclosure of which is herein incorporated by reference in its entirety, discloses use of aluminum triflate for polymerization of C9 related monomers to obtain a polymer having a number average molecular weight (Mn) around 3000. This document also discloses that aluminum triflate could be useful for the direct "resinification" of mixtures of aromatic monomers and solvents arising from specific petroleum cuts.
Other documents, the disclosures of which are herein incorporated by reference in their entireties, which generally disclose the use of solid acid catalysts to polymerize monomers for the preparation of resins include U.S. Patent No. 4,068,062 to LEPERT, U.S.
Patent No. 4,130,701 to LEPERT, U.S. Patent No. 4,245,075 to LEPERT, and U.S.
Patent No. 4,824,921 to LUVINH.
_5_ SUMMARY OF THE INVENTION
The present invention involves the preparation of hydrocarbon resins. More particularly, the present invention involves the use of at least one of supported metal halides and metal halide solid acid catalysts to polymerize a feed of hydrocarbon monomers.
Hydrocarbon resins are prepared from at least one of pure monomer, CS
monomers, and C9 monomers using relatively environmentally benign, recyclable, at least one of supported metal halides and metal halide solid acid catalysts in which freely-associated water may have been removed. In the present invention, hydrocarbon resins are prepared by a cationic polymerization (e.g., Friedel-Crafts) wherein a feed stream containing at least one of pure monomer, CS monomers, and C9 monomers is preferably treated with at least one of supported metal halides and metal halide solid acid catalyst.
Before use, the solid acid catalysts and/or supports may be treated to remove freely-associated water associated with the solids to maximize catalyst acidity and activity toward the polymerization. For example, prior to use, the catalyst and/or support may be calcined for a sufficient time to remove freely-associated water and/or the catalyst and/or support can be exposed to reduced atmospheric pressure. For instance, the calcining may be at a temperature up to about 700°C, preferably at a temperature between about 50°C and 500°C.
The calcining may be under reduced atmospheric pressure for up to about 8 hours, preferably between about 1 hour to 4 hours.
2p In accordance with one aspect, the present invention is directed to a process for making a hydrocarbon resin, including polymerizing a feed stream comprising at least one member selected from the group consisting of pure monomer, CS monomers, and C9 monomers in the presence of a supported metal halide solid acid catalyst to produce a hydrocarbon resin, wherein substantially all freely-associated water has been removed from the supported metal halide solid acid catalyst.
In accordance with another aspect, the present invention is directed to a process for making a hydrocarbon resin, including polymerizing a feed stream comprising at least one member selected from the group consisting of pure monomer, CS monomers, and C9 monomers in the presence of ZrCl4 to produce a hydrocarbon resin.
The supported metal halide solid acid catalyst may comprise Lewis acid on clay, silica, silica-alumina, mesoporous silica, mesoporous silica-alumina, ion exchange resin, zeolite. The Lewis acid may include at least one member selected from the group consisting _6_ of ZnClz, A1C1~, AlBr3, BFj, BC13, FeCl3, SnCl4, TiCl4, ZrCl4, HfCl4, BiCl3, and lanthanide halides.
The clay supports may include naturally occurring clay mineral such as at least one member selected from the group consisting of kaolinite, bentonite, attapulgite, montmorillonite, clarit, Fuller's earth, hectorite, and beidellite; synthetic clay such as at least one member selected from the group consisting of saponite and hydrotalcite;
montmorillonite clay treated with at least one member selected from the group consisting of sulfuric acid and hydrochloric acid; and modified clay including at least one member selected from the group consisting of aluminum oxide pillared clay, cerium modified alumina pillared clay, and metal oxide pillared clay.
The zeolite support may include at least one member selected from the group consisting of zeolite Y, zeolite Vii, MFI, MEL, NaX, NaY, faujasite, and mordenite.
In another feature of the present invention, the supported metal halide solid acid catalyst includes polymer grafted aluminum halide.
1n accordance with another feature of the invention, the feed stream includes between about 20 wt'% and 80 wt% monomers and about 80 wt% to 20 wt% of solvent.
Preferably, the feed stream includes about 30 wt% to 70 wt% monomers and about 70 wt'ro to 30 wrt%
of solvent. More preferably, the feed stream includes about SO wt% to 70 wt°,~o monomers and about 50 wt'% to 30 wt% of solvent. The solvent may include an aromatic solvent. The aromatic solvent may include at least one member selected from the group consisting of toluene, xylenes, and aromatic petroleum solvents. The solvent may include an aliphatic solvent. The invention may further include recycling the solvent.
In accordance with a feature of the invention, the feed stream includes at least CS
monomers. The feed stream may include at least CS monomers, wherein cyclopentadiene and methylcyclopentadienc components are removed from the feed stream by heating at a temperature between about 100°C and 160°C and fractionating by distillation. The CS
monomers may include at least one member selected from the group consisting of isobutylene, 2-methyl-2-butene, 1-pentene, 2-methyl-1-pentene, 2-methyl-2-pentene, 2-pentene, cyclopentene, cyclohexene, 1,3-pentadiene, 1,4-pentadiene, isoprene, 1,3-hexadiene, 1,4-hexadiene, cyclopentadiene, and dicyclopentadiene. The feed stream may include at least CS monomers, wherein the feed stream includes at least about 70 wt% of polymerizable monomers with at least about 50 wt% 1,3-pentadiene. The feed stream may contain low levels of isoprene, generally contains a portion of 2-methyl-2-butene, and may contain one or more cyclodiolefins.
The feed stream may include at least CS monomers, wherein the feed stream further includes up to about 40 wt% of chain transfer agent, preferably up to about 20 wt% of chain transfer agent. The chain transfer agent may include at least one member selected fi~om the group consisting of C4 olefins, CS olefins, dimers of C4 olefins, and dimers of CS olefins.
The chain transfer agent may include at least one member selected from the group consisting of isobutylene, 2-methyl-1-butene, 2-methyl-2-butene, dimers thereof, and oligomers thereo f.
In accordance with a feature of the invention, the feed stream includes about 30 wt%
to 95 wt% of CS monomers and about 70 wt% to S wt% of a cofeed including at (cast one member selected from the group consisting of pure monomer, C9 monomers, and terpenes.
Preferably, the feed stream includes about 50 wt% to 85 wt% of CS monomers and about 50 wt% to 15 wt% of a cofeed including at least one member selected from the group consisting of pure monomer, C9 monomers, and tcrpencs.
In accordance with another feature of the invention, the feed stream includes at least C9 monomers. The C9 monomers may include at least one member selected from the group consisting of styrene, vinyl toluene, indene, dicyclopentadiene, and alkylated derivatives thereof. The C9 monomers may include at least about 20 wt% polymerizable unsaturated hydrocarbons. The C9 monomers may include about 30 wt°a to 75 wt'%
polymerizable unsawrated hydrocarbons. The C9 monomers may include about 35 wt°r~ to 7O wt'~a polymerizable unsaturated hydrocarbons.
In accordance with a feature of the invention, the feed stream includes about 3U wt'%
to 95 wt% of the C9 monomers and about 70 wt% to 5 wt% of a cofeed including at least one member selected from the group consisting of pure monomer, CS monomers, and terpenes. Preferably, the feed stream includes about 50 wt% to 85 wt°/<. of the C9 monomers and about 50 wt% to 15 wt% of a cofeed including at least one member selected from the group consisting of pure monomer, CS monomers, and terpenes.
Many of the supported metal halides and metal halide solid acid catalysts function -g_ most effectively in the presence of a controlled amount of water in the monomer feed stream. In accordance with this feature of the invention, the feed stream should include less than about 500 ppm water, preferably less than about 200 ppm water, more preferably less than about 100 ppm water, and most preferably less than about 50 ppm water.
S In accordance with yet another feature of the invention, the feed stream is contacted with about 0.5 wt% to 30 wt%, preferably about 1 wt% to 20 wt%, more preferably about 3 wt% to 15 wt%, and most preferably 0.5 wt% to 5 wt% of the catalyst based on monomer weight in a batch reactor.
In accordance with yet another feature of the invention, the catalyst is added to the feed stream.
In accordance with another feature of the invention, the feed stream is added to a slurry of the catalyst in solvent. The feed stream may be passed over a fixed bed of the catalyst.
In accordance with yet another feature of the invention, the feed stream is cofed with 1 S a slurry of the catalyst into a reactor.
In accordance with a feature of the invention, the polymerization is carried out as a continuous process or as a batch process. A reaction time in the batch process is about 30 minutes to 8 hours, preferably about 1 hour to 4 hours at reaction temperature.
In accordance with a feature of the invention, the feed stream is polymerized at a reaction temperature between about -50°C and 1 SO°C, preferably between about -20°C and 100°C, and more preferably between about 0°C and 70°C.
In accordance with another feature of the invention, the polymerization is stopped by removing the catalyst from the hydrocarbon resin. The catalyst may be removed from the hydrocarbon resin by filtration. The hydrocarbon resin may be removed from a fixed bed reactor which includes the catalyst.
In accordance with a feature of the invention, the hydrocarbon resin is stripped to remove unreacted monomers, solvents, and low molecular weight oligomers. The unreacted monomers, solvents, and low molecular weight oligomers may be recycled.
In accordance with a feature of the invention, the hydrocarbon resin is separated from a hydrocarbon resin solution.
In accordance with a feature of the invention, the hydrocarbon resin has a softening point as measured by ASTM-E28 "Standard Test Method for Softening Point by Ring and Ball Apparatus", between about 5°C and 170°C. The feed stream may include at least CS
monomers, wherein the softening point of the resulting hydrocarbon resin is between about 50°C and 150°C. The feed stream may include at least C9 monomers, wherein the softening point of the resulting hydrocarbon resin is between about 70°C and 160°C.
In accordance with a feature of the invention, the feed stream includes at least pure monomer, wherein the resulting hydrocarbon resin has a number average molecular weight (Mn) ranging from about 400 to 2000, a weight average molecular weight (Mw) ranging from about S00 to 5000, a Z average molecular weight (Mz) ranging from about 500 to 10,000, and a polydispersity (PD) as measured by Mw/Mn between about 1.2 and 3.5, where Mn, Mw, and Mz are determined by size exclusion chromatography (SEC).
In accordance with a feature of the invention, the feed stream includes at least CS
monomers, wherein the resulting hydrocarbon resin has a number average molecular weight (Mn) of about 400 to 2000, a weight average molecular weight (Mw) of about 500 to 3500, a Z average molecular weight (Mz) of about 700 to 15,000, and a polydispcrsity (PD) as measured by Mw/Mn between about 1.2 and 5, where Mn, Mw, and Mz are determined by size exclusion chromatography (SEC).
In accordance with another feature of the invention, the feed stream includes at least C9 monomers, wherein the resulting hydrocarbon resin has a number average molecular weight (Mn) of about 400 to 1200, a weight average molecular weight (Mw) of about 500 to 2000, a Z average molecular weight (Mz) of about 700 to 6000, and a polydispcrsity (PD) as measured by Mw/Mn between about 1.2 and 3.5, preferably 1.2 and 2.5, where Mn, Mw, and Mz are determined by size exclusion chromatography (SEC).
In accordance with another feature of the invention, the hydrocarbon resin is hydrogenated.
BRIEF DESCRIPTION OF THE DRAWINGS
The present invention is further described in the detailed description which follows, in reference to the noted plurality of non-limiting drawings, and wherein:
Figures 1-4 depict contour plots generated from regression analysis of various pure monomer resin polymerizations.
DETAILED DESCRIPTION OF THE INVENTION
The particulars shown herein are by way of example and for purposes of illustrative discussion of the various embodiments of the present invention only and are presented in the cause of providing what is believed to be the most useful and readily understood description of the principles and conceptual aspects of the invention. In this regard, no attempt is made to show details of the invention in more detail than is necessary for a fundamental understanding of the invention, the description making apparent to those skilled in the art how the several forms of the invention may be embodied in practice.
All percent measurements in this application, unless otherwise stated, are measured by weight based upon 100% of a given sample weight. Thus, for example, 30%
represents 30 weight parts out of every 100 weight parts of the sample.
Unless otherwise stated, a reference to a compound or component includes the compound or component by itself, as well as in combination with other compounds and components, such as mixtures of compounds.
Before further discussion, a definition of the following terms will aid in the understanding of the present invention.
SOLID ACID: a solid which changes the color of a basic Hammett indicator with apK~<0.
METAL HALIDE SOLID ACID: a solid acid comprising metal covalently bonded to halide.
SUPPORTED METAL HALIDE SOLID ACID: a solid catalyst comprising a support) e.g., silica, silica-alumina, clay, zcolite, associated with a compound comprising metal covalently bonded to halide.
HYDROCARBON RESIN: a low molecular weight (i.e., a number average molecular weight of about 200 to less than about 3000 as determined by size exclusion chromatography (SEC)) thermoplastic polymer synthesized via thermal or catalytic polymerization of cracked petroleum distillates, terpenes, coal tar fractions, or pure olefmic monomers, wherein one of the monomers is at least a CS or higher.
PURE MONOMER: a composition comprising synthetically generated or highly purified monomer species, e.g., styrene from ethyl benzene or alpha methyl styrene from cumene.
WO 98/30587 PCT/US98l00012 PURE MONOMER FEED STREAM: a composition comprising any number of pure monomer species.
CS MONOMERS: a composition derived from petroleum processing, e.g., cracking, containing unsaturated hydrocarbons comprising CS and/or C6 olefin species boiling in the range from about 20°C to 100°C at atmospheric pressure.
C9 MONOMERS: a composition derived from petroleum processing, e.g., cracking, containing unsaturated aromatic C8, C9, and/or C10 olefin species with a boiling range of about 100°C to 300°C at atmospheric pressure.
FREELY-ASSOCIATED WATER: water associated with a solid acid catalyst or support where the water is chemisorbed and/or physisorbed.
As a general overview of the present invention, hydrocarbon resins are produced by using at least one of supported metal halides and metal halide solid acids as catalysts for the cationic polymerization of a feed stream containing at least one of pure monomer (e.g..
styrene based monomers), CS monomers, and C9 monomers. Resins with softening points (Ring and Ball) preferably in the range of about 5°C to 170°C, more preferably about 30°C
to 1 SO°C, can be prepared. These catalysts offer advantages over the traditional unsupported Lewis acid polymerization catalysts since the acid sites are an integral part of the solid or a Lewis acid is supported on a solid. Further, for the supported Lewis acids, the Lewis acid is supported on a solid and therefore can be removed from the reaction solution.
Looking at the present invention in more detail, hydrocarbon resins are prepared through a polymerization reaction wherein a feed stream containing at least one of pure monomer, CS monomers) and C9 monomers are contacted with a at least one of a supported metal halides and metal halide solid acid catalyst. Supported metal halides and metal halide solid acid catalysts which are useful in the current invention include, but are not limited to, the following.
Lewis acids on clays The Lewis acids on clays including, for example ZnCl2 AlCl3 AlBr3 FeCl3 SnCl4 TiCl4 ZrCl4 HfCl4 BiCl3 Lanthanide halides The clays supporting the Lewis acids including, for example Naturally occurring clay minerals, for example Kaolinite Bentonite Attapulgite Montmorillonite Clarit Fuller's Earth Hectorite Beidellite Synthetic clays, for example Saponite Hydrotalcite Montmorillonite clays treated with sulfuric or hydrochloric acid Modified clays (i.e., clays modified by backbone element replacement), e.g.
Aluminum oxide pillared clays Cerium modified alumina pillared clays Metal oxide pillared clays Lewis acids on silica or silica-alumina, for example ZnClz AICI, AlBr3 FeCl3 SnCla TiCl4 ZrCI~
HfCl4 BCI
BiCl3 Lanthanide halides Lewis acids on mesoporous silica or silica-alumina, for example ZnCl2 AlBr3 FeCl3 SnCl4 TiCl4 ZrCl4 HfCl4 BiCl3 Lanthanide halides Lewis acids on ion exchange resins, for example ZnClz AlCl3 AlBr3 FeCI
SnCl4 TiCl4 ZrCl4 HfCI~
BiCl3 Lanthanide halides Lewis acids on natural or synthetic zeolites The Lewis acids on zeolites including, for example ZnCl2 A1C1;
AlBr3 BC1~
FeClz SnCl4 TiCl4 ZrCl4 HfCl4 BiCI, Lanthanide halides The zcolites supporting Lewis acids including, for example Zeolite Y
Zeolite (3 (i.e., BEA) MFI (e.g., "Zeolite Sacony Mobil-5" ("ZSM-5")) MEL (e.g., "Zeolite Sacony Mobil-11" ("ZSM-11")) NaX
NaY
Faujasite (i.e., FAU) Mordenite (i.e., MOR) Polymer grafted aluminum halides Solid Inorganic Acids ZrCl4 HfCl4 Lanthanide halides As mentioned previously, the above list of supported metal halides and metal halide solid acid catalysts is not intended to be an exhaustive list. In selecting other supported metal halides and metal halide solid acid catalysts which may be useful in the present invention, it is generally true that the supported metal halides and metal halide solid acid catalyst should be more acidic than about -3 on the Hammett scale.
Examples of the lanthanide halides mentioned in the above list include ScCI,, YC1,, LaCI;, YbCI,, CeCl3) PrCl3, NdCl3, NdBr;, SmCl3, EuCI,, GdCI~, TbCl3, DyCI~, HoCI,, HoBr~, ErCI,, TmCI~, and LuCl3.
1 S Concerning the zeolites, the names BEA, MFI, MEL, FAU, and MOR are the framework structure type IUPAC definitions of the listed species.
Examples of polymer grafted aluminum halides mentioned in the above list arc found in U.S. Patent No. 5,414,177 to CHUNG et al. and U.S. Patent No. 5,409,873 to CHUNG
et al., the disclosures of which are herein incorporated by reference in their entireties.
Before use) the solid acid catalysts and/or supports may be treated to remove Creeiy-associated water to maximize the catalyst acidity and activity toward the polymcriration.
The freely-associated water may be removed by various techniques, including thermal treatment, reduced pressure treatment, dry atmosphere treatment such as nitrogen or air, or a combination thereof While not wishing to be bound by theory, removing freely-associated water maximizes the acid strength of the Lewis acid catalyst and makes the polymerizations more reproducible.
The freely-associated water may be removed from the solid acid catalyst and/or support by calcining which generally means heating the metal halide solid acid and/or support to high temperature without fusing the catalyst. The metal halide solid acid and/or support may be calcined under an inert atmosphere, such as nitrogen or dry air, or under reduced pressure. The calcining is performed for preferably up to about 8 hours or more, more preferably about 1 hour to 4 hours, preferably at temperatures up to about 700°C, more preferably about 100°C to 400°C.
The freely-associated water removed from the metal halide solid acid catalyst and/or support may have been derived from water (physisorbed water) or hydroxyl groups (chemisorbed water) associated with the metal halide solid acid catalyst andlor support. By removal of substantially all freely-associated water is meant removing all or essentially all physisorbed water and removing at least a majority of chemisorbed water.
For the supported metal halide acid catalysts, the solid acid catalyst may consist essentially of a single type of a metal halide, e.g., a Lewis acid, on a single type of support.
However, the supported metal halide solid acid catalyst may involve any combination of a single type or plurality of types of a metal halide on a single type or plurality of types of supports.
Before the support and the metal halide are combined, the support may be calcined.
The importance of calcining the support before the support and metal halide are combined varies depending upon the metal halide. For instance, calcination is critical for supported A1C1,, AlBr3, BFI, TiCl4, HfCl4, FeCI~, and BCI;. Calcination is important for supported ZrCl4 and BiCI~. In contrast, supported FeCI~ and ZnCI, may be used with or without pre-1 S calcination of the support.
It is expected that by controlling the conditions under which the at least one of supported metal halides and metal halide solid acid catalyst is calcined, such as controlling the temperature or time under which the calcination step takes place, tailoring of the physical properties of the resultant resin, such as its softening point or its molecular weight, may be achieved.
Many of the supported metal halides and metal halide solid acid catalysts of the present invention are most effective in the presence of a controlled amount of water in the feed stream. For instance, the feed stream may include less than about 500 ppm water, preferably less than about 200 ppm water, more preferably less than about 100 ppm water, and most preferably less than about SO ppm water.
Pure monomer feed streams may contain relatively pure styrene-based monomers such as styrene, alpha-methyl styrene, beta-methyl styrene, 4-methyl styrene, and vinyl toluene fractions. The monomers can be used as pure components or as blends of two or more monomer feeds to give desired resin properties. Preferred blends include about 20 wt% to 90 wt% alpha-methyl styrene with about 80 wt% to 10 wt% of one or more comonomers, preferably styrene, vinyl toluene, 4-methyl styrene or blends of these components. In addition, other alkylated styrenes can be used as monomers in this invention such as t-butyl styrene or phenyl styrene. Feed streams can be dried, if desired, and preferably contain less than about 200 ppm water, more preferably less than about 100 ppm water, and most preferably less than about 50 ppm water.
In the case of CS resins, the petroleum feed streams contain unsaturated CS
andlor S C6 olefins and diolefins boiling in the range from about 20°C to 100°C, preferably about 30°C to 70°C. In some cases, cyclopentadiene and methylcyclopentadiene components are removed from the feed by heat soaking at temperatures preferably between about 100°C and 160°C, and fractionating by distillation. Monomers found in these feedstocks may include but are not limited to olefins such as isobutylene, 2-methyl-2-butene, I -pentene, 2-methyl-1-pentene, 2-methyl-2-pentene, as well as 2-pentene, cycloolefins such as cyclopentene, and cyclohexene, diolefins such as 1,3-pentadiene, 1,4-pentadiene, isoprene, 1,3-hexadienc, and 1,4-hexadiene, cyclodiolefins such as cyclopentadiene, dicyclopentadiene, and alkyl substituted derivatives and codimers of these cyclodiolefins. Commercial samples of this type of feed include, but are not limited to "Naphtha Petroleum 3 Pipcrylencs"
from Lyondell Petrochemical Company, Houston, TX, regular "Piperylcne Concentrate"
or "Super Piperylene Concentrate" both from Shell Nederland Chemie B.V., Hoogvilet, the Netherlands. The CS feed streams generally contain at least about 70 wt%
polymerizablc monomers with at least about SO wt% 1,3-pentadiene. The CS feed stream may contain low levels of isoprene, generally contains 2-methyl-2-butene, and may contain one or more cyclodiolefins.
Also concerning CS monomer feed streams, in addition to the reactive components, nonpolymerizable components in the feed may include saturated hydrocarbons which can be codistilled with the unsaturated components such as pentane, cyclopentane, or 2-mcthylpentane. This monomer feed can be copolymerized with C4 or CS olefins or dimers as chain transfer agents. Chain transfer agents may be added to obtain resins with lower and narrower molecular weight distributions than can be prepared from using monomers alone.
Chain transfer agents stop the propagation of a growing polymer chain by terminating the chain in a way which regenerates a polymer initiation site. Components which behave as chain transfer agents in these reactions include but are not limited to isobutylene, 2-methyl-1-butene, 2-methyl-2-butene or dimers or oligomers of these species. The chain transfer agent can be added to the reaction in pure form or diluted in a solvent. Feed streams can be dried if desired and preferably contain less than about 500 ppm water, more preferably less WO 98/30587 PCTlUS98/00012 than about 200 ppm water, and most preferably less than about SO ppm water.
In the case of C9 monomer resins, the feed streams contain unsaturated aromatic C8, C9, and/or CI O monomers with a boiling range of about 100°C to 300°C at atmospheric pressure. Aromatic C8-C 10 feed streams (also referred to as C9 feed streams) can be derived fiom steam cracking of petroleum distillates. Monomers found in these feed stocks may include but are not limited to styrene, vinyl toluene, indene, dicyclopentadiene, and alkylated derivatives of these components. Commercial samples of this type of feed include but are not limited to "LRO-90" from Lyondell Petrochemical Company, Houston, TX, "DSM C9 Resinfeed Classic" from DSM, Geleen, the Netherlands, "RO-60" and "RO-80"
from Dow Chemical Company of Midland, Michigan, and "Dow Resin Oil 60-L" from the Dow Chemical Company of Terneuzen, the Netherlands. The C9 feed stream generally contains at least about 20% by weight, preferably about 30% to 75% by weight, and most preferably about 35% to 70% by weight polymerizable unsaturated hydrocarbons.
The remainder is generally alkyl substituted aromatics which can be incorporated into the resins by alkyiation reactions. Feed streams can be dried if desired and preferably contain less than about 500 ppm water, more preferably less than about 200 ppm water, and most preferably less than about 50 ppm water.
The feed streams may be limited to pure monomer, CS monomers, or C9 monomers.
Alternatively, cofeed streams can be used in combination with main feed streams of pure monomer, CS monomers, or C9 monomers. Depending upon the main feed stream, pure monomer, CS monomers, C9 monomers, or even terpenes, and any combination thereof, may serve as a cofeed stream. Terpene feed stocks include but are not limited to d-limonene, alpha- and beta-pinene, as well as dipentene. Resins from blends of main feed streams with cofeed streams may be prepared in the range of about 30 wt% to 95 wt°/~ rnain feed with about 70 wt% to 5 wt% of a cofeed, preferably about SO-85 wt% main feed and about 50 wt% to 1 S wt% cofeed.
The polymerization feed stream preferably contains between about 20 wt% and 80 wt% monomers, more preferably about 30 wt% to 70 wt%, and most preferably about 40 wt% to 70 wt%. In the case of CS resins, the feed may contain up to about 40 wt% of a chain transfer agent, more preferably up to about 20 wt%, chain transfer agents as discussed above. The feed stream also contains about 80 wt% to 20 wt% of a solvent such as toluene, octane, higher boiling aromatic solvent, aliphatic solvent, or solvent blend.
-lg_ Regarding the solvents, for pure monomer polymerization, the preferred solvents are aromatic solvents. Typically toluene, xylenes, or light aromatic petroleum solvents such as "Aromatic 100" from Exxon Chemical Company, Houston, TX, "HiSol 10" from Ashland Chemical Incorporated, Columbus, OH, and "Cyclosol 53" from Shell Chemical Company, S Houston, TX can be used. These solvents can be used fresh or recycled from the process.
The solvents generally contain less than about 200 ppm water, preferably less than about 100 ppm water, and most preferably less than about 50 ppm water.
For C5 polymerization, the preferred solvents are aromatic solvents.
Generally, unreacted resin oil components are recycled through the process as solvent. In addition to the recycled solvents, toluene, xylenes, or aromatic petroleum solvents such as "Solvesso 100" from Exxon Chemical Company, Houston, TX and "Shellsol A" from Shell Chemical Company, Houston, TX can be used. These solvents can be used fresh or recycled from the process. The solvents generally contain less than about 500 ppm water, preferably less than about 200 ppm water, and most preferably less than about 50 ppm water.
For C9 polymerization, the preferred solvents are aromatic solvents.
Generally, unreacted resin oil components are recycled through the process as solvent. In addition to the recycled solvents, toluene, xylenes, or aromatic petroleum solvents such as "Solvesso 100" from Exxon Chemical Company, Houston, TX and "Shcllsol A" from Shell Chemical Company, Houston, TX can be used. These solvents can be used fresh or recycled from the process. The solvents generally contain less than about 200 ppm water, preferably less than about 100 ppm water, and most preferably less than about 50 ppm water.
Concerning the polymerization reaction conditions, a first important variable is the amount of at least one of supported metal halides and metal halide solid acid catalyst which is used. The at least one of supported metal halides and metal halide solid acids are preferably used at a level of about 0.1 wt% to 30 wt% based on the weight of the monomer.
For pure monomer resins, the at least one of supported metal halides and metal halide solid acid concentration is preferably about 0.1 to 15 wt%, more preferably about 0.5 wt% to 10 wt%, and most preferably about 0.5 wt% to 8 wt%. For C5 monomers, the at least one of supported metal halides and metal halide solid acid concentration is preferably about 0.5 wt% to 30 wt%, more preferably about 1 wt% to 20 wt%, and most preferably about 3 wt%
to 15 wt%. For C9 monomers, the at least one of supported metal halides and metal halide solid acid concentration is preferably about 0.5 wt% to 30 wt%, more preferably about 1 wt% to 20 wt%, and most preferably about 3 wt% to 15 wt%.
A second important variable in the reaction is the reaction sequence, i.e., the order and manner in which reactants are combined. In one reaction sequence, the catalyst can be added to a solution of the monomers incrementally while controlling the reaction temperature. Alternatively, in another reaction sequence, the monomer can be added incrementally to a slurry of the at least one of supported metal halides and metal halide solid acid catalyst in a solvent. For a set catalyst level and reaction temperature, substantially lower softening point resins are obtained when the monomer is added to a catalyst slurry.
As discussed in more detail in the following paragraphs, lower molecular weights and narrow polydispersity (PD), i.c., Mw/Mn, as measured by size exclusion chromatography, are obtained when the monomer is added to the catalyst solution compared with resins where the catalyst is added to the monomer.
The molecular weight averages of the resins were measured using size exclusion chromatography, SEC. The column set for the analysis consisted of four Waters I S "Ultrastyragel" columns of 500, 500, 1000, and 100 A pore size, in series, (Pan Nos. VVAT
010571, 010571, 010572, 010570 respectively) available from Waters Corporation, Milford, MA. The molecular weight calibration was calculated from the peak elution times of a standard set of narrow molecular weight distribution polystyrene polymers. The calibration set encompassed 18 standards ranging in peak molecular weight from I 62 to 43,900. The peak molecular weight of a narrow molecular weight standard is defined as equal to (MwMn)''' (ASTM test method D3536-76). The calibration curve is defined by a third degree polynomial curve fit of a plot of log MW vs. V~/V" where V~ is the elution volume of the standard and V, is the elution volume of the reference peak, oxygen, present as dissolved air in the injected solution. The columns and detector cell (Hewlett-Packard Differential Refractometer) are maintained at 40°C. The solvent (mobile phase) was tetrahydrofuran containing 250 ppm butylated hydroxytoluene (BHT, 2,6-di-tert-butyl-4-methylphenol) as a stabilizer (the tetrahydrofuran with BHT being available from Burdick and Jackson, Muskegon, MI). The mobile phase reservoir is purged with helium and is maintained at a flow rate of I milliliter per minute. Under these conditions, BHT eluted at 35.86 minutes. Samples are dissolved in THF, 0.25% wt/vol, and filtered through a 0.45 micron pore size "TEFLON" (polytetrafluoroethylene) membrane filter prior to injection (200 microliters) into the chromatograph. The reported molecular weights are the "polystyrene equivalent" molecular weights as calculated from the calibration curve.
For the pure monomer resins, the resins produced using the current invention have number average molecular weights (Mn) ranging from about 400 to 2000, weight average molecular weights (Mw) ranging from about 500 to 5000, Z average molecular weights (Mz) S ranging from about 500 to 10,000, and polydispersities (PD) as measured by Mw/Mn between about 1.2 and 3.5, typically between about 1.2 and 2.5. For the CS
hydrocarbon resins, the resins produced using the current invention have number average molecular weights (Mn) ranging from about 400 to 2000, weight average molecular weights (Mw) ranging from about 500 to 3500, Z average molecular weights (Mz) ranging from about 700 to 15,000, and polydispersities (PD) as measured by Mw/Mn between about I.2 and S, typically between about 1.2 and 3.5. For the C9 hydrocarbon resins, the resins produced using the current invention have number average molecular weights (Mn) ranging from about 400 to 1200, weight average molecular weights (Mw) ranging from about 500 to 2000, Z average molecular weights (Mz) ranging from about 700 to 6000, and polydispersities (PD) as measured by Mw/Mn between about 1.2 and 3.5, typically between about 1.2 and 2.5.
As mentioned previously, it is expected that narrower polydispcrsitics and lower molecular weights are obtained when the monomer is added to the catalyst solution than when the catalyst is added to the monomer. Taking into consideration the effect of the reaction sequence, it is expected that polydispersities more narrow than those obtained using traditional unsupported Lewis acid Friedel-Crafts catalysts can be obtained using the at least one of supported metal halides and metal halide solid acids if desired. Narrow polydispersity is important to ensure compatibility of resin with polymers in end use applications.
A third important reaction variable is the reaction temperature.
Polymerization temperatures between about -50°C and 150°C can be used in these reactions, however, more preferred reaction temperatures are between about -20°C and 100°C, most preferred temperatures are between about 0 ° C and 70 ° C. For pure monomer, the reaction temperature is preferably between about -50°C and 100°C, more preferably between about -20°C and 75°C, and most preferably between about -10°C and 60°C.
For CS monomers, the reaction temperature is preferably between about -50°C and 100°C, more preferably between about -20°C and 75°C, and most preferably between about -10°C
and 70°C. For C9 monomers, the reaction temperature is preferably between about 0°C and 150°C, more preferably between about 10°C and 120°C, and most preferably between about 20°C and 110°C.
Temperature is found to have a significant effect on the properties of the resulting resins.
Higher molecular weight and high softening point resins are prepared at lower reaction temperatures. The reaction time at reaction temperature is preferably between about 30 minutes and 8 hours, and more preferably between about 1 hour and 4 hours.
The polymerization process can be carried out as a continuous, semi-batch, or batch process in such diverse reactors as continuous, batch, semi-batch, fixed bed, fluidizcd bed, and plug flow. For instance, in continuous processes, a solution of the monomers can be passed over the catalyst in a fixed bed, or the monomers can be cofed with a catalyst slurry into a continuous reactor.
The reaction may be stopped by physically separating the at least one of supported metal halides and metal halide solid catalysts from the products. Physical separation may render the reaction solution neutral. Furthermore, physical separation can be performed by 1 S simple filtration or by separation of the resin solutions from a fixed catalyst bed. As a result, physical separation is easy and complete such that, for many the at least one of supported metal halides and metal halide solid acid catalysts, acid functionality and catalyst residue are not left in the resin product.
If leaching of acid is possible, then acid neutralization is required. This step is commonly known in the art as "quenching". For the at least one of supported metal halides and metal halide solid acid catalysts of the present invention which require quenching, less salt is generated than by traditional unsupported Lewis acid catalysts.
Thus, use of the at least one of supported metal halides and metal halide solid acid catalysts minimizes or eliminates the need for extra processing steps to quench the reactions, neutralize the catalyst, and filter the catalyst salt residues from the resulting products.
Once the at least one of supported metal halides and metal halide solid acid catalyst and resin solution are separated, the resin solution can be stripped to remove unreacted hydrocarbons, solvents, and low molecular weight oligomers which can be recycled through the process. When pure monomer is reacted, water white resins can be obtained from this invention in yields of up to about 99% based on starting monomer.
Resins obtained from this invention typically have softening points as measured by ASTM-E28 "Standard Test Method for Softening Point by Ring and Ball Apparatus"
(revised 1996), varying from preferably about 5°C to 170°C, more preferably from about 30°C to 150°C. For pure monomer, the softening points preferably range from about S°C
to 170°C, more preferably from about 50°C to 1 SO°C. For CS hydrocarbon resins, the softening point ranges from preferably about 5°C to 170°C, more preferably from about 50°C to 150°C, and most preferably about 70°C to 130°C. For C9 hydrocarbon resins, the softening point is preferably up to about 170°C, and the softening point range is most preferably from about 70°C to 160°C. Flowable resin or those that are liquids at room temperature can also be prepared if desired using proper reaction conditions.
After the resin is produced, it may be subsequently subjected to hydrogenation to reduce coloration and improve color stability. Hydrogenation of resins is well known in the art. For a discussion of hydrogenation, reference is made to U.S. Patent No.
5,491,214 to DAUGHENBAUGH et al., which is incorporated herein by reference in its entirety.
The resins of the current invention can be used as modifiers in adhesives, sealants, printing inks, protective coatings, plastics, road markings, flooring, and as dry cleaning retexturizing agents.
The at least one of supported metal halides and metal halide solid acid catalysts of the present invention offer several advantages over unsupported Lewis acids (e.g., AICI,) AIBr,, BF,, complexes of BF3, TiCla, and others which arc traditionally used for Friedcl-Crafts polymerizations). Many of these advantages are a result of the acid sites being an integral part of the solid catalysts or a Lewis acid supported on a solid.
Because the acid sites are an integral part of the solid catalyst or the Lewis acid is supported on a solid, contamination of the resin products or solvents with catalyst residues is minimal. As a result, the at least one of supported metal halides and metal halide solid acid catalysts do not impart color to the hydrocarbon resins due to catalyst residues. If pure styrene-based monomers are used, the resulting resins can be water white.
The at least one of supported metal halides and metal halide solid acid catalysts of the present invention can generally be regenerated and recycled to thereby minimize waste disposal of spent catalyst. In contrast, the unsupported Lewis acids are generally single use catalysts.
Further, the at least one of supported metal halides and metal halide solid acid catalysts of the present invention are nonhazardous when compared with traditional unsupported Lewis acid catalysts such as BF3 and AICI 3 The catalysts of the present WO 98/30587 PCT/US98l00012 invention generally do not generate corrosive or hazardous liquid or gaseous acids on exposure to moisture.
The present invention will be further illustrated by way of the following Examples.
Examples 1-17 involve pure monomer resins, Examples 18-53 involve CS resins, and $ Examples 54-76 involve C9 resins. These examples are non-limiting and do not restrict the scope of the invention.
Unless stated otherwise, all percentages, parts, etc. presented in the examples are by weight.
These examples illustrate the effect of zinc chloride supported on silica as a catalyst for the polymerization of pure monomer.
Catalyst preparation involves dissolving 20 grams of reagent grade zinc chloride in 75-100 ml methanol and adding to a slurry of synthetic amorphous silica, Grade "EP-12", Crosfield Limited, Warrington, England. The solution is stirred for 1 hour.
The solvent is slowly removed on a rotary evaporator to avoid bumping of the mixture. After the rotary evaporation, the material should be a free flowing solid. The catalyst is calcined by carefully heating the solid for 2 hours at 2 mm of Hg at 40°C, followed by 2 hours at 2 mm of Hg at 100°C, and finished at 1 hour at 2 mm of Hg at 140°C.
The catalyst is handled in a nitrogen filled glove bag prior to use.
Catalyst recycle tests were done in a jacketted one gallon reactor with a flat-bed turbine agitator, cooling coil, sample line, thermowell, bottom valve and sintered metal filters. The filters were located on the end of the sample line and in the bottom valve seat of the reactor and had a nominal rating of 7 microns. The jacket of the reactor was controlled at 0°C t 5°C. Thirty-five (35) grams of the supported zinc chloride catalyst described above and 1000 grams of toluene were added to the reactor. The catalyst/toluene mixture was cooled to 0°C.
A mixture of 866 grams of alpha-methyl styrene and 366 grams of styrene were pumped into the 1 gallon reactor at a rate such that the temperature was controlled to 0°C
~ 5°C by flowing -20°C fluid through the cooling coil. The time for pumping in the monomer was 100 minutes. The reactor was held at 0°C for an additional 3 hours. The catalyst was contained in the reactor by using the two in situ filters. One gram of catalyst was removed and one gram of fresh catalyst was added between each of the catalyst recycle tests. An aliquot of the filtered reaction mixture was rotary evaporated, with an end condition of 3 mm of Hg and 190°C to produce a resin product.
Subsequent reactions using the same catalyst were done in essentially the same manner. The yield and properties of the resins are listed in Table 1.
Ex. Catalyst Yield SofteningMolecular P Weight i t o Mn Mw Mz n (R&B) 1 ZnClz on silica 87% 135C 1176 2407 4492 2 Catalyst recycled from 76% 142C 1431 3268 6825 Example 1 3 Catalyst recycled from 59% 142C 1383 3467 7486 Example 2 The following examples illustrate the preparation of pure monomer resins using a catalyst to monomer addition scheme with styrene based monomers and a supported ZnClz on silica catalyst.
CATALYST PREPARATION
Zinc chloride (98% Aldrich, Milwaukee, WI), S.0 grams (0.037 mol), was dissolved in SO milliliters ofmethanol (reagent grade, Aldrich, Milwaukee, WI). The support material, 13.5 grams, ("EP12" silica from Crosfield Catalysts, Warrington, England which had been calcined at 1 SO°C under vacuum to remove excess water for the purpose of obtaining an accurate weight of the support) was added to the methanol solution. The slurry was stirred at room temperature for 30 minutes. The solvent was removed on a rotary evaporator at 2-S
mm Hg with mild heating to obtain a flowable powder. The catalyst was calcined at 150°C
under a dry nitrogen purge for 2 hours prior to use.
POLYMERIZATION
A S00 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, thermometer, and a dropping addition funnel. The flask was charged with 86.6 grams alpha-methyl styrene (reagent grade, Aldrich, Milwaukee, WI), 36.6 grams styrene (reagent grade, Aldrich, Milwaukee, WI), and 36.6 grams toluene (reagent grade, Aldrich, Milwaukee, WI). The monomers and solvent were dried as follows: the styrene based monomers were dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer) immediately prior to use, the toluene was dried over 3 angstrom molecular sieves prior to use.
The catalyst, 3.7 grams ZnClz/Si02 - prepared as described above, was transferred to the solid addition funnel in an inert, moisture free atmosphere. The catalyst was added to the reaction from the dropping addition funnel over 15 minutes maintaining the target reaction temperature with external cooling of the reaction flask. The reaction was stirred at temperature for a total reaction time of 1-2 hour.
After the reaction time was completed, the resulting resin solution was vacuum filtered from the catalyst at room temperature. The reaction flask and catalyst filter cake were rinsed with approximately 100 milliliters of toluene.
After catalyst filtration, the solvent was removed from the resin solution at 100°C
I S at 2-5 mm Hg. The resin oil was placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube, thermometer, and attached to a condenser and receiving flask. The resin oil was heated to 235°C with a nitrogen purge followed by a steam purge at 235-245°C to remove the light oil products. The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The resin produced has the properties listed in Table 2.
Example Reaction Yield SofteningMolecular Weight Temperature Point (R&B) Mn Mw Mz 4 0C 69% 150C 1770 4050 8250 5 25C 83% 122C 960 1470 2430 The following examples illustrate a range of resin properties available from the current invention using styrene and alpha-methyl styrene as the monomers and a calcined ZnClz on silica as the catalyst. When combined, the following examples serve to define a half factorial designed experiment with two variables. The variables in these experiments include reaction temperature and catalyst loading. Replicate points are included to estimate experimental error. The results from the following examples are used to generate a model equation for each measured response in terms of the variables studied. The responses S studied in these examples include: product yield, Ring and Ball softening point, and molecular weight distribution. as defined by number average molecular weight (Mn), weight average molecular weight (Mw), and Z average molecular weight (Mz).
CATALYST PREPARATION
Zinc chloride (98% Aldrich, Milwaukee, WI) 20.0 grams (0.15 mol) was dissolved in 300 milliliters of methanol (reagent grade, Aldrich, Milwaukee, WI). The support material, 80 grams, ("EP12" silica from Crosfield Catalysts, Warrington, England) was added to the methanol solution. The slurry was stirred at room temperature for 30 minutes.
The solvent was removed on a rotary evaporator at 2-5 mm Hg with mild heating to obtain a flowable powder. Prior to use, the catalyst was calcined for 2 hours at 40°C, 1 hour at 1 S 100°C, and 2 hours at 150°C all under vacuum.
POLYMERIZATION
A S00 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, thermometer, and a dropping addition funnel. The flask was charged with 86.6 grams alpha-methyl styrene (reagent grade, Aldrich, Milwaukee, WI), 36.6 grams styrene (reagent grade, Aldrich, Milwaukee, WI), and 36.6 grams toluene (reagent grade, Aldrich, Milwaukee, WI). Immediately prior to use, the styrene based monomers were dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer). Also prior to use, the toluene was dried over 3 angstrom molecular sieves.
The catalyst, prepared as described above, was transferred to the dropping addition funnel in an inert, moisture free atmosphere. The catalyst was added to the reaction from the dropping addition funnel over 15 minutes maintaining the target reaction temperature with external cooling of the reaction flask. The reaction solution was stirred at temperature for a total reaction time of 1 hour.
After completion of the reaction time, the resulting resin solution was vacuum filtered from the catalyst at room temperature. The reaction flask and catalyst filter cake were rinsed with approximately 100 milliliters of toluene.
After catalyst filtration, the resin oil was placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube, thermometer, and attached to a condenser and receiving flask. The resin oil was heated to 235°C
with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products.
The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The reaction conditions for each example are outlined in the Table 3 below.
The level of each variable was coded as -1, 0, or 1 for low, middle, and high, respectively. Use of coded variable values facilitates generation of the model equations for each response.
Coded values are included in parenthesis.
Ex. CatalystReaction Yield Softening Mol eculareight Point W
1 S LoadingTemp. (R&B) (wt%) Mn Mw Mz 6 3.25 25C (0) 74% 118C 910 1470 2420 (0) 7 1 (-1) 50C (I) 72% 68C 610 830 1130 8 6 (1) 25C (0) 86/~ 100C 960 I~50 2630 9 1 (-1 0C (-1 10% 142C 1240 2080 4400 ) ) 10 3.25 50C ( 1 73% 76C 660 890 1220 (0) ) I 3.25 25C (0) 77% 125C 1000 1680 2810 1 (0) 12 6 ( 50C ( 1 18% 70C 450 480 520 I ) ) 13 3.25 0C (-1) 36% 131C 1650 3100 5700 (0) 14 1 (-1) 25C (0) 64% 133C 1080 1680 2620 IS 6 (1) 0C (-1) 70% 139C 2130 5490 11780 16 3.25 25C (0) 63% 103C 790 1150 2110 (0) The data from the above tables was analyzed by regression analysis for each of the responses (steam stripped product yield, Ring and Ball softening point, Mn molecular weight, Mw molecular weight, and Mz molecular weight). The process variables, (reaction temperature (TMP) and catalyst loading (CAT), were coded to -l, 0, and 1 for the low, mid, _2g_ and high levels respectively. The following regression models were obtained based on the coded variables. The proportion of the variation in the response data that is explained by the models is listed as RZ(adj).
Equation 1 Resin Yield % - 72.8 - 29.3(CAT)(TMP) - 26.3(TMP)z Rz(adj) = 78.9%
Equation 2 R & B Softening Point - 110 - 33.0(TMP) Rz(adj) = 82.1%
Equation 3 In[Mn] - 6.86 - 0.537(TMP) - 0.214(CAT)(TMP) RZ(adj) = 93.7%
Eauation 4 In[Mw] - 7.32 - 0.780(TMP) - 0.385(CAT)(TMP) R-'(adj) = 94.0%
Equation 5 (n[Mz] - 7.81 - 1.02(TMP) - 0.45(CAT)(TMP) R'(adj) = 96.4%
The regression equations listed above can be used to predict the properties of all resins which can be obtained for a set of reaction conditions where the control variables lie within the intervals tested. Contour plots can be generated to investigate the factor effects and make comparisons of resin properties predicted to be generated using various reaction conditions. Sample contour plots are shown in Figures 1 - 4 for product yield, Mn, Mw, and Mz molecular weights versus catalyst loading and reaction temperature.
This example demonstrates the use of supported aluminum trichloride as a catalyst for the polymerization of styrene based monomers.
CATALYST PREPARATION
Aluminum chloride (- 40 mesh, Vanchlor Co., Inc., Lockport, NY), 20.0 grams (0.15 mol), was dissolved in 100 milliliters of toluene dried over 4 angstrom molecular sieves (reagent grade, Aldrich, Milwaukee, WI). The support material, 80 grams, ("EP12" silica from Crosfield Catalysts, Warrington, England) was dried prior to contacting the aluminum trichloride solution for 2 hours at 40°C, 1 hour at 100°C, and 2 hours at 150°C all under vacuum. The aluminum trichloride solution was added to the dried support material and the resulting slurry was stirred at room temperature for 30 minutes. The solvent was removed under vacuum at 2-5 mm Hg while maintaining the temperature near 40°C
to obtain a flowable powder. Prior to use, the catalyst was stored and handled in an inert atmosphere.
POLYMERIZATION
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, thermometer, and a dropping addition funnel. The flask was charged with 86.6 grams alpha-methyl styrene (reagent grade, Aldrich, Milwaukee, WI), 36.6 grams styrene (reagent grade, Aldrich. Milwaukee) WI), and 36.6 grams toluene (reagent grade, Aldrich, Milwaukee, WI). Immediately prior to use, the styrene based monomers were dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer). Prior to use, the toluene was dried over 3 angstrom molecular sieves.
The catalyst, 2.5 wt% based on monomer, was transferred to the dropping addition funnel in an inert, moisture free atmosphere. The catalyst was added to the reaction from the dropping addition funnel over 1 S minutes maintaining a 25°C
reaction temperature with external cooling of the reaction flask. The reaction solution was stirred at temperature for a total reaction time of 1 hour.
After completion of the reaction time, the resin solution was vacuum filtered from the catalyst at room temperature. The reaction flask and catalyst filter cake were rinsed with approximately 100 milliliters of toluene.
After catalyst filtration, the resin oil was placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube, thermometer, and attached to a condenser and receiving flask. The resin oil was heated to 235°C
with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products.
The steam purge was S continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The following summarizes the reaction conditions and resin properties.
Reaction temperature 25°C
Resin yield 24%
Ring and Ball Softening Point 59°C
Molecular Weight Mn 520 Mw 600 Mz 740 These examples illustrate the effect of zinc chloride supported on a variety of substrates as a catalyst for the polymerization of piperylene concentrate, a CS feed.
CATALYST PREPARATION
Zinc chloride (98% Aldrich, Milwaukee, WI) 27.3 grams (0.2 mol ) was dissolved in 300 milliliters of methanol (reagent grade, Aldrich, Milwaukee, WI). The support material, 100 grams, ("F-22" and "F-6" acid treated clays from Engelhard, Iselin, NJ, "K-10"
acid treated clay from Sud Chemie, Munich, Germany, or "EP12" silica from Crosfield Catalysts, Warrington, England) was added to the methanol solution. The slurry was stirred at room temperature for 30 minutes. The solvent was removed on a rotary evaporator at 2-5 mm Hg with mild heating to obtain a flowable powder. The catalyst was calcined at 1 SO°C
under a dry nitrogen purge for 2 hours prior to use.
POLYMERIZATION
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, a thermometer, and a dropping addition funnel. The flask was charged with 60 grams of toluene (reagent grade, Aldrich Milwaukee, WI) and 14 grams of the supported zinc chloride catalyst as prepared above. The catalyst slurry was heated to SO°C with stirring.
Piperylene concentrate (Naphtha Petroleum 3 "Piperylenes", Lyondell Petrochemical Company, Houston, TX), 140 grams, was added to the nitrogen purged reaction flask via the dropping addition funnel over 15 minutes. Immediately prior to use, the monomers and solvent were dried as follows, the solvents were dried over 4 angstrom molecular sieves and the piperylene concentrate was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams of alumina to 1 milliliter of monomer).
The reaction solution was stirred at 50°C for a total reaction time of one hour. The resulting resin solution was separated from the catalyst by vacuum filtration at room temperature. The volatile components and solvent were removed by heating the reaction solution to 50°C under vacuum (2-5 mm Hg) for 2 hours. The flask was fitted with a distillation head with an adaptor for an inlet tube and a thermometer, and attached to a condenser and receiving flask. The resin oil in the flask was then heated to 235°C with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products. The steam purge was continued until less than t ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The resins produced have the properties listed in Table 4. Examples 18-21 are in accordance with the present invention, whereas Comparative Example 22 is for comparison purposes.
Example Catalyst Yield SofteningMolecular P Weight i o nt Mn Mw Mz (R&B) 18 ZnClz on F-22 13% 40C I 520 2710 6500 Clay S 19 ZnCl2 on F-6 28% 41 C 1400 2490 6760 Clay 20 ZnCIZ on K-10 13% - 1160 2180 5160 Clay 21 ZnCl2 on EP12 64% 44C 1350 2360 4320 silica 22 ZnCh unsupported0% - - - -These examples illustrate the effect of reaction temperature on the polymerization of piperylene concentrate, a CS feed, with zinc chloride supported on silica.
Reaction procedures are similar to those listed for Examples l 8-22. The catalyst used was ZnClz on "EP12" silica prepared as described in Example 7 above. The reaction temperature was varied as described in the Table 5 below with the properties of the resulting resin also listed in Table 5.
TABLE S
Example Catalyst and Yield SofteningMolecular R P Weight ti i T
eac nt on o Mn Mw Mz emperature (R&B) 23 ZnCI,/Si02 - 50C 50'% 30C 1000 1710 3260 24 ZnCI~/SiO~ - 25C 29% 27C 1410 2300 3600 25 ZnCh/SiOz - 0C 14% 31 C 1480 2640 4360 These examples illustrate the effect of zinc chloride loading on silica and the total zinc loading in the reaction on the polymerization of piperylene concentrate, a CS feed. At a constant wt% ZnClz based on monomer, higher resin yields are obtained at lower loadings of ZnClz on the silica. For a given loading of ZnCl2 on silica, higher yields are obtained at higher loadings of catalyst with respect to monomer.
CATALYST PREPARATION
Catalyst A
Zinc chloride on silica was prepared as described in Example 21.
Catalyst B
Zinc chloride (98% Aldrich, Milwaukee, WI) 13.7 grams (0.059 mol) was dissolved in 150 grams of methanol (reagent grade, Aldrich, Milwaukee, WI). The support material, 25 grams, ("EP12" silica from Crosfield Catalysts, Warrington, England) was added to the methanol solution. The slurry was stirred at room temperature for 30 minutes.
The solvent was removed on a rotary evaporator at 2-S mm Hg with mild heating to obtain a ilowablc powder. The catalyst was calcined at 150°C under a dry nitrogen purge for 2 hours prior to use.
1 S Catalyst C, D, and E
The procedures for preparing catalysts C-E were similar to the procedures outlined for catalyst B. The zinc chloride loading for each catalyst is as follows, 20.> grams for catalyst C, 27.3 grams for catalyst D, and 34.2 grams for catalyst E using 25 grams of silica.
POLYMERIZATION
Preparation of the resins was as described for Examples 18-22. Catalysts and catalyst loadings were as described in the Table 6 and the resulting resin had the properties listed in Table 6.
ExampleCat. Loading LoadingYield SofteningMolecular Weight Cat. ZnClz Point wt% wt% (R&B) Mn Mw Mz 26 A 10 2.1 64% 44C 1350 2360 4320 27 B 3.6 1.3 23% 39C 1630 3000 5400 28 B 6.1 2.1 26% 43C 1690 3050 5390 29 B 10 3.5 39% 42C 1540 2810 4960 30 C 3.4 1.5 12% 21 C 1370 2290 4930 31 C 4.8 2.1 21% 25C 1410 2220 3750 32 C 10 4.5 34% 19C 1270 1990 3110 33 D 2.5 1.3 6% 41 C 1890 3660 6810 34 D 4.1 2.1 11% 38C 1790 3270 5820 S 35 D 10 5.2 27% 39C 1550 2970 5560 36 E 3.7 2.1 7% 25C 1520 2540 4480 These examples illustrate the effect of unsupported metal halides as catalysts for the I 0 polymerization of pipcrylene concentrate, a CS feed. In particular, these examples compare the effectiveness of the solid acid catalyst ZrCl4 with the effectiveness of the conventional Lewis acids FeCI, and A1C1~.
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, a thermometer, and a dropping addition funnel. The I S flask was charged with 30 grams toluene (reagent grade, Aldrich Milwaukee, WI) and 0.008 moles of the metal chloride catalyst, FeCl3 97%, ZrCI~ 99.9+% (all from Aldrich, Milwaukee, WI) and A1C13 (Vanchlor Co. Inc., Lockport, NY). The catalyst slurry was heated to 50°C with stirring.
Piperylene concentrate (Naphtha Petroleum 3 "Piperylenes", Lyondell Petrochemical 20 Company, Houston, TX), 100 grams, was added to the nitrogen purged reaction flask via the dropping addition funnel over 1 S minutes. Immediately prior to use, the monomers and solvent were dried as follows, the solvent was dried over 4 angstrom molecular sieves and the piperylene concentrate was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams of alumina to 1 milliliter of monomer).
25 The reaction solution was stirred at 50°C for a total reaction time of two hours.
Catalyst solids were removed from the reaction solution via filtration. After filtration, the reaction solutions were quenched with 4 milliliters of NI-I40H in 100 milliliters of water and the water removed using a separatory funnel. After quenching, the resin solution was separated from the catalyst salts formed during quenching by vacuum filtration at room 30 temperature.
The resin oil was then placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube and a thermometer, and attached to a WO 98/30587 PCT/US98/00(112 condenser and a receiving flask. The resin oil was heated to 200°C to 235°C with a nitrogen purge for all resins, followed by a steam purge at 235-245°C to remove light oil products for the AlCl3 and ZrCl4 reactions. The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was $ collected. The steam purge was followed by a nitrogen purge at 235°C
to remove water from the remaining resin.
The resins produced have the properties listed in Table 7. Examples 37 and 39 are in accordance with the invention, whereas Comparison Example 38 is for comparison purposes.
Example Catalyst Yield Softening Molecular Point Weight (R&B) Mn Mw Mz 37 FeCl3 7%' - 950 3750 16910 38 A1C1~ 52% 95C 1580 3120 6790 39 ZrCl4 52% ~ 68C I 2250 I 5730 I 15160 1. Sample was not steam stripped.
These examples illustrate the effect of supported metal halides as catalysts for the polymerization of piperylene concentrate, a CS feed.
CATALYST PREPARATION
Supported ZnCl2 and FeCl3 Zinc chloride, 98+%, or iron chloride, 97%, {both from Aldrich, Milwaukee, WI) grams was dissolved in 100 milliliters of methanol (Reagent grade, Aldrich, Milwaukee, WI). The support material, 24 grams, ("EP12" silica from Crosfield Catalysts, Warrington, England) was added to the methanol solution. The slurry was stirred at room temperature for 30 minutes. The solvent was removed on a rotary evaporator at 2-5 mm Hg with mild heating to obtain a flowable powder. The catalyst was calcined at 150°C
under a dry nitrogen purge for 2 hours prior to use.
Supported BiCl3, AICl3, and ZrCl4 The silica support material ("EP12" from Crosfield Catalysts, Warrington, England) was dried under vacuum, 2-5 mm Hg, using the following thermal cycle, 0.5 hours at room temperature, 1 hour at 35-40°C, 1.5 hours at 100°C, and 2 hours at 150°C. The dried support was added to the reaction flask under an inert atmosphere with the desired metal halide, 6 grams, (bismuth chloride or zirconium tetrachloride from Aldrich, Milwaukee, WI, or aluminum chloride from Vanchlor Chemical, Inc., Lockport, NY). Toluene, 100 ml, was added via syringe to the solids. The catalyst slurry was stirred at ambient temperature for one hour and the solvent removed under vacuum, 2-5 mm Hg, maintaining the temperature near 20°C. Drying the flowable solid continued under vacuum at ambient temperature for 3 hours.
POLYMERIZATION
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, a thermometer, and a dropping addition funnel. The flask was charged with 30-50 grams of toluene (reagent grade, Aldrich Milwaukee, W1) and 0.011 moles of the metal chloride on the catalyst support as prepared above.
The catalyst slurry was heated to 50°C with stirnng.
Piperylene concentrate (Naphtha Petroleum 3 "Piperylenes", Lyondell Petrochemical Company, Houston, TX)) 100 grams, was added to the nitrogen purged reaction flask via the dropping addition funnel over 1 S minutes. Immediately prior to use, the monomers and solvent were dried as follows, the solvent was dried over 4 angstrom molecular sieves and the piperylene concentrate was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams of alumina to 1 milliliter of monomer).
The reaction solution was stirred at 50°C for a total reaction time of two hours.
Catalyst solids were removed from the reaction solution via filtration. The reaction solutions were quenched with 4 milliliters of NH40H in 100 milliliters of water and the water removed using a separatory funnel. After quenching, the resin solution was separated from any catalyst salt residues formed during quenching by vacuum filtration at room temperature.
The resin oil was then placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube and a thermometer, and attached to a condenser and a receiving flask. The resin oil was heated to 23 $ °C
with a nitrogen purge followed by a steam purge at 23$-24$°C to remove light oil products.
The steam purge was $ continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 23$°C to remove water ftom the remaining resin.
The resins produced have the properties listed in Table 8.
Example Catalyst Yield Softening Molecular Point Weight (R&B) Mn Mw Mz 40 BiCI,/Si0211 - 1290 1900 6300 %
41 ZnCl2/SiOz37/~ 42C 1780 2990 $340 1$ 42 FeCl3/Si027% - 9$0 2360 10800 43 A1C13/SiOZ41 $4C 990 1490 2410 %
44 ZrCl4/Si02$$/> 60C 1310 2370 46$0 COMPARATIVE EXAMPLE 4$
This comparative example illustrates that the silica used as a support for the metal halide catalysts is not an effective catalyst for C$ hydrocarbon resin synthesis.
POLYMERIZATION
A $00 milliliter three neck flask was equipped with an overhead stirrer, reflux 2$ condenser, gas inlet and outlet ports, a thermometer, and a dropping addition funnel. The flask was charged with 60.0 grams of toluene (reagent grade, Aldrich, Milwaukee, WIl and 14.0 grams silica ("EP12" grade, Crosfield Catalysts, Warrington England).
Prior to use, the solvent was dried over 4 angstrom molecular sieves. The catalyst slurry was heated to $0°C with stirnng.
Piperylene concentrate (Naphtha Petroleum 3 "Piperylenes", Lyondell Petrochemical Company, Houston, TX), 140 grams, was added to the nitrogen purged flask via the dropping addition funnel over 1$ minutes. Prior to use, the piperylene concentrate was dried _3g_ by passing through a column of activated alumina (Fischer 8-I6 mesh, 0.3 grams of alumina to I milliliter of monomer). The reaction solution was stirred at 50°C
for a total reaction time of one hour.
After completion of the reaction time, the resulting resin solution was separated from the silica by vacuum filtration at room temperature. The volatile materials were removed under reduced pressure at 50°C, no product remained.
These examples serve to illustrate the reuse of a ZrCl4 supported on silica as a catalyst for the polymerization of piperylene concentrate, a CS monomer feed.
CATALYST PREPARATION
The silica support material ("EP12" silica from Crosfield Catalysts, Warrington, England) was dried under vacuum, 2-5 mm Hg, using the following thermal cycle, 0.5 hours at room temperature, 1 hour at 35-40°C, 1.5 hours at 100°C, and 2 hours at 150°C. The 1 S dried support was added to the reaction flask under an inert atmosphere with zirconium tetrachloride (Aldrich, Milwaukee, WI). Loadings for the 10% catalyst were 3 grams ZrCl4 and 27 grams silica and for the 5% catalyst were 3 grams ZrCl4 and 57 grams silica.
Toluene, 100 ml, which had been dried over 4 angstrom molecular sieves, was added via syringe to the solids. The catalyst slurry was stirred at ambient temperature for one hour and the solvent removed under vacuum, 2-S mm Hg, maintaining the temperature near 20°C.
Drying the flowable solid continued under vacuum at ambient temperature for 3 hours.
POLYMERIZATION
A S00 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, a thermometer, and a dropping addition funnel. The flask was charged with 70 grams toluene (reagent grade, Aldrich Milwaukee, WI) and catalyst as follows. Prior to use, the solvent was dried over 4 angstrom molecular sieves.
For the 10% catalyst, 25.6 grams supported catalyst prepared as described above was added.
For the 5% catalyst, 51.2 grams supported catalyst prepared as described above was added.
Thus, in each case, 2.56 grams ZrCl4, 0.011 moles of the metal chloride was added to the solution. The catalyst slurry was heated to SO°C with stirring.
Piperylene concentrate (Naphtha Petroleum 3 "Piperylenes", Lyondell Petrochemical Company, Houston, TX), 100 grams, was added to the nitrogen purged reaction flask via the dropping ftumel over 15 minutes. Prior to use, the piperylene concentrate was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer). The reaction solution was stirred at 50°C for a total reaction time of two hours.
For the recycle examples, the catalyst was allowed to settle and the reaction solution removed from the flask via syringe. The catalyst was washed with 100 milliliters of dry toluene which was also removed from the catalyst via syringe. Additional solvent and monomer was added to the catalyst as described above.
For all of the examples, after completion of the reaction time, catalyst solids were removed from the reaction solution via filtration. The reaction solutions were then quenched with 4 milliiiters of NH40H in 100 milliliters of water and the water removed using a separatory funnel. The resin solution was then separated from any catalyst salt residues formed during quenching by vacuum filtration at room temperature.
The resin oil was then placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube, thermometer, and attached to a condenser and receiving flask. The resin oil was heated to 235°C with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products. The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The resins produced have the properties listed in Table 9.
Example Catalyst Yield Softening Molecular Weight Point (R&B) Mn Mw Mz 46 10% ZrCl4/Si0243% 63C 1890 3830 8490 47 10% ZrCl4/Si0247% 56C 1940 4020 8200 recycle 48 5% Zl'Cl4/SlOz35% 57C 1450 2910 6860 49 S% ZrCl4/Si0259% 49C 1440 3170 7460 recycle These examples illustrate the use of a supported aluminum trichloride catalyst on alumina for the polymerization of piperylene concentrate, a CS monomer feed.
POLYMERIZATION
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, a thermometer, and a dropping addition funnel. The flask was charged with 40 grams toluene (reagent grade, Aldrich Milwaukee, WI) and a solid supported aluminum trichloride catalyst, "CAT-59" catalyst (UOP, Des Plains, IL) as outlined below.
Prior to use, the solvent was dried over 4 angstrom molecular sieves. Also prior to use, the catalyst was crushed to a powder. All catalyst handling was performed in a nitrogen purged atmosphere. The catalyst slurry was heated to 50°C with stirring.
Piperylene concentrate (Naphtha Petroleum 3 "Piperylenes", Lyondell Petrochemical Company, Houston, TX), 100 grams, was added to the nitrogen purged reaction flask via the dropping addition funnel over 15 minutes. Immediately prior to use, the pipcrylene concentrate was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer). The reaction solution was stirred at _SO°C for a total reaction time of one hour.
Upon completion of the reaction time, the catalyst solids were removed from the reaction solution via filtration. The reaction solutions were then quenched with 4 milliliters of NH40H in 100 milliliters of water and the water removed using a separatory funnel.
After quenching, the reaction solution was then separated from any catalyst salt residues formed by vacuum filtration at room temperature.
The resulting resin solution was then washed to neutral pH with water and dried over MgS04 (reagent grade, Aldrich, Milwaukee, WI) The resin oil was then placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube, thermometer, and attached to a condenser and receiving flask. The resin oil was heated to 235°C with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products. The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The resins produced have the properties listed in Table 10.
Ex. Catalyst Yield SofteningMolecular Weight Point (R&B) Mn Mw Mz 50 27 wt% "CAT-59" 50% 62C 1510 2900 5950 on monomer 51 13.5 wt% "CAT-59"27% 62C 1640 3320 6980 on monomer These examples demonstrate the use of a synthetic supported aluminum trichloride as a catalyst for the polymerization of piperylene concentrate, a CS monomer feed.
CATALYST PREPARATION
Aluminum chloride (- 40 mesh, Vanchlor Co., Inc., Lockport, NY) 7.5 grams (O.U6 mol) and the support material, 30 grams "EP12" silica (Crosficld Catalysts) Warrington, England), were combined with 180 milliliters of toluene dried over 4 angstrom molecular sieves (reagent grade, Aldrich, Milwaukee, WI). The support material was dried prior to contacting with the aluminum trichloride solution for 2 hours at 40°C, 1 hour at 100°C, and 2 hours at I50°C all under vacuum. The aluminum trichloride solution was added to the dried support material and the resulting slurry was stirred at room temperature for one hour.
'The solvent was removed under vacuum at 2-5 mm Hg while maintaining the temperature near 25-30°C to obtain a flowable powder. The catalyst was stored and handled under an inert atmosphere prior to use.
POLYMERIZATION
Resins were prepared by the procedures outlined for Examples 50 and 5 I above.
The resins produced have the properties listed in Table 11.
Example Catalyst Yield SofteningMolecular Weight P
i o nt (R&B) Mn Mw Mz 52 7.5 wt% A1C13/SiOz21% 54C 960 1330 2010 on monomer 53 3.75 wt% 26% 47C 1030 1540 2610 AlCl3/Si02 on monomer These examples illustrate the use of zinc chloride on a variety of support materials as solid acid catalysts for the preparation of hydrocarbon resins from C9 unsaturated aromatic hydrocarbon feed stocks.
The supported zinc chloride catalysts were prepared by dissolving 27.3 grams ZnCI, (Aldrich Milwaukee, WI) in 300 grams of methanol (reagent grade, Aldrich, Milwaukee, WI). One hundred grams of support was added to the methanol solution and stirred as a 1 S slurry for 30 minutes. The support materials used were "F-22" and "F-6"
clays (Engelhard Corporation, Iselin, NJ), "K 10" clay (Sud Chemie/Llnited Catalyst Inc., Louisville, KY), and "EP12" silica (Crosfield Catalysts, Warrington, England). The methanol was evaporated from the catalysts on a rotary evaporator under reduced pressure.
The catalysts were calcined at 150°C for 2 hours under a nitrogen purge prior to use.
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, thermometer, and a dropping addition funnel. The flask was charged with 50 grams of toluene (reagent grade, Aldrich Milwaukee, WI) and 1 S
wt°/> of the supported ZnCl2 catalysts described above.
The C9 monomer feed, 100 grams of "LRO-90" (from Lyondell Petrochemicals, Houston, TX), was added to the flask via the dropping addition funnel.
Immediately prior to use, the monomers and solvent were dried as follows: the C9 monomer feed was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams of alumina to 1 milliliter of monomer). Also immediately prior to use, the toluene was dried over 3 angstrom molecular sieves prior to use.
The reaction solution was heated to a 50°C reaction temperature. The monomer was added to the reaction flask from the dropping addition funnel at a rate to maintain the desired reaction temperature with external cooling. Monomer addition time was approximately 1 S
minutes. The reaction solution was stirred at the desired reaction temperature for a total reaction time of 2 hours.
After completion of the reaction time, the resin solution was vacuum filtered from the acid treated clay catalyst at room temperature. The reaction flask and catalyst filter cake were rinsed with approximately 100 milliliters of toluene.
After catalyst filtration, the solvent was removed from the resin solution at 100°C
at 2-5 mm Hg. Also, the resin oil was placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube and a thermometer, and attached to a condenser with a receiving flask. The resin oil was heated to 23S°C
with a nitrogen purge followed by a steam purge at 23S-24S°C to remove light oil products.
The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensatc or until 1000 ml of steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
1 S The resins produced have the properties listed in Table 12. Examples S4-S7 are in accordance with the present invention, whereas Comparison Example 58 is for comparison purposes.
Example Catalyst Yield Softening ~ Mo lecular Point Weight (R&B) Mn Mw Mz 54 ZnCI,/F-2229% 121 C 680 96n 1390 SS ZnCh/K 39% 101C 540 800 1230 S6 ZnCI,/EP1238% 113C 590 8S0 2590 S7 ZnCI,/F-6 40% 124C 690 960 1410 S8 ZnCl2 0% - - - -The following examples illustrate the effect on C9 resin properties produced using a supported ZnCl2 catalyst on silica at various reaction temperatures and catalyst loadings.
CATALYST PREPARATION
Zinc chloride {98% Aldrich, Milwaukee, WI), S.0 grams (0.037 mol), was dissolved in 50 milliliters of methanol (reagent grade, Aldrich, Milwaukee, WI). The support material, 13.5 grams, ("EP12" silica from Crosfield Catalysts, Warnngton, England which had been calcined at 1 SO°C under vacuum to remove excess water for the purpose of obtaining an accurate weight of the support) was added to the methanol solution. The slurry was stirred at room temperature for 30 minutes. The solvent was removed on a rotary evaporator at 2-5 mm Hg with mild heating to obtain a flowable powder. The catalyst was calcined at 150°C
under a dry nitrogen purge for 2 hours prior to use.
POLYMERIZATION
A S00 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, thermometer, and a dropping addition funnel. The flask was charged with 50 grams of toluene (reagent grade, Aldrich Milwaukee, W1) and a supported ZnClz on Si02 prepared as described about. Prior to use, the toluene was dried over 3 angstrom molecular sieves. The catalyst level for each reaction is described in Table 13 below.
The C9 monomer feed, 100 grams ("LRO-90" from Lyondell Petrochemicals, Nouston, TX) was added to the dropping addition funnel. Immediately prior to use, the C9 monomer feed was dried by passing through a column of activated alumina (Fischer 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer). The reaction solution was heated to the reaction temperature described in Table 13 below. The monomer solution was added to the reaction flask from the dropping addition funnel at a rate to maintain the desired reaction temperature with external cooling. Monomer addition time was approximately 1 ~
minutes.
The reaction solution was stirred at the desired reaction temperature for a total reaction time of 2 hours.
Upon completion of the reaction time, the resin solution was vacuum filtered from the catalyst at room temperature. The reaction flask and catalyst filter cake were rinsed with approximately 100 milliliters of toluene.
After filtration, the resin oil was placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube and thermometer and attached to a condenser with a receiving flask. The resin oil was heated to 235°C
with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products.
The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The resins produced have the properties listed in Table 13.
Ex. Catalyst ReactionYieldSoftening M olecularWeight Loading Temp. Point (R&B) Mn Mw Mz PD
59 S wt% 100C 41% 102C 530 750 1440 1.4 60 20 wt% 60C 38% 134C 790 1220 4410 1.6 61 5 wt% 20C 7% 145C 1010 1750 3950 1.8 62 12.5 wt% 100 40% I 07 C 620 810 2040 1.3 C
63 12.5 wt% 60C 37% 132C 880 1210 2100 1.4 64 20 wt% 100C 42% 105C 620 810 2730 1.3 65 12.5 wt% 20C 1% - 790 2450 8260 3.1 66 5 wt% 60C 18% 139C 910 1230 2210 1.4 67 20 wt% 20C I% - 960 2890 8040 ?.8 68 12.5 wt% 60C 25% 122C 790 1070 1950 1.4 69 12.5 wt% 60C 17% 123C 740 960 1320 1.3 70 S wt% 136C 37% 88C 480 600 790 1.3 7l 12.5 wt% 136C 41% 62C 390 470 580 1.2 72 20 wt% 120C 35% 80C 490 580 690 1.2 I
The following examples illustrate the effect on C9 resin properties produced using a supported ZnClz catalyst on silica at various reaction temperatures and catalyst loadings.
CATALYST PREPARATION
Zinc chloride (98% Aldrich, Milwaukee, WI), 20.0 grams (0.1 S mol), was dissolved in 300 milliliters of methanol (reagent grade, Aldrich, Milwaukee, WI). The support material, 80 grams, ("EP 12" silica from Crosfield Catalysts, Warrington, England) was added to the methanol solution. The slurry was stirs ed at room temperature for 30 minutes.
The solvent was removed on a rotary evaporator at 2-5 mm Hg with mild heating to obtain a flowable powder. The catalyst was calcined for 2 hours at 40°C, 1 hour at 100°C, and 2 hours at 150°C all under vacuum prior to use.
POLYMERIZATION
A 500 milliliter three neck flask was equipped with an overhead stirrer, reflux condenser, gas inlet and outlet ports, thermometer, and a dropping addition funnel. The flask was charged with 100 grams of toluene (reagent grade, Aldrich Milwaukee, WI) and a supported ZnClz on SiOz prepared as described above. Prior to use, the toluene was dried over 3 angstrom molecular sieves. The catalyst level for each reaction is described in Table 14 below.
The C9 monomer feed, 100 grams ("LRO-90" from Lyondell Petrochemicals, Houston, TX) was added to the dropping addition funnel. Immediately prior to use, the C9 monomer feed was dried by passing through a column of activated alumina (Fischcr 8-16 mesh, 0.3 grams alumina to 1 milliliter monomer). The reaction solution was heated to the reaction temperature described in Table 14 below. The monomer solution was added to the reaction flask from the dropping addition funnel at a rate to maintain the desired reaction temperature with external cooling. Monomer addition time was approximately 15 minutes.
The reaction solution was stirred at the desired reaction temperature for a total reaction time of 2 hours.
Upon completion of the reaction time, the resin solution was vacuum filtered from the catalyst at room temperature. The reaction flask and catalyst filter cake were rinsed with approximately 100 milliliters of toluene.
After filtration, the resin oil was placed in a round-bottom flask which was fitted with a distillation head with an adaptor for an inlet tube and thermometer and attached to a condenser with a receiving flask. The resin oil was heated to 235°C
with a nitrogen purge followed by a steam purge at 235-245°C to remove light oil products.
The steam purge was continued until less than 1 ml of oil was collected per 100 ml of steam condensate or until 1000 ml steam condensate was collected. The steam purge was followed by a nitrogen purge at 235°C to remove water from the remaining resin.
The resulting resins had the properties listed in Table 14.
WO 98130587 PCT/iJS98/00012 Ex. CatalystReactionYield SofteningMolecular I Weight LoadingTemp. Point (R&B) Mn Mw Mz PD
73 10 wt% 50C 37% 134C 830 1280 2040 1.5 74 5 wt% 50C 21% 144C 890 1380 2260 1.6 75 10 wt% 100C 28% 126C 690 920 1320 1.3 76 10 wt% 50C 35% 141 C 850 1230 1890 1.5 While the invention has been described in connection with certain preferred embodiments so that aspects thereof may be more fully understood and appreciated, it is not intended to limit the invention to these particular embodiments. On the contrary, it is intended to cover all alternatives, modifications and equivalents as may be included within the scope of the invention as defined by the appended claims.
Claims (29)
1. A process for making a hydrocarbon resin, comprising polymerizing a feed seam comprising at least one member selected from the group consisting of pure monomer, C5 monomers, and C9 monomers in the presence of a supported metal halide solid acid catalyst to produce a hydrocarbon resin) wherein substantially all freely-associated water has been removed from the supported metal halide solid acid catalyst.
2. The process of claim 1, wherein water removal from the supported metal halide solid acid catalyst comprises calcining at a temperature up to about 700°C.
3. The process of claim 1, wherein the supported metal halide comprises a metal halide and a support, and wherein substantially all freely-associated water has been removed from the support before the support is combined with the metal halide.
4. The process of claim 1, wherein the supported metal halide solid acid catalyst comprises Lewis acid on clay, and wherein the Lewis acid comprises at least one member selected from the group consisting of ZnCl2, AlCl3, AlBr3, BF3, BCl3, FeCl3, SnCl4, TiCl4, ZrCl4, HfCl4, BiCl3, and lanthanide halides.
5. The process of claim 1, wherein the supported metal halide solid acid catalyst comprises Lewis acid on silica, and wherein the Lewis acid comprises at least one member selected from the group consisting of ZnCl2, AlCl3, BF3, BCl3, FeCl3, SnCl4, TiCl4, ZrCl4, HfCl4, BiCl3, and lanthanide halides.
6. The process of claim 1, wherein the supported metal halide solid acid catalyst comprises Lewis acid on silica-alumina, and wherein the Lewis acid comprises at least one member selected from the group consisting of ZnCl2, AlCl3, BF3, BCl3. FeCl3, SnCl4, TiCl4, ZrCl4, HfCl4, BiCl3, and lanthanide halides.
7. The process of claim 1, wherein the supported metal halide catalyst comprises Lewis acid on mesoporous silica, and wherein the Lewis acid comprises at least one member selected from the group consisting of ZnCl2, AlCl3, BF3, BCl3, FeCl3. SnCl4, TiCl4, ZrCl4, HfCl4, BiCl3, and lanthanide halides.
8. The process of claim 1, wherein the supported metal halide catalyst comprises Lewis acid on mesoporous silica-alumina, and wherein the Lewis acid comprises at least one member selected from the group consisting of ZnCl2, AlCl3, BF3, BCl3, FeCl3, SnCl4, TiCl4, ZrCl4, HfCl4, BiCl3, and lanthanide halides.
9. The process of claim 1, wherein the supported metal halide solid acid catalyst comprises Lewis acid on ion exchange resin, and wherein the Lewis acid comprises at least one member selected from the group consisting of ZnCl2, AlCl3, BF3, BCl3, FeCl3, SnCl4, TiCl4, ZrCl4, HfCl4, BiCl3, and lanthanide halides.
10. The process of claim 1, wherein the supported metal halide solid acid catalyst comprises Lewis acid on zeolite, and wherein the Lewis acid comprises at least one member selected from the group consisting of ZnCl2, AlCl3, BF3, BCl3, FeCl3, SnCl4, TiCl4, ZrCl4, HfCl4, BiCl3, and lanthanide halides, and wherein the zeolite comprises at least one member selected from the group consisting of zeolite Y, zeolite .beta., MFI, MEL, NaX, NaY, faujasite, and mordenite.
11. The process of claim 1, wherein the supported metal halide solid acid catalyst comprises polymer grafted aluminum halide.
12. The process of claim 1, wherein the feed stream comprises at least pure monomer, and wherein the pure monomer comprises at least one member selected from the group consisting of styrene, alpha-methyl styrene, beta-methyl styrene, 4-methyl styrene, and vinyl toluene fractions.
13. The process of claim 1, wherein the feed stream comprises at least C5 monomers comprising at least one member selected from the group consisting of isobutylene, 2-methyl-2-butene, 1-pentene, 2-methyl-1-pentene, 2-methyl-2-pentene, 2-pentene, cyclopentene, cyclohexene, 1,3-pentadiene, 1,4-pentadiene, isoprene, 1,3-hexadiene, 1,4-hexadiene, cyclopentadiene, and dicyclopentadiene.
14. The process of claim 1, wherein the feed stream comprises at least C9 monomers comprising at least one member selected from the group consisting of styrene, vinyl toluene, indene, dicyclopentadiene, and alkylated derivatives thereof.
15. The process of claim 1, wherein the feed stream is contacted with about 0.1 wt% to 30 wt% of the supported metal halide solid acid catalyst based on monomer weight in a batch reactor.
16. The process of claim 1, wherein the supported metal halide solid acid catalyst is added to the feed stream.
17. The process of claim 1, wherein the feed stream is added to a slurry of the supported metal halide solid acid catalyst in solvent.
18. The process of claim 1, wherein the feed stream is polymerized at a reaction temperature between about -50°C and 150°C.
19. The process of claim 1, wherein the feed stream comprises at least pure monomer, and wherein the hydrocarbon resin has a number average molecular weight (Mn) ranging from about 400 to 2000, a weight average molecular weight (Mw) ranging from about 500 to 5000, a Z average molecular weight (Mz) ranging from about 500 to 10,000, and a polydispersity (PD) as measured by Mw/Mn between about 1.2 and 3.5, where Mn, Mw, and Mz are determined by size exclusion chromatography (SEC).
20. The process of claim 1, wherein the feed stream comprises at least C5 monomers, and wherein the hydrocarbon resin has a number average molecular weight (Mn) of about 400 to 2000, a weight average molecular weight (Mw) of about 500 to 3500, a Z average molecular weight (Mz) of about 700 to 15,000, and a polydispersity (PD) as measured by Mw/Mn between about 1.2 and 5, where Mn, Mw, and Mz are determined by size exclusion chromatography (SEC).
21. The process of claim 1, wherein the feed stream comprises at least C9 monomers, and wherein the hydrocarbon resin has a number average molecular weight (Mn) of about 400 to 1200, a weight average molecular weight (Mw) of about 500 to 2000, a Z average molecular weight (Mz) of about 700 to 6000, and a polydispersity (PD) as measured by Mw/Mn between about 1.2 and 3.5, where Mn, Mw, and Mz are determined by size exclusion chromatography (SEC).
22. A process for making a hydrocarbon resin, comprising polymerizing a feed stream comprising at least one member selected from the group consisting of pure monomer, C5 monomers, and C9 monomers in the presence of ZrCl4 to produce a hydrocarbon resin, wherein the pure monomer comprises at least one member selected from the group consisting of styrene, alpha-methyl styrene, beta-methyl styrene, 4-methyl styrene, and vinyl toluene fractions, wherein the C5 monomers comprise at least one member selected from the group consisting of isobutylene, 2-methyl-2-butene, 2-methyl-2-pentene, 2-pentene, cyclopentene, cyclohexene, cyclopentadiene, and dicyclopentadiene, and wherein the C9 monomers comprise at least one member selected from the group consisting of styrene, vinyl toluene, indene, dicyclopentadiene, and alkylated derivatives thereof.
23. The process of claim 22, wherein the feed stream is contacted with about 0.1 wt% to 30 wt% of the supported metal halide solid acid catalyst based on monomer weight in a batch reactor.
24. The process of claim 22, wherein the supported metal halide solid acid catalyst is added to the feed stream.
25. The process of claim 22, wherein the feed stream is added to a slurry of the supported metal halide solid acid catalyst in solvent.
26. The process of claim 22, wherein the feed stream is polymerized at a reaction temperature between about -50°C and 150°C.
27. The process of claim 22, wherein the feed stream comprises at least pure monomer, and wherein the hydrocarbon resin has a number average molecular weight (Mn) ranging from about 400 to 2000, a weight average molecular weight (Mw) ranging from about 500 to 5000, a Z average molecular weight (Mz) ranging from about 500 to 10,000, and a polydispersity (PD) as measured by Mw/Mn between about 1.2 and 3.5, where Mn, Mw, and Mz are determined by size exclusion chromatography (SEC).
28. The process of claim 22, wherein the feed stream comprises at least C5 monomers, and wherein the hydrocarbon resin has a number average molecular weight (Mn) of about 400 to 2000, a weight average molecular weight (Mw) of about 500 to 3500, a Z average molecular weight (Mz) of about 700 to 15,000, and a polydispersity (PD) as measured by Mw/Mn between about 1.2 and 5, where Mn, Mw, and Mz are determined by size exclusion chromatography (SEC).
29. The process of claim 22, wherein the feed stream comprises at least C9 monomers, and wherein the hydrocarbon resin has a number average molecular weight (Mn) of about 400 to 1200, a weight average molecular weight (Mw) of about 500 to 2000, a Z average molecular weight (Mz) of about 700 to 6000, and a polydispersity (PD) as measured by Mw/Mn between about 1.2 and 3.5, where Mn, Mw, and Mz are determined by size exclusion chromatography (SEC).
Applications Claiming Priority (7)
Application Number | Priority Date | Filing Date | Title |
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US60/035,217 | 1997-01-08 | ||
US3457997P | 1997-01-09 | 1997-01-09 | |
US60/034,579 | 1997-01-09 | ||
US3579797P | 1997-01-10 | 1997-01-10 | |
US60/035,797 | 1997-01-10 | ||
PCT/US1998/000012 WO1998030587A2 (en) | 1997-01-08 | 1998-01-07 | Metal halide solid acids and supported metal halides as catalysts for the preparation of hydrocarbon resins |
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CA2277294A1 true CA2277294A1 (en) | 1998-07-16 |
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CA002277295A Abandoned CA2277295A1 (en) | 1997-01-08 | 1998-01-07 | Metal oxide solid acids as catalysts for the preparation of hydrocarbon resins |
CA002277292A Abandoned CA2277292A1 (en) | 1997-01-08 | 1998-01-07 | Solid acids as catalysts for the preparation of hydrocarbon resins |
CA002277294A Abandoned CA2277294A1 (en) | 1997-01-08 | 1998-01-07 | Metal halide solid acids and supported metal halides as catalysts for the preparation of hydrocarbon resins |
CA002277297A Abandoned CA2277297A1 (en) | 1997-01-08 | 1998-01-07 | Fluorinated solid acids as catalysts for the preparation of hydrocarbon resins |
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CA002277295A Abandoned CA2277295A1 (en) | 1997-01-08 | 1998-01-07 | Metal oxide solid acids as catalysts for the preparation of hydrocarbon resins |
CA002277292A Abandoned CA2277292A1 (en) | 1997-01-08 | 1998-01-07 | Solid acids as catalysts for the preparation of hydrocarbon resins |
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1998
- 1998-01-07 US US09/003,888 patent/US6133386A/en not_active Expired - Fee Related
- 1998-01-07 AU AU58133/98A patent/AU5813398A/en not_active Abandoned
- 1998-01-07 KR KR1019997006219A patent/KR20000070004A/en not_active Application Discontinuation
- 1998-01-07 JP JP53096498A patent/JP2001509185A/en active Pending
- 1998-01-07 EP EP98901669A patent/EP0964844B1/en not_active Expired - Lifetime
- 1998-01-07 EP EP98901668A patent/EP0954516A1/en not_active Withdrawn
- 1998-01-07 WO PCT/US1998/000009 patent/WO1998030519A1/en not_active Application Discontinuation
- 1998-01-07 AU AU57309/98A patent/AU5730998A/en not_active Abandoned
- 1998-01-07 DE DE69818018T patent/DE69818018T2/en not_active Expired - Fee Related
- 1998-01-07 US US09/003,879 patent/US6608155B2/en not_active Expired - Fee Related
- 1998-01-07 WO PCT/US1998/000011 patent/WO1998030521A1/en not_active Application Discontinuation
- 1998-01-07 US US09/003,596 patent/US6310154B1/en not_active Expired - Fee Related
- 1998-01-07 CA CA002277295A patent/CA2277295A1/en not_active Abandoned
- 1998-01-07 JP JP53096798A patent/JP2001508103A/en active Pending
- 1998-01-07 CA CA002277292A patent/CA2277292A1/en not_active Abandoned
- 1998-01-07 JP JP53096598A patent/JP2001508102A/en active Pending
- 1998-01-07 KR KR1019997006221A patent/KR20000070006A/en not_active Application Discontinuation
- 1998-01-07 KR KR1019997006222A patent/KR20000070007A/en not_active Application Discontinuation
- 1998-01-07 CA CA002277294A patent/CA2277294A1/en not_active Abandoned
- 1998-01-07 AU AU58134/98A patent/AU5813498A/en not_active Abandoned
- 1998-01-07 EP EP98901163A patent/EP0970117A2/en not_active Withdrawn
- 1998-01-07 CN CN98803202A patent/CN1249735A/en active Pending
- 1998-01-07 CA CA002277297A patent/CA2277297A1/en not_active Abandoned
- 1998-01-07 JP JP53096698A patent/JP2001511194A/en active Pending
- 1998-01-07 WO PCT/US1998/000012 patent/WO1998030587A2/en not_active Application Discontinuation
- 1998-01-07 CN CN98802978A patent/CN1249732A/en active Pending
- 1998-01-07 EP EP98901667A patent/EP0963365B1/en not_active Expired - Lifetime
- 1998-01-07 CN CN98803201A patent/CN1249734A/en active Pending
- 1998-01-07 CN CN98803007A patent/CN1249733A/en active Pending
- 1998-01-07 KR KR1019997006224A patent/KR20000070009A/en not_active Application Discontinuation
- 1998-01-07 US US09/003,594 patent/US6281309B1/en not_active Expired - Fee Related
- 1998-01-07 WO PCT/US1998/000010 patent/WO1998030520A1/en not_active Application Discontinuation
- 1998-01-07 AU AU58132/98A patent/AU5813298A/en not_active Abandoned
- 1998-01-07 DE DE69815301T patent/DE69815301T2/en not_active Expired - Fee Related
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