CA1267645A - Process and catalyst for the oligomerization of olefins - Google Patents
Process and catalyst for the oligomerization of olefinsInfo
- Publication number
- CA1267645A CA1267645A CA000509427A CA509427A CA1267645A CA 1267645 A CA1267645 A CA 1267645A CA 000509427 A CA000509427 A CA 000509427A CA 509427 A CA509427 A CA 509427A CA 1267645 A CA1267645 A CA 1267645A
- Authority
- CA
- Canada
- Prior art keywords
- catalyst
- set forth
- oligomerization
- composite
- group metal
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 120
- 238000006384 oligomerization reaction Methods 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 25
- 150000001336 alkenes Chemical class 0.000 title abstract description 25
- -1 alkyl aluminum compound Chemical class 0.000 claims abstract description 45
- 229910052751 metal Inorganic materials 0.000 claims abstract description 36
- 239000002184 metal Substances 0.000 claims abstract description 36
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical group [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 15
- 230000036571 hydration Effects 0.000 claims abstract description 10
- 238000006703 hydration reaction Methods 0.000 claims abstract description 10
- 239000002131 composite material Substances 0.000 claims description 50
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 35
- 229930195733 hydrocarbon Natural products 0.000 claims description 25
- 150000002430 hydrocarbons Chemical class 0.000 claims description 25
- 230000003197 catalytic effect Effects 0.000 claims description 19
- 238000006243 chemical reaction Methods 0.000 claims description 19
- 239000004215 Carbon black (E152) Substances 0.000 claims description 17
- 229910052759 nickel Inorganic materials 0.000 claims description 17
- 239000000203 mixture Substances 0.000 claims description 12
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 10
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 10
- 125000004432 carbon atom Chemical group C* 0.000 claims description 8
- LIKMAJRDDDTEIG-UHFFFAOYSA-N 1-hexene Chemical compound CCCCC=C LIKMAJRDDDTEIG-UHFFFAOYSA-N 0.000 claims description 6
- JMMZCWZIJXAGKW-UHFFFAOYSA-N 2-methylpent-2-ene Chemical compound CCC=C(C)C JMMZCWZIJXAGKW-UHFFFAOYSA-N 0.000 claims description 5
- KWKAKUADMBZCLK-UHFFFAOYSA-N 1-octene Chemical compound CCCCCCC=C KWKAKUADMBZCLK-UHFFFAOYSA-N 0.000 claims description 3
- WSSSPWUEQFSQQG-UHFFFAOYSA-N dimethylbutene Natural products CC(C)CC=C WSSSPWUEQFSQQG-UHFFFAOYSA-N 0.000 claims description 3
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 claims description 3
- WEPNJTDVIIKRIK-UHFFFAOYSA-N 2-methylhept-2-ene Chemical compound CCCCC=C(C)C WEPNJTDVIIKRIK-UHFFFAOYSA-N 0.000 claims description 2
- 229910017052 cobalt Inorganic materials 0.000 claims description 2
- 239000010941 cobalt Substances 0.000 claims description 2
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 2
- ILPBINAXDRFYPL-UHFFFAOYSA-N 2-octene Chemical compound CCCCCC=CC ILPBINAXDRFYPL-UHFFFAOYSA-N 0.000 claims 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 claims 1
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 45
- 239000002585 base Substances 0.000 description 36
- 239000000243 solution Substances 0.000 description 33
- 239000000047 product Substances 0.000 description 18
- YNLAOSYQHBDIKW-UHFFFAOYSA-M diethylaluminium chloride Chemical compound CC[Al](Cl)CC YNLAOSYQHBDIKW-UHFFFAOYSA-M 0.000 description 17
- 150000001875 compounds Chemical class 0.000 description 15
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 14
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 12
- 238000007792 addition Methods 0.000 description 12
- 235000010210 aluminium Nutrition 0.000 description 12
- 238000001354 calcination Methods 0.000 description 11
- 238000010438 heat treatment Methods 0.000 description 10
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 10
- 230000003213 activating effect Effects 0.000 description 9
- 239000000306 component Substances 0.000 description 9
- 239000000539 dimer Substances 0.000 description 9
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 9
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 7
- 229940063656 aluminum chloride Drugs 0.000 description 7
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 7
- 238000007669 thermal treatment Methods 0.000 description 7
- 239000002841 Lewis acid Substances 0.000 description 6
- 239000007864 aqueous solution Substances 0.000 description 6
- 239000007795 chemical reaction product Substances 0.000 description 6
- 150000007517 lewis acids Chemical class 0.000 description 6
- 239000003446 ligand Substances 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 6
- 150000003839 salts Chemical class 0.000 description 6
- 239000000377 silicon dioxide Substances 0.000 description 6
- 239000003638 chemical reducing agent Substances 0.000 description 5
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 5
- 238000005470 impregnation Methods 0.000 description 5
- 239000012299 nitrogen atmosphere Substances 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 230000002378 acidificating effect Effects 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 239000003960 organic solvent Substances 0.000 description 4
- 238000006116 polymerization reaction Methods 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000543 intermediate Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 229910044991 metal oxide Inorganic materials 0.000 description 3
- 150000004706 metal oxides Chemical class 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- 150000002816 nickel compounds Chemical class 0.000 description 3
- AOPCKOPZYFFEDA-UHFFFAOYSA-N nickel(2+);dinitrate;hexahydrate Chemical compound O.O.O.O.O.O.[Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O AOPCKOPZYFFEDA-UHFFFAOYSA-N 0.000 description 3
- 150000002902 organometallic compounds Chemical class 0.000 description 3
- 238000013021 overheating Methods 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 239000004014 plasticizer Substances 0.000 description 3
- 229920000642 polymer Polymers 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- IAQRGUVFOMOMEM-ONEGZZNKSA-N trans-but-2-ene Chemical compound C\C=C\C IAQRGUVFOMOMEM-ONEGZZNKSA-N 0.000 description 3
- 239000013638 trimer Substances 0.000 description 3
- CRSBERNSMYQZNG-UHFFFAOYSA-N 1-dodecene Chemical compound CCCCCCCCCCC=C CRSBERNSMYQZNG-UHFFFAOYSA-N 0.000 description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- KZMGYPLQYOPHEL-UHFFFAOYSA-N Boron trifluoride etherate Chemical compound FB(F)F.CCOCC KZMGYPLQYOPHEL-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- XYFCBTPGUUZFHI-UHFFFAOYSA-N Phosphine Chemical compound P XYFCBTPGUUZFHI-UHFFFAOYSA-N 0.000 description 2
- 230000002730 additional effect Effects 0.000 description 2
- 125000005234 alkyl aluminium group Chemical group 0.000 description 2
- 229910000323 aluminium silicate Inorganic materials 0.000 description 2
- 239000012298 atmosphere Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000005119 centrifugation Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000011437 continuous method Methods 0.000 description 2
- 238000010908 decantation Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 229940079593 drug Drugs 0.000 description 2
- 239000000975 dye Substances 0.000 description 2
- 239000000796 flavoring agent Substances 0.000 description 2
- 235000019634 flavors Nutrition 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- BMGNSKKZFQMGDH-FDGPNNRMSA-L nickel(2+);(z)-4-oxopent-2-en-2-olate Chemical compound [Ni+2].C\C([O-])=C\C(C)=O.C\C([O-])=C\C(C)=O BMGNSKKZFQMGDH-FDGPNNRMSA-L 0.000 description 2
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 2
- SPIFDSWFDKNERT-UHFFFAOYSA-N nickel;hydrate Chemical compound O.[Ni] SPIFDSWFDKNERT-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002304 perfume Substances 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000011949 solid catalyst Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 230000004580 weight loss Effects 0.000 description 2
- ZGEGCLOFRBLKSE-UHFFFAOYSA-N 1-Heptene Chemical class CCCCCC=C ZGEGCLOFRBLKSE-UHFFFAOYSA-N 0.000 description 1
- ADOQBZAVKYCFOI-UHFFFAOYSA-N 2-dodecene Chemical class CCCCCCCCCC=CC ADOQBZAVKYCFOI-UHFFFAOYSA-N 0.000 description 1
- CMAOLVNGLTWICC-UHFFFAOYSA-N 2-fluoro-5-methylbenzonitrile Chemical compound CC1=CC=C(F)C(C#N)=C1 CMAOLVNGLTWICC-UHFFFAOYSA-N 0.000 description 1
- SMDXUIYTBVHJNX-UHFFFAOYSA-N 2-methylundec-2-ene Chemical class CCCCCCCCC=C(C)C SMDXUIYTBVHJNX-UHFFFAOYSA-N 0.000 description 1
- XUKUURHRXDUEBC-KAYWLYCHSA-N Atorvastatin Chemical compound C=1C=CC=CC=1C1=C(C=2C=CC(F)=CC=2)N(CC[C@@H](O)C[C@@H](O)CC(O)=O)C(C(C)C)=C1C(=O)NC1=CC=CC=C1 XUKUURHRXDUEBC-KAYWLYCHSA-N 0.000 description 1
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 1
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229910021581 Cobalt(III) chloride Inorganic materials 0.000 description 1
- SNRUBQQJIBEYMU-UHFFFAOYSA-N Dodecane Natural products CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 description 1
- 108091035710 E-box Proteins 0.000 description 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 1
- 239000005909 Kieselgur Substances 0.000 description 1
- 229910021586 Nickel(II) chloride Inorganic materials 0.000 description 1
- 241000083552 Oligomeris Species 0.000 description 1
- 101710094173 Otefin Proteins 0.000 description 1
- 239000007868 Raney catalyst Substances 0.000 description 1
- 229910000564 Raney nickel Inorganic materials 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 1
- MQRWBMAEBQOWAF-UHFFFAOYSA-N acetic acid;nickel Chemical compound [Ni].CC(O)=O.CC(O)=O MQRWBMAEBQOWAF-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- CECABOMBVQNBEC-UHFFFAOYSA-K aluminium iodide Chemical compound I[Al](I)I CECABOMBVQNBEC-UHFFFAOYSA-K 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052796 boron Inorganic materials 0.000 description 1
- JKRAPJXEWBPBTP-UHFFFAOYSA-M bromo(dipropyl)alumane Chemical compound [Br-].CCC[Al+]CCC JKRAPJXEWBPBTP-UHFFFAOYSA-M 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000012876 carrier material Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 125000001309 chloro group Chemical group Cl* 0.000 description 1
- 125000004965 chloroalkyl group Chemical group 0.000 description 1
- XGRJZXREYAXTGV-UHFFFAOYSA-N chlorodiphenylphosphine Chemical compound C=1C=CC=CC=1P(Cl)C1=CC=CC=C1 XGRJZXREYAXTGV-UHFFFAOYSA-N 0.000 description 1
- 150000004700 cobalt complex Chemical class 0.000 description 1
- 229910000428 cobalt oxide Inorganic materials 0.000 description 1
- MPMSMUBQXQALQI-UHFFFAOYSA-N cobalt phthalocyanine Chemical compound [Co+2].C12=CC=CC=C2C(N=C2[N-]C(C3=CC=CC=C32)=N2)=NC1=NC([C]1C=CC=CC1=1)=NC=1N=C1[C]3C=CC=CC3=C2[N-]1 MPMSMUBQXQALQI-UHFFFAOYSA-N 0.000 description 1
- KTVIXTQDYHMGHF-UHFFFAOYSA-L cobalt(2+) sulfate Chemical compound [Co+2].[O-]S([O-])(=O)=O KTVIXTQDYHMGHF-UHFFFAOYSA-L 0.000 description 1
- BSUSEPIPTZNHMN-UHFFFAOYSA-L cobalt(2+);diperchlorate Chemical compound [Co+2].[O-]Cl(=O)(=O)=O.[O-]Cl(=O)(=O)=O BSUSEPIPTZNHMN-UHFFFAOYSA-L 0.000 description 1
- QAHREYKOYSIQPH-UHFFFAOYSA-L cobalt(II) acetate Chemical compound [Co+2].CC([O-])=O.CC([O-])=O QAHREYKOYSIQPH-UHFFFAOYSA-L 0.000 description 1
- YCYBZKSMUPTWEE-UHFFFAOYSA-L cobalt(ii) fluoride Chemical compound F[Co]F YCYBZKSMUPTWEE-UHFFFAOYSA-L 0.000 description 1
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical compound [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 description 1
- 229940000425 combination drug Drugs 0.000 description 1
- 230000002301 combined effect Effects 0.000 description 1
- 229940125890 compound Ia Drugs 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 150000001993 dienes Chemical class 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- JJSGABFIILQOEY-UHFFFAOYSA-M diethylalumanylium;bromide Chemical compound CC[Al](Br)CC JJSGABFIILQOEY-UHFFFAOYSA-M 0.000 description 1
- PPQUYYAZSOKTQD-UHFFFAOYSA-M diethylalumanylium;iodide Chemical compound CC[Al](I)CC PPQUYYAZSOKTQD-UHFFFAOYSA-M 0.000 description 1
- 238000006471 dimerization reaction Methods 0.000 description 1
- 230000000447 dimerizing effect Effects 0.000 description 1
- 125000000118 dimethyl group Chemical group [H]C([H])([H])* 0.000 description 1
- JGHYBJVUQGTEEB-UHFFFAOYSA-M dimethylalumanylium;chloride Chemical compound C[Al](C)Cl JGHYBJVUQGTEEB-UHFFFAOYSA-M 0.000 description 1
- CGGWHUZJDXLSTD-UHFFFAOYSA-M dimethylalumanylium;iodide Chemical compound C[Al](C)I CGGWHUZJDXLSTD-UHFFFAOYSA-M 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- ZMXPNWBFRPIZFV-UHFFFAOYSA-M dipropylalumanylium;chloride Chemical compound [Cl-].CCC[Al+]CCC ZMXPNWBFRPIZFV-UHFFFAOYSA-M 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 125000005843 halogen group Chemical group 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 150000004687 hexahydrates Chemical class 0.000 description 1
- 229920006158 high molecular weight polymer Polymers 0.000 description 1
- 150000004678 hydrides Chemical class 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 229910052809 inorganic oxide Inorganic materials 0.000 description 1
- TUAINSCBEUWUOI-UHFFFAOYSA-M iodo(dipropyl)alumane Chemical compound [I-].CCC[Al+]CCC TUAINSCBEUWUOI-UHFFFAOYSA-M 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000000314 lubricant Substances 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 150000002736 metal compounds Chemical class 0.000 description 1
- 229910001507 metal halide Inorganic materials 0.000 description 1
- 150000005673 monoalkenes Chemical class 0.000 description 1
- SYSQUGFVNFXIIT-UHFFFAOYSA-N n-[4-(1,3-benzoxazol-2-yl)phenyl]-4-nitrobenzenesulfonamide Chemical class C1=CC([N+](=O)[O-])=CC=C1S(=O)(=O)NC1=CC=C(C=2OC3=CC=CC=C3N=2)C=C1 SYSQUGFVNFXIIT-UHFFFAOYSA-N 0.000 description 1
- 229940078494 nickel acetate Drugs 0.000 description 1
- QMMRZOWCJAIUJA-UHFFFAOYSA-L nickel dichloride Chemical compound Cl[Ni]Cl QMMRZOWCJAIUJA-UHFFFAOYSA-L 0.000 description 1
- 229910000480 nickel oxide Inorganic materials 0.000 description 1
- UQPSGBZICXWIAG-UHFFFAOYSA-L nickel(2+);dibromide;trihydrate Chemical compound O.O.O.Br[Ni]Br UQPSGBZICXWIAG-UHFFFAOYSA-L 0.000 description 1
- DWAHIRJDCNGEDV-UHFFFAOYSA-N nickel(2+);dinitrate;hydrate Chemical compound O.[Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O DWAHIRJDCNGEDV-UHFFFAOYSA-N 0.000 description 1
- DBJLJFTWODWSOF-UHFFFAOYSA-L nickel(ii) fluoride Chemical compound F[Ni]F DBJLJFTWODWSOF-UHFFFAOYSA-L 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 230000003606 oligomerizing effect Effects 0.000 description 1
- 125000000962 organic group Chemical group 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- YWAKXRMUMFPDSH-UHFFFAOYSA-N pentene Chemical compound CCCC=C YWAKXRMUMFPDSH-UHFFFAOYSA-N 0.000 description 1
- QMMOXUPEWRXHJS-UHFFFAOYSA-N pentene-2 Natural products CCC=CC QMMOXUPEWRXHJS-UHFFFAOYSA-N 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 150000003018 phosphorus compounds Chemical class 0.000 description 1
- 229910000073 phosphorus hydride Inorganic materials 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- PUGUQINMNYINPK-UHFFFAOYSA-N tert-butyl 4-(2-chloroacetyl)piperazine-1-carboxylate Chemical compound CC(C)(C)OC(=O)N1CCN(C(=O)CCl)CC1 PUGUQINMNYINPK-UHFFFAOYSA-N 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
- 238000005829 trimerization reaction Methods 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
- 150000003738 xylenes Chemical class 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/74—Iron group metals
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
- B01J31/12—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing organo-metallic compounds or metal hydrides
- B01J31/14—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing organo-metallic compounds or metal hydrides of aluminium or boron
- B01J31/143—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing organo-metallic compounds or metal hydrides of aluminium or boron of aluminium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/26—Catalysts comprising hydrides, coordination complexes or organic compounds containing in addition, inorganic metal compounds not provided for in groups B01J31/02 - B01J31/24
- B01J31/28—Catalysts comprising hydrides, coordination complexes or organic compounds containing in addition, inorganic metal compounds not provided for in groups B01J31/02 - B01J31/24 of the platinum group metals, iron group metals or copper
- B01J31/30—Halides
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
- C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
- C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
- C07C2/08—Catalytic processes
- C07C2/26—Catalytic processes with hydrides or organic compounds
- C07C2/30—Catalytic processes with hydrides or organic compounds containing metal-to-carbon bond; Metal hydrides
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
- B01J2231/20—Olefin oligomerisation or telomerisation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/02—Boron or aluminium; Oxides or hydroxides thereof
- C07C2521/04—Alumina
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- C07C2521/08—Silica
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- C07C2527/06—Halogens; Compounds thereof
- C07C2527/125—Compounds comprising a halogen and scandium, yttrium, aluminium, gallium, indium or thallium
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2531/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- C07C2531/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
- C07C2531/12—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing organo-metallic compounds or metal hydrides
- C07C2531/14—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing organo-metallic compounds or metal hydrides of aluminium or boron
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2531/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- C07C2531/26—Catalysts comprising hydrides, coordination complexes or organic compounds containing in addition, inorganic metal compounds not provided for in groups C07C2531/02 - C07C2531/24
Abstract
"PROCESS AND CATALYST FOR THE
OLIGOMERIZATION OF OLEFINS"
ABSTRACT
Olefins are oligomerized to a desired oligomer by utilizing a catalyst which comrpises a porous support containing a catalytically effective amount of an iron group metal hydrate in which the mole ratio of water of hydration to iron group metal is greater than 0.5:1 in combination with a catalytically effective amount of an alkyl aluminum compound and and aluminum halide.
OLIGOMERIZATION OF OLEFINS"
ABSTRACT
Olefins are oligomerized to a desired oligomer by utilizing a catalyst which comrpises a porous support containing a catalytically effective amount of an iron group metal hydrate in which the mole ratio of water of hydration to iron group metal is greater than 0.5:1 in combination with a catalytically effective amount of an alkyl aluminum compound and and aluminum halide.
Description
~L~6~6~
; "PROCFSS AND CQTALYST FOR THE
;- OLIGOMERIZATION OF OLEFINS' BACKGROUND OF _HE INVENTION
The oligomerizat.on of olefins is known in the art, such oligo-merization processes being effected by treating olefinic hydrocarbons with certain catalysts to obtain various oligomers which will find a useful function in the chemical art. One type of catalyst which may be employed for this particular type of reaction comprises a supported metal compound.
For example, U.S. Patent 3,562,351 discloses a method for dimerizing ole-fins utilizing a supported catalyst which has been prepared by impregna-ting a suitable support with a salt solution of a Group VIII metal followed by a heat treatment in an inert atmosphere at a temperature less than that which is required to form a metal oxide but which will form a complex on the surface of the solid support. Following this, the catalyst is acti-vated by treatment with an organometallic compound. U.S. Patent 3,483,269 describes a catalyst useful for oligomerizing lower olefins which com-prises a ~r-allyl nickel halide supported on an acidic inorganic oxide support. If so desired, the support may have been optionally treated with an alkyl aluminum compound. U.S. Patent 3,592,869 also describes a cata-lyst which is useful for the oligomerization of olefins. A divalent nickel compound and an alkyl aluminum compound are contacted with an olefinic compound. The resulting mixture is then used to impregnate an inorganic refractory oxide support. Another patent, namely U.S. Patent 3,644,56~, describes a catalyst for the oligomerization of ethylene which comprises an organo aluminum-free reaction product of a nickel compound which is an atom of nickel in complex with an olefinically unsaturated compound and a fluorine-containing ligand. The catalysts are typically formed in situ.
U.S. Patent 3,679,772 describes a process for reacting monoolefins with diolefins, the catalyst for such a reaction comprising a complex of ~1) nickel, ~2) a Group VA electron donor ligand such as an organophosphine, (3) a nonprotonic Lewis acid and (4) a reducing agent which itself may be :
a Lewis acid, all of which are composited on an acidic silica-based sup-port.
U.S. Patent 3,697,617 describes an oligomerization process in-volving the use of a catalyst ~omprising a complex of nickel with a chlo-ro-containing electron donor ligand such as chlorodiphenylphosphine com-bined with a nonprotonic Lewis acid which is capable of forming a coordin-ation bond with nickel and a reducing agent capable of reducing nickel acetylacetonate to an oxidation state less than 2. This complex may be composited on a solid support comprising an acidic silica-based material such as silica alumina. The Lewis acid and the reducing agent may com-prise the same compound as, for example, ethyl aluminum sesqui chloride.
U.S. Patent 3,663,451 describes a catalyst which is obtained by reacting a transition metal halide such as nickel halide with a carrier to give a carrier-metal bond. This product is then reacted with a ligand such as a phosphine or ~ ketone and finally activated by treatment with an aluminum alkyl or chloro alkyl.
U.S. Patent 3,755,490 describes the polymerization of an olefin utilizing a catalyst comprising nickel, a Group VA electron donor ligand, a Lewis acid, and a reducing agent on a solid acidic silica-based support.
U.S. Patent 3,954,668 is drawn to an oligomerization catalyst comprising a nickel compound, a chloro-containing electron donor ligand, or a phos-phorous compound, a nonprotonic Lewis acid reducing agent which is capable of reducing nickel acetylacetonate to an oxidation s~ate of less than 2 and which is also capable of forming a coordination bond with a nickel.
U.S. Patent 3,170,904 speaks to a catalyst which is useful for polymeriza-tion comprising a large surface area metal of Groups VIIA or VIII of the Periodic Table, boron trifluoride etherate, an organometallic compound of Groups I, II, III or IV or a halo derivative of an organometallic compound of Groups II, III or IV or a hydride of a metal of Groups I, II or III.
The large surface area metal which comprises one component of this cata-lyst is in metallic form as, for example, Raney nickel. If so desired, the catalyst may be composited on a diatomaceous earth carrier. In like manner, U.S. Patent 3,170,904 discloses a catalyst which compr;ses (A) a ~6~
carrier-supported nickel or cobalt oxide which has been prepared by impreg-nating th~ carrier with the hydroxide, organic acid salt, inorganic acid salt, followed by oxidation in the presence of oxygen or a combination of nitrogen and oxygen; (B) a boron, titanium, zirconium, or vanadium ha-lide; and (C) an alkyl metal or alkyl metal halide. In addition to these patents, British Patent 1,390,530 describes an oligomerization catalyst which has been prepared by thermally pretreating a metal oxide carrier material followed by reacting with a halogen-containing organo-aluminum compound and thereafter in a step-wise fashion, impregnating this product -with a divalent nickel or cobalt complex at temperatures ranging from -50 to 150C.
As will hereinafter be shown in greater de~ail, the oligomeriza-tion of olefinic hydrocarbons may be accomplished by treating said olefins in the presence of a catalyst which has been prepared in a manner such ~5 that the catalyst will remain active and stable for a relatively long period of time and, in addition, will provide products which possess a de-sired configuration with respect to the branching or minimal branching oF
the chain.
BRIEF SUMMARY OF T~E INVENTION
This invention relates to a catalytic composite which is useful for the oligomerization of olefinic hydrocarbons. More specifically9 the invention is concerned with a catalyst composite and a process for the oligomerization of olefinic compounds, particularly olefinic hydrocarbons, whereby the use of the catalytic composite will result in the obtention of selective oligomers of the olefinic feed stock.
The term "polymerization" has a relatively broad meaning in the chemical art. Although it is generally referred to as the preparation of relatively high molecular weight polymers, that is polymers possessing molecular weights of greater than 50,000 or more, it may also refer ~o low molecular weight polymers9 that is, polymers possessing molecular weights lower than 50,000. In contradistinction to this, the term "oligomeriza-.
67~
tion" refers to polymeric compounds in which the molecules consist of only a r-elatively few monomeric units and thus would include dimerization, trimerization or tetramerization.
Many olefinic hydrocarbons which contain from 4 to about 12 car-bon atoms in the chain are utilized in various industries in many ways.
For example, dimers of propylene regardless of the amount of branching may be used to improve the octane number of motor fuels which are utilized in internal combustion engines utilizing gasoline as the fuel thereof. The presence of these compounds in a motor fuel such as gasoline will improve the octane number of the fuel to a high level, thus enabling the gasoline to be utilized in combustion engines in an unleaded state. Other uses For dimers containing 6 carbon atoms would be in the synthesis of flavors, per-fumes, medicines, dyes and resins. Another use of an oligomer would be found in the d;merization product of butene in which the dimer which pos-sesses a relatively straight chain configuration with a minimum of branch-ing such as one methyl substituent on the chain would be as an intermediate in the production of a plastici2er. The plasticizer, when added to a plastic will facilitate compounding and improve the flexibility as well as other properties of the finished product. Likewise, a trimer of butene or a dimer of hexene in which the olefin contains 12 carbon atoms may be used as an intermediate in various organic syntheses such as in the prep-aration of detergents, lubricants, additives, plasticizers, flavors, per-fumes, medicines, oils, dyes, etc. In addition, linearized oligomers con-taining 12 or more carbon atoms, upon hydrogenation, provide excellent diesel fuels.
It is therefore an object of this invention to provide a cata-lyst for the oligomerization of olefinic hydrocarbons.
A further object of this invention is to provide a specific cata-lyst system which may be used in a process for the oligomerization of olefinic hydrocarbons whereby selective oligomers may be obtained thereby.
In one aspect an embodiment of this invention resides in a cata-lytic composite comprising a combination of a catalytically effective ~ ~6 7~
amount o~ an alkyl aluminum compound on a porous support containing a cata-lytically effective amount of an iron group metal hydrate in which the mole ratio of water of hydration to iron group metal is greater than 0.5:1.
Another embodiment of this invention is found in a process for the oligomerization of an olefinic hydrocarbon which comprises treating said hydrocarbon in the presence of a catalyst comprising a combination of a catalytically effective amount of an alkyl aluminum compound composited on a porous support containing a catalytically effective amount of an iron group metal hydrate in which the mole ratio of water of hydration to iron group metal is greater than 0.5:1, at oligomerization conditions, and re-covering the resultant ol;gomer.
A specific embodiment of this invention is found in a catalytic composite comprising a combination of a catalytically effective amount of diethyl aluminum chloride on an alumina support which contains a catalyti-cally effective amount of nickel hydrate, the mole ratio of water of hy-dration to iron group metal being in a range o`f from about 0.5:1 to about 6:1 prior to reaction with said diethyl aluminum chloride, said diethyl aluminum chloride being present in a mole ratio in the range of from about 0.05:1 to about 6:1 moles of diethyl aluminum chloride per mole of nickel.
Another specific embodiment of this invention is found in the process for the oligomerization of an olefinic hydrocarbon which comprises treating propylene in the presence oFa catalyst comprising a combination of a catalytically effective amount of diethyl aluminum chloride on an alumina support wh;ch contains a catalytically effective amount of nickel hydrate, the mole ratio of water of hydration to iron group metal being in a range of from about 0.5:1 to about &:1 prior to reaction with said di-ethyl aluminum chloride, said diethyl aluminum chloride being present in a mole ratio in the range of from about 0.05:1 to about 6:1 moles of di-ethyl aluminum chloride per mole of nickel at a temperature in the range of from about -20 to about 120C and a pressure in the range of from about 350 to about ~O`O`Opsig t2410 to 6895 kPag), and recovering the resul-tant oligomer comprising a mixture of hexene, methylpentene and dimethyl-butene.
-pther objects and embodiments will be found in the following de-tailed description of the invention.
DETAILED D~SCRIPTION OF THE INVENTION
.
; As hereinbefore set forth, the present invention is concerned with a catalyst composite which may be utilized for the oligomerization of olefins and to a process which employs the catalyst. HeretofQre, the preparation of a catalytic composite which may be used for the polymeriza-tion or oligomerization of olefinic compounds was relatively difficult in-asmuch as several relatively expensive compounds were required as compo-nents of the composite. In contradistinction to this, the catalytic com-posite of the present invention is relatively easy to prepare and, in addi-tion, employs compounds which are less expensive than the components of the other catalyst. The final catalytic composite of the present invention will possess a high activity and will be stable over a relatively long period of time. In addition to these desired attributes, the catalyst will also produce a high yield of dimer products9 especially from C3 and C4 ole-fins as compared to trimer and tetramer products. The dimer products pro-duced by the oligomerization of propylene or the n-butenes will possess a high percentage of linear compounds, that is, n-hexenes and n-octenes and also a high percentage of dimers which contain only one methyl substituent;
more highly branched oligomers being minority products. The propylene di-mers which are produced by the process of the present invention all possess high octane numbers regardless of the branching, and thus are excellent octane blending components. In addition, the n-butene dimers are excellent as intermediates in the preparation of plasticizers.
; "PROCFSS AND CQTALYST FOR THE
;- OLIGOMERIZATION OF OLEFINS' BACKGROUND OF _HE INVENTION
The oligomerizat.on of olefins is known in the art, such oligo-merization processes being effected by treating olefinic hydrocarbons with certain catalysts to obtain various oligomers which will find a useful function in the chemical art. One type of catalyst which may be employed for this particular type of reaction comprises a supported metal compound.
For example, U.S. Patent 3,562,351 discloses a method for dimerizing ole-fins utilizing a supported catalyst which has been prepared by impregna-ting a suitable support with a salt solution of a Group VIII metal followed by a heat treatment in an inert atmosphere at a temperature less than that which is required to form a metal oxide but which will form a complex on the surface of the solid support. Following this, the catalyst is acti-vated by treatment with an organometallic compound. U.S. Patent 3,483,269 describes a catalyst useful for oligomerizing lower olefins which com-prises a ~r-allyl nickel halide supported on an acidic inorganic oxide support. If so desired, the support may have been optionally treated with an alkyl aluminum compound. U.S. Patent 3,592,869 also describes a cata-lyst which is useful for the oligomerization of olefins. A divalent nickel compound and an alkyl aluminum compound are contacted with an olefinic compound. The resulting mixture is then used to impregnate an inorganic refractory oxide support. Another patent, namely U.S. Patent 3,644,56~, describes a catalyst for the oligomerization of ethylene which comprises an organo aluminum-free reaction product of a nickel compound which is an atom of nickel in complex with an olefinically unsaturated compound and a fluorine-containing ligand. The catalysts are typically formed in situ.
U.S. Patent 3,679,772 describes a process for reacting monoolefins with diolefins, the catalyst for such a reaction comprising a complex of ~1) nickel, ~2) a Group VA electron donor ligand such as an organophosphine, (3) a nonprotonic Lewis acid and (4) a reducing agent which itself may be :
a Lewis acid, all of which are composited on an acidic silica-based sup-port.
U.S. Patent 3,697,617 describes an oligomerization process in-volving the use of a catalyst ~omprising a complex of nickel with a chlo-ro-containing electron donor ligand such as chlorodiphenylphosphine com-bined with a nonprotonic Lewis acid which is capable of forming a coordin-ation bond with nickel and a reducing agent capable of reducing nickel acetylacetonate to an oxidation state less than 2. This complex may be composited on a solid support comprising an acidic silica-based material such as silica alumina. The Lewis acid and the reducing agent may com-prise the same compound as, for example, ethyl aluminum sesqui chloride.
U.S. Patent 3,663,451 describes a catalyst which is obtained by reacting a transition metal halide such as nickel halide with a carrier to give a carrier-metal bond. This product is then reacted with a ligand such as a phosphine or ~ ketone and finally activated by treatment with an aluminum alkyl or chloro alkyl.
U.S. Patent 3,755,490 describes the polymerization of an olefin utilizing a catalyst comprising nickel, a Group VA electron donor ligand, a Lewis acid, and a reducing agent on a solid acidic silica-based support.
U.S. Patent 3,954,668 is drawn to an oligomerization catalyst comprising a nickel compound, a chloro-containing electron donor ligand, or a phos-phorous compound, a nonprotonic Lewis acid reducing agent which is capable of reducing nickel acetylacetonate to an oxidation s~ate of less than 2 and which is also capable of forming a coordination bond with a nickel.
U.S. Patent 3,170,904 speaks to a catalyst which is useful for polymeriza-tion comprising a large surface area metal of Groups VIIA or VIII of the Periodic Table, boron trifluoride etherate, an organometallic compound of Groups I, II, III or IV or a halo derivative of an organometallic compound of Groups II, III or IV or a hydride of a metal of Groups I, II or III.
The large surface area metal which comprises one component of this cata-lyst is in metallic form as, for example, Raney nickel. If so desired, the catalyst may be composited on a diatomaceous earth carrier. In like manner, U.S. Patent 3,170,904 discloses a catalyst which compr;ses (A) a ~6~
carrier-supported nickel or cobalt oxide which has been prepared by impreg-nating th~ carrier with the hydroxide, organic acid salt, inorganic acid salt, followed by oxidation in the presence of oxygen or a combination of nitrogen and oxygen; (B) a boron, titanium, zirconium, or vanadium ha-lide; and (C) an alkyl metal or alkyl metal halide. In addition to these patents, British Patent 1,390,530 describes an oligomerization catalyst which has been prepared by thermally pretreating a metal oxide carrier material followed by reacting with a halogen-containing organo-aluminum compound and thereafter in a step-wise fashion, impregnating this product -with a divalent nickel or cobalt complex at temperatures ranging from -50 to 150C.
As will hereinafter be shown in greater de~ail, the oligomeriza-tion of olefinic hydrocarbons may be accomplished by treating said olefins in the presence of a catalyst which has been prepared in a manner such ~5 that the catalyst will remain active and stable for a relatively long period of time and, in addition, will provide products which possess a de-sired configuration with respect to the branching or minimal branching oF
the chain.
BRIEF SUMMARY OF T~E INVENTION
This invention relates to a catalytic composite which is useful for the oligomerization of olefinic hydrocarbons. More specifically9 the invention is concerned with a catalyst composite and a process for the oligomerization of olefinic compounds, particularly olefinic hydrocarbons, whereby the use of the catalytic composite will result in the obtention of selective oligomers of the olefinic feed stock.
The term "polymerization" has a relatively broad meaning in the chemical art. Although it is generally referred to as the preparation of relatively high molecular weight polymers, that is polymers possessing molecular weights of greater than 50,000 or more, it may also refer ~o low molecular weight polymers9 that is, polymers possessing molecular weights lower than 50,000. In contradistinction to this, the term "oligomeriza-.
67~
tion" refers to polymeric compounds in which the molecules consist of only a r-elatively few monomeric units and thus would include dimerization, trimerization or tetramerization.
Many olefinic hydrocarbons which contain from 4 to about 12 car-bon atoms in the chain are utilized in various industries in many ways.
For example, dimers of propylene regardless of the amount of branching may be used to improve the octane number of motor fuels which are utilized in internal combustion engines utilizing gasoline as the fuel thereof. The presence of these compounds in a motor fuel such as gasoline will improve the octane number of the fuel to a high level, thus enabling the gasoline to be utilized in combustion engines in an unleaded state. Other uses For dimers containing 6 carbon atoms would be in the synthesis of flavors, per-fumes, medicines, dyes and resins. Another use of an oligomer would be found in the d;merization product of butene in which the dimer which pos-sesses a relatively straight chain configuration with a minimum of branch-ing such as one methyl substituent on the chain would be as an intermediate in the production of a plastici2er. The plasticizer, when added to a plastic will facilitate compounding and improve the flexibility as well as other properties of the finished product. Likewise, a trimer of butene or a dimer of hexene in which the olefin contains 12 carbon atoms may be used as an intermediate in various organic syntheses such as in the prep-aration of detergents, lubricants, additives, plasticizers, flavors, per-fumes, medicines, oils, dyes, etc. In addition, linearized oligomers con-taining 12 or more carbon atoms, upon hydrogenation, provide excellent diesel fuels.
It is therefore an object of this invention to provide a cata-lyst for the oligomerization of olefinic hydrocarbons.
A further object of this invention is to provide a specific cata-lyst system which may be used in a process for the oligomerization of olefinic hydrocarbons whereby selective oligomers may be obtained thereby.
In one aspect an embodiment of this invention resides in a cata-lytic composite comprising a combination of a catalytically effective ~ ~6 7~
amount o~ an alkyl aluminum compound on a porous support containing a cata-lytically effective amount of an iron group metal hydrate in which the mole ratio of water of hydration to iron group metal is greater than 0.5:1.
Another embodiment of this invention is found in a process for the oligomerization of an olefinic hydrocarbon which comprises treating said hydrocarbon in the presence of a catalyst comprising a combination of a catalytically effective amount of an alkyl aluminum compound composited on a porous support containing a catalytically effective amount of an iron group metal hydrate in which the mole ratio of water of hydration to iron group metal is greater than 0.5:1, at oligomerization conditions, and re-covering the resultant ol;gomer.
A specific embodiment of this invention is found in a catalytic composite comprising a combination of a catalytically effective amount of diethyl aluminum chloride on an alumina support which contains a catalyti-cally effective amount of nickel hydrate, the mole ratio of water of hy-dration to iron group metal being in a range o`f from about 0.5:1 to about 6:1 prior to reaction with said diethyl aluminum chloride, said diethyl aluminum chloride being present in a mole ratio in the range of from about 0.05:1 to about 6:1 moles of diethyl aluminum chloride per mole of nickel.
Another specific embodiment of this invention is found in the process for the oligomerization of an olefinic hydrocarbon which comprises treating propylene in the presence oFa catalyst comprising a combination of a catalytically effective amount of diethyl aluminum chloride on an alumina support wh;ch contains a catalytically effective amount of nickel hydrate, the mole ratio of water of hydration to iron group metal being in a range of from about 0.5:1 to about &:1 prior to reaction with said di-ethyl aluminum chloride, said diethyl aluminum chloride being present in a mole ratio in the range of from about 0.05:1 to about 6:1 moles of di-ethyl aluminum chloride per mole of nickel at a temperature in the range of from about -20 to about 120C and a pressure in the range of from about 350 to about ~O`O`Opsig t2410 to 6895 kPag), and recovering the resul-tant oligomer comprising a mixture of hexene, methylpentene and dimethyl-butene.
-pther objects and embodiments will be found in the following de-tailed description of the invention.
DETAILED D~SCRIPTION OF THE INVENTION
.
; As hereinbefore set forth, the present invention is concerned with a catalyst composite which may be utilized for the oligomerization of olefins and to a process which employs the catalyst. HeretofQre, the preparation of a catalytic composite which may be used for the polymeriza-tion or oligomerization of olefinic compounds was relatively difficult in-asmuch as several relatively expensive compounds were required as compo-nents of the composite. In contradistinction to this, the catalytic com-posite of the present invention is relatively easy to prepare and, in addi-tion, employs compounds which are less expensive than the components of the other catalyst. The final catalytic composite of the present invention will possess a high activity and will be stable over a relatively long period of time. In addition to these desired attributes, the catalyst will also produce a high yield of dimer products9 especially from C3 and C4 ole-fins as compared to trimer and tetramer products. The dimer products pro-duced by the oligomerization of propylene or the n-butenes will possess a high percentage of linear compounds, that is, n-hexenes and n-octenes and also a high percentage of dimers which contain only one methyl substituent;
more highly branched oligomers being minority products. The propylene di-mers which are produced by the process of the present invention all possess high octane numbers regardless of the branching, and thus are excellent octane blending components. In addition, the n-butene dimers are excellent as intermediates in the preparation of plasticizers.
2~ The catalytic composite of the present invention will comprise a combination of a catalytically effective amount of an alkyl aluminum com-pound on a porous support which contains a catalytically effective amount of an iron group metal hydrate. In addition, if so desired, the catalytic composite can also contain, in combination therewith, a catalytically ef-3n fective amount of an aluminum halide. In the preferred embodiment of the ~67~
invention, the iron group metal hydrate will be obtained from a soluble salt of nic;~el or cobalt such as, for example, nickel nitrate, nickel hydroxi~e, nickel bromide, nickel chloride, nickel fluoride, nickel ace-tate, cobaltic chloride, cobaltous acetate, cobaltous ammoni~m chloride, co-baltous bromide, cobaltous fluoride, cobaltous perchlorate, cobaltous sulfate,etc. The porous support upon which the iron group metal hydrate is im-pregnated will include inorganic metal oxides such as alumina, silica9 mix-tures of oxides such as alumina-silica, alumina-zirconia-magnesia, etc. or crystalline aluminosilicates which are commonly known as zeolites.
The other components of the catalytic composite will comprise alkyl aluminum compounds such as dimethyl aluminum chloride, diethyl alu-minum chloride, dipropyl aluminum chloride, dimethyl a1uminum bromidè, diethyl aluminum bromide, dipropyl aluminum bromide, dimethyl aluminum iodide, diethyl aluminum iodide, dipropyl aluminum iodide, etc. In addition, the aluminum halide which may be used to form a component of the catalytic composite in conjunction with the alkyl aluminum compound will include aluminum chloride, aluminum bromide, aluminum iodide, etc. It is to be understood that the aforementioned list of iron group metal compounds, porous supports, alkyl aluminum com-pounds and aluminum halides are only representative of the class of com-pounds which may be employed to form the catalytic composite of the pres-ent invention, and that said in~ention is not necessarily limited thereto.
The oligomerization catalyst of the present invention may be pre-pared in such a manner so as to provide the finished catalyst with certain characteristics with regard to the selectivity of olefins obtained by the reaction of an olefin in the presence of sa;d catalyst as well as a speci~
ficity of the product so obtained. The catalyst composite is prepared by impregnating a porous support of the type hereinbefore set forth with a simple divalent iron group metal salt such as, for example, nickel nitrate, ~2~;76~5 preferably from an aqueous solution. After impregnation of the porous sup-port such~as alumina, which is effected at ambient temperature and atmo-spheric pressure, the impregnated support is then subjected to a thermal treatment. By varying the temperature of the thermal treatment, it is pos-sible to obtain a catalyst composite which will provide a greater selec-tivity to dimer products resulting from the oligomerization of the olefin in contrast to trimer and tetramer products than are obtained when using other conventional oligomerization catalys~s. The thermal treatment of the impregnated support is preferably effected in a range of from about 350~ to about 450C, the preferred thermal treatment temperature being in a range of from about 340 to about 360C. The thermal treatment of the catalyst base containing the impregnated iron group metal salt in hydrate form will result in a weight loss due to a loss of water of hydration from the metal salt. In the preferred embodiment of the invention, the mole ratio of water of hydration to iron group metal following the thermal treatment will be greater than 0.5:1 and preferably in a range of from about 0.5:1 to about 6:1.
Following the thermal treatment, the iron group metal impreg-nated catalyst base is then treated with an alkyl aluminum compound where-in the activated solution will produce a catalyst of maximum activity.The treatment of the base with the activating agent is also effected at ambient temperature and atmospheric pressure utilizing a solution of the alkyl aluminum compound dissolved in an organic solvent such as benzene, toluene, the xylenes, etc. In the preferred embodiment of the invention, in addition to the alkyl aluminum compound which may be of the type herein-before set forth in greater detail, an aluminum halide compound may also be used in this step. The addition of the impregnated base to the organic solution will result in an exothermic reaction and after thorough admix-ture, the solution is allowed to return to room temperature. The solvent may then be removed by conventional means such as decantation~ evaporation7 etc. and the catalyst thereafter washed with an organic solvent to remove residue or trace portions of unwanted compounds. Thereafter, the catalyst ~L267~
may then he dried by purging with nitrogenl and recovered. In the fin-ished composite, the alkyl aluminum compound ia present in the composite in a mole ratio in the range of from about 0.05:1 to about 6:1, prefer-ably in a range of from about 0.1:1 to about 1:1, moles of alkyl aluminum compound per mole of iron group metal, the latter being present in said composite, on an elemental basis, in an amount in the range of from about 1% to about 20% by weight of the composite, and preferably in an amount in a range of from about 1% to about 10%.
As will hereinafter be shown in greater detail, by preparing a lo catalyst which possesses the various components in the finished composite in mole ratios or weight percent within the ranges hereinbefore set forth, it is possible to selectively oligomeri~e olefin compounds containing from about 2 to about 6 carbon atoms with a concurrent obtention of de-sirable isomers ~n each of the ol~gomer products. In addition, by ut;l-izing an aluminum halide as a component of the catalyst composite in addi-tion to the alkyl aluminum compound, it is possible to obtain a catalyst composite which will be more stable and more active in the conversion of olefins to oligomers than are catalysts which do not contain this com-POund .
As an example of how the catalyst composite of the present in-vention may be prepared, a predetermined amount of a porous base such as alumina, silica, silica-alumina, aluminosilicate, e~c. which may be in the form of spheres, pellets, rods, etc. may be prepared in an appropriate apparatus such as an evaporator along with an aqueous solution of a hy-drated salt of an iron group metal. The mixture may be thoroughly admixed and following this~ the apparatus heated to form the desired iron group metal impregnated base. The impregnated base may then be placed in a heating apparatus such as a tube furnace and treated with air while bring-ing the catalyst to a temperature of about 250~C. The heating is accom-plished at a relatively slow rate and after the determined temperature has been reached, it is maintained thereat for an additional period of time which may range from about 2 to about 4 hours or more in duration. The - `
~2~i7~
calcination of the catalyst base is then effected by increasing the tem-perature to a predetermined level and maintaining thereat for a period of time su fficient to bring the mole ratio of water of hydration present in the iron group metal salt to a determined level which is preFerably in an excess of about 5:1 moles of water of hydration per mole of iron group metal.
After allo~ing the calcination to pro~eed for this predetermined period of time, heating is discontinued and the catalyst base which con-tains from about 1% to about 20% by weight of iron group metal is allowed to cool. The cooled base may then be admixed with a solution of an alkyl aluminum compound and an aluminum halide dissolved in an organic solvent.
As previously discussed, the resulting reaction is exothermic in nature and after allowing the heat to dissipate, the resulting admixture is thor-oughly stirred and allowed to stand for a period of time which may range from about 1 to about 100 hours or more in duration. At the end of this period, the organic solvent is removed by decantation, filtration, cen-trifugation, etc. and the solid catalyst is washed to remove any unreacted material. After washing, the catalyst is then dried in an inert atmo-sphere such as that provided for by the presence of nitrogen, and recovered.
The oligomerization of olefins containing from 2 to about 6 car-bon atoms such as ethylene, propylene, butene-l, butene-2, pentene-1, pentene-2, pentene-3 may then be effected by treating the ole~in in the presence of the catalyst at oligomerization conditions which will include a temperature in the range of from about -20C to about 120C, the pre-ferred range being from about 30 to about 80C, and a pressure in the range of from about 350 to about 1000 psig (2410 to 6895 kPag).
The pressure which is utilized may be the autogenous pressure provided for by the feedstock, if in gaseous phase, or, the feedstock may supply only a partial pressure, the remainder of said pressure being provided by the introduction of an inert gas such as nitrogen, helium, argon, etc. into the reaction zone.
It is conte~plated within the scope of this invention that the oligomerization process may be effected in either a batch or continuous type operation. For example, when a batch type operation is employed, a quantity; of the novel catalyst composite of the present invention mav be placed in an appropriate apparatus such as, for example, an autoclave of the rotating, mixing or stirring type. If the olefinic feedstock is in gaseous form, the autDclave is sealed and the feedstock comprising the olefinic hydrocarbon or a mixture of olefinic and paraffinic hydrocarbon or similar carbon atom length are charged to the reactor until the de-sired operating pressure has been attained. The apparatus is then heated to the desired operating temperature and maintained thereat for a prede-termined period of time which may range from about 1 to about 6 hours or~ore in duration. At the end of this period of time, heating is discon-tinued and after the apparatus and contents thereof have returned to room temperature, the excess pressure is discharged and the autoclave is opened. The reaction product is recovered, separated from the catalyst by conventional means such as decantationl filtratlon, centrifugation, etc.
and, if so desired, subjected to fract;onal distillation whereby the vari-ous isomers may be separated, one from another, and stored. Conversely, if so desired, the reaction product comprising a mixture of isomers may ; be recovered and stored per se without separating the various isomeric fractions which are present in the product mixture.
In the event that the olefinic charge stock is in liquid form, it may be charged to the reactor which is thereafter sealed and pressured to the desired operating pressure by the introduction of an inert gas of the type hereinbefore set forth. The remainder of the operating pressure to obtain the desired oligomer product is carried out in a manner similar to that previously described.
When utilizing a continuous method of operation to obtain the desired oligomer products, a quantity of the catalyst composite is placed in an appropriate apparatus. The feedstock comprising the olefinic com-pound is continuously charged to this reactor which is maintained at theproper operating conditions of temperature and pressure. As in the case of the batch type operation, the desired operating pressure may be pro-~2~i7~
vided for by the olefinic hydrocarbon itself or by the addition of a heated ine~t gas. After passage through the reactor for a predetermined period of time, the reactor effluent is continuously discharged and the reaction product may be recovered and passed to storage or it may be passed to a distillation apparatus whereby separation of the various iso-mers and oligomers may be effected. Any unreacted olefinic hydrocarbon which is recovered from the reactor effluent may be recycled back to the reactor to form a portion of the feed charge.
Inasmuch as the catalyst composite of the present invention is in solid form, the continuous method of operation for obtaining the de-sired oligomers of the olefinic hydrocarbons may be effected in various types of operations. For example, in one type of operation, the catalyst is positioned as a fixed bed in the reaction zone and the olefinic feed-stock is charged so that it passes over the catalyst bed in either an up-ward or downward flow. Another type of continuous operation which may be employed comprises the moving bed type of operation in which the catalyst bed and the feedstock are passed through the reaction zone either concur-rently or countercurrently to each other. In addition to the fixed or moving bed type of operation, it is also contemplated that the slurry type of operation may be employed, especially when the olefinic hydrocar-bon feedstock is in liquid form. When this type of operation is employed, the catalyst is charged to the reactor as a slurry in the olefinic feed-stock.
Examples of oligomers of olefinic compounds which may be ob-tained when utilizing the catalyst composite of the present invention will include n-butene, isobutene, n-hexene, methyl pentene, dimethyl butene, _-octene, the isomeric heptenes, dimethyl hexenes, n-dodecene, the isomeric methyl undecenes, dimethyl decenes, etc. As was previously stated, the oligomer products which are obtained in the process of this invention will comprise, in the main, the dimers of the particular olefinic compound which was employed as the feedstock, thus, for example, when employing ethylene as the feed, the reaction product will comprise mostly ~4 olefins;
when employing propylene as the feedstock, the reaction product will com-~2~7Ç~
prise mostly C6 olefins; and when employing butene as the feedstock, the reaction ~roduct will comprise mostly C8 olefins. Thus, the catalyst composite of the present invention will result in products which find particular uses in the finished product.
The following examples are given for purposes of illustrating the novel catalyst composites of the present invention9 methods for pre-paring these composites and a process for utilizing these composites.
However, it is to be understood that these examples are merely illustra-tive in nature and that the present invention is not necessarily limited thereto.
EXAMPLE I
A catalyst was prepared by impregnating 250 cc of alumina spheres with an aqueous solution of 250 cc of water containing 34.6 grams of nickel nitrate hexahydrate. The impregnation was effected in a rotary evaporator in which the mixture was rolled for a period of 0.5 hours with no heat.
The evaporator was then heated with steam for a period of two hours at which time the water phase was evaporated. The catalyst base was then loaded into a tube furnace and air was passed through the catalyst bed at a rate of 600 cc per minute. Following this, the temperature of the bed was raised to 2~0C during a period of two hours and thereafter the bed was maintained at this temperature for an additional period of three hours.
At the end of this time, the bed was allowed to cool to room temperature and thereafter the bed was calcined by raising the temperature to 400C
during a two-hour period. The 400C calcination temperature was maintained for an additional period of three hours following which heating was dis-2~ continued and the impregnated base was recovered.
An activating solution was prepared by adding 3.91 grams of an-hydrous aluminum chloride to 174 cc of toluene in a 500 cc flask along with 18 grams of diethyl aluminum chloride as a S0 weight percent solution in toluene. The addition ~f the solutions was accomplished in a glove box while maintaining a nitrogen atmosphere for the addition. After thorough admixture, 67~
the solution was allowed to stand for a period of 3.5 hours with intermit-tent swirl;ing thereof.
The impregnated base was placed in a 500 cc flask along with 240 cc of toluene. The activating solution containing the aluminum chlo-~ 5 ride and diethyl aluminum chloride was slowly added during a period of 15 ; minutes to avoid overheating of the catalyst due to the exothermic nature of the reaction. After addition of the activating solution to the sup-port, the resulting solution was slightly warm with a concurrent emission of some gas bubbles. The solution was allowed to stand for a period of 18.5 hours at the end of which time thP impregnated liquors were decanted and the catalyst was washed with six portions of isopentane utilizing 100 to 115 cc per wash. The resulting catalyst compos;te was then allowed to dry in a glove box under nitrogen atmosphere until it became free-flowing.
This catalyst was designated as "A."
EXAMPLE II
A second catalyst composite was prepared in a manner similar to that set forth in Example I above. The catalyst base comprised 250 cc of alumina containing 5% by weight of nickel, said impregnated base again be-ing calcined at a temperature of 400C. The catalyst support was placed in a ~00 cc ftask along with 250 cc of toluene. A solution prepared in a manner similar to that set forth in Example I above from 18 grams of diethyl aluminum chloride as a 50 weight percent solution in toluene and 174 cc of toluene (no aluminum chloride being present) was slowly added during a period of 15 minutes to prevent overheating of the catalyst.
Again, it was noted that the solution was slightly warm following the addi-tion with the evolution of some gas bubbles. The solution was again al-lowed to stand for a period of 18.5 hours following which the impregnation liquors were decanted and the solid catalyst washed with six portions of isopentane using 115 to 120 cc per wash. This catalyst was then allowed to dry in a glove box under nitrogen until it was free-flowing in nature.
The catalyst was designated as "B."
~ Z~ t~3 EXAMPLE III
;- ~he catalysts prepared according to the methods set forth in Ex-amples I and II above were utilized in the oligomerization of butene-l.
The oligomerization was effected by placing 100 cc of l;he catalysts in a tubular reactor having an outside diameter of 0.5". A feedstock compris-ing a mixture of 60% butene-l and 40% n-butane was charged to the reac-tor at a LHSV of 1.0 hours 1 based upon the otefin. Reaction conditions which were employed for the oligomerization included a reactor inlet tem-perature of 35C and a pressure of 700 psig ~4827 kPag). The oligomerization was allowed to proceed for a period of 100 hours, samples being taken and analyzed at various points during the react;on period. The results of these analyses are set forth in Table 1 below:
Table 1 -Catalyst A Catalyst B
Unreacted Olefin %
Hours - ~8 11.5 12.5 31.5 12.0 - 32.5 100 13.0 37.5 Butene Conversion %
EXAMPLE IV
To illustrate the difference in selectivity factors which may be obtained by calcining the impregnated catalyst base at various tempera-tures, three different catalysts were prepared. The calcination of the alumina base was effected in a manner similar to that set forth in Example
invention, the iron group metal hydrate will be obtained from a soluble salt of nic;~el or cobalt such as, for example, nickel nitrate, nickel hydroxi~e, nickel bromide, nickel chloride, nickel fluoride, nickel ace-tate, cobaltic chloride, cobaltous acetate, cobaltous ammoni~m chloride, co-baltous bromide, cobaltous fluoride, cobaltous perchlorate, cobaltous sulfate,etc. The porous support upon which the iron group metal hydrate is im-pregnated will include inorganic metal oxides such as alumina, silica9 mix-tures of oxides such as alumina-silica, alumina-zirconia-magnesia, etc. or crystalline aluminosilicates which are commonly known as zeolites.
The other components of the catalytic composite will comprise alkyl aluminum compounds such as dimethyl aluminum chloride, diethyl alu-minum chloride, dipropyl aluminum chloride, dimethyl a1uminum bromidè, diethyl aluminum bromide, dipropyl aluminum bromide, dimethyl aluminum iodide, diethyl aluminum iodide, dipropyl aluminum iodide, etc. In addition, the aluminum halide which may be used to form a component of the catalytic composite in conjunction with the alkyl aluminum compound will include aluminum chloride, aluminum bromide, aluminum iodide, etc. It is to be understood that the aforementioned list of iron group metal compounds, porous supports, alkyl aluminum com-pounds and aluminum halides are only representative of the class of com-pounds which may be employed to form the catalytic composite of the pres-ent invention, and that said in~ention is not necessarily limited thereto.
The oligomerization catalyst of the present invention may be pre-pared in such a manner so as to provide the finished catalyst with certain characteristics with regard to the selectivity of olefins obtained by the reaction of an olefin in the presence of sa;d catalyst as well as a speci~
ficity of the product so obtained. The catalyst composite is prepared by impregnating a porous support of the type hereinbefore set forth with a simple divalent iron group metal salt such as, for example, nickel nitrate, ~2~;76~5 preferably from an aqueous solution. After impregnation of the porous sup-port such~as alumina, which is effected at ambient temperature and atmo-spheric pressure, the impregnated support is then subjected to a thermal treatment. By varying the temperature of the thermal treatment, it is pos-sible to obtain a catalyst composite which will provide a greater selec-tivity to dimer products resulting from the oligomerization of the olefin in contrast to trimer and tetramer products than are obtained when using other conventional oligomerization catalys~s. The thermal treatment of the impregnated support is preferably effected in a range of from about 350~ to about 450C, the preferred thermal treatment temperature being in a range of from about 340 to about 360C. The thermal treatment of the catalyst base containing the impregnated iron group metal salt in hydrate form will result in a weight loss due to a loss of water of hydration from the metal salt. In the preferred embodiment of the invention, the mole ratio of water of hydration to iron group metal following the thermal treatment will be greater than 0.5:1 and preferably in a range of from about 0.5:1 to about 6:1.
Following the thermal treatment, the iron group metal impreg-nated catalyst base is then treated with an alkyl aluminum compound where-in the activated solution will produce a catalyst of maximum activity.The treatment of the base with the activating agent is also effected at ambient temperature and atmospheric pressure utilizing a solution of the alkyl aluminum compound dissolved in an organic solvent such as benzene, toluene, the xylenes, etc. In the preferred embodiment of the invention, in addition to the alkyl aluminum compound which may be of the type herein-before set forth in greater detail, an aluminum halide compound may also be used in this step. The addition of the impregnated base to the organic solution will result in an exothermic reaction and after thorough admix-ture, the solution is allowed to return to room temperature. The solvent may then be removed by conventional means such as decantation~ evaporation7 etc. and the catalyst thereafter washed with an organic solvent to remove residue or trace portions of unwanted compounds. Thereafter, the catalyst ~L267~
may then he dried by purging with nitrogenl and recovered. In the fin-ished composite, the alkyl aluminum compound ia present in the composite in a mole ratio in the range of from about 0.05:1 to about 6:1, prefer-ably in a range of from about 0.1:1 to about 1:1, moles of alkyl aluminum compound per mole of iron group metal, the latter being present in said composite, on an elemental basis, in an amount in the range of from about 1% to about 20% by weight of the composite, and preferably in an amount in a range of from about 1% to about 10%.
As will hereinafter be shown in greater detail, by preparing a lo catalyst which possesses the various components in the finished composite in mole ratios or weight percent within the ranges hereinbefore set forth, it is possible to selectively oligomeri~e olefin compounds containing from about 2 to about 6 carbon atoms with a concurrent obtention of de-sirable isomers ~n each of the ol~gomer products. In addition, by ut;l-izing an aluminum halide as a component of the catalyst composite in addi-tion to the alkyl aluminum compound, it is possible to obtain a catalyst composite which will be more stable and more active in the conversion of olefins to oligomers than are catalysts which do not contain this com-POund .
As an example of how the catalyst composite of the present in-vention may be prepared, a predetermined amount of a porous base such as alumina, silica, silica-alumina, aluminosilicate, e~c. which may be in the form of spheres, pellets, rods, etc. may be prepared in an appropriate apparatus such as an evaporator along with an aqueous solution of a hy-drated salt of an iron group metal. The mixture may be thoroughly admixed and following this~ the apparatus heated to form the desired iron group metal impregnated base. The impregnated base may then be placed in a heating apparatus such as a tube furnace and treated with air while bring-ing the catalyst to a temperature of about 250~C. The heating is accom-plished at a relatively slow rate and after the determined temperature has been reached, it is maintained thereat for an additional period of time which may range from about 2 to about 4 hours or more in duration. The - `
~2~i7~
calcination of the catalyst base is then effected by increasing the tem-perature to a predetermined level and maintaining thereat for a period of time su fficient to bring the mole ratio of water of hydration present in the iron group metal salt to a determined level which is preFerably in an excess of about 5:1 moles of water of hydration per mole of iron group metal.
After allo~ing the calcination to pro~eed for this predetermined period of time, heating is discontinued and the catalyst base which con-tains from about 1% to about 20% by weight of iron group metal is allowed to cool. The cooled base may then be admixed with a solution of an alkyl aluminum compound and an aluminum halide dissolved in an organic solvent.
As previously discussed, the resulting reaction is exothermic in nature and after allowing the heat to dissipate, the resulting admixture is thor-oughly stirred and allowed to stand for a period of time which may range from about 1 to about 100 hours or more in duration. At the end of this period, the organic solvent is removed by decantation, filtration, cen-trifugation, etc. and the solid catalyst is washed to remove any unreacted material. After washing, the catalyst is then dried in an inert atmo-sphere such as that provided for by the presence of nitrogen, and recovered.
The oligomerization of olefins containing from 2 to about 6 car-bon atoms such as ethylene, propylene, butene-l, butene-2, pentene-1, pentene-2, pentene-3 may then be effected by treating the ole~in in the presence of the catalyst at oligomerization conditions which will include a temperature in the range of from about -20C to about 120C, the pre-ferred range being from about 30 to about 80C, and a pressure in the range of from about 350 to about 1000 psig (2410 to 6895 kPag).
The pressure which is utilized may be the autogenous pressure provided for by the feedstock, if in gaseous phase, or, the feedstock may supply only a partial pressure, the remainder of said pressure being provided by the introduction of an inert gas such as nitrogen, helium, argon, etc. into the reaction zone.
It is conte~plated within the scope of this invention that the oligomerization process may be effected in either a batch or continuous type operation. For example, when a batch type operation is employed, a quantity; of the novel catalyst composite of the present invention mav be placed in an appropriate apparatus such as, for example, an autoclave of the rotating, mixing or stirring type. If the olefinic feedstock is in gaseous form, the autDclave is sealed and the feedstock comprising the olefinic hydrocarbon or a mixture of olefinic and paraffinic hydrocarbon or similar carbon atom length are charged to the reactor until the de-sired operating pressure has been attained. The apparatus is then heated to the desired operating temperature and maintained thereat for a prede-termined period of time which may range from about 1 to about 6 hours or~ore in duration. At the end of this period of time, heating is discon-tinued and after the apparatus and contents thereof have returned to room temperature, the excess pressure is discharged and the autoclave is opened. The reaction product is recovered, separated from the catalyst by conventional means such as decantationl filtratlon, centrifugation, etc.
and, if so desired, subjected to fract;onal distillation whereby the vari-ous isomers may be separated, one from another, and stored. Conversely, if so desired, the reaction product comprising a mixture of isomers may ; be recovered and stored per se without separating the various isomeric fractions which are present in the product mixture.
In the event that the olefinic charge stock is in liquid form, it may be charged to the reactor which is thereafter sealed and pressured to the desired operating pressure by the introduction of an inert gas of the type hereinbefore set forth. The remainder of the operating pressure to obtain the desired oligomer product is carried out in a manner similar to that previously described.
When utilizing a continuous method of operation to obtain the desired oligomer products, a quantity of the catalyst composite is placed in an appropriate apparatus. The feedstock comprising the olefinic com-pound is continuously charged to this reactor which is maintained at theproper operating conditions of temperature and pressure. As in the case of the batch type operation, the desired operating pressure may be pro-~2~i7~
vided for by the olefinic hydrocarbon itself or by the addition of a heated ine~t gas. After passage through the reactor for a predetermined period of time, the reactor effluent is continuously discharged and the reaction product may be recovered and passed to storage or it may be passed to a distillation apparatus whereby separation of the various iso-mers and oligomers may be effected. Any unreacted olefinic hydrocarbon which is recovered from the reactor effluent may be recycled back to the reactor to form a portion of the feed charge.
Inasmuch as the catalyst composite of the present invention is in solid form, the continuous method of operation for obtaining the de-sired oligomers of the olefinic hydrocarbons may be effected in various types of operations. For example, in one type of operation, the catalyst is positioned as a fixed bed in the reaction zone and the olefinic feed-stock is charged so that it passes over the catalyst bed in either an up-ward or downward flow. Another type of continuous operation which may be employed comprises the moving bed type of operation in which the catalyst bed and the feedstock are passed through the reaction zone either concur-rently or countercurrently to each other. In addition to the fixed or moving bed type of operation, it is also contemplated that the slurry type of operation may be employed, especially when the olefinic hydrocar-bon feedstock is in liquid form. When this type of operation is employed, the catalyst is charged to the reactor as a slurry in the olefinic feed-stock.
Examples of oligomers of olefinic compounds which may be ob-tained when utilizing the catalyst composite of the present invention will include n-butene, isobutene, n-hexene, methyl pentene, dimethyl butene, _-octene, the isomeric heptenes, dimethyl hexenes, n-dodecene, the isomeric methyl undecenes, dimethyl decenes, etc. As was previously stated, the oligomer products which are obtained in the process of this invention will comprise, in the main, the dimers of the particular olefinic compound which was employed as the feedstock, thus, for example, when employing ethylene as the feed, the reaction product will comprise mostly ~4 olefins;
when employing propylene as the feedstock, the reaction product will com-~2~7Ç~
prise mostly C6 olefins; and when employing butene as the feedstock, the reaction ~roduct will comprise mostly C8 olefins. Thus, the catalyst composite of the present invention will result in products which find particular uses in the finished product.
The following examples are given for purposes of illustrating the novel catalyst composites of the present invention9 methods for pre-paring these composites and a process for utilizing these composites.
However, it is to be understood that these examples are merely illustra-tive in nature and that the present invention is not necessarily limited thereto.
EXAMPLE I
A catalyst was prepared by impregnating 250 cc of alumina spheres with an aqueous solution of 250 cc of water containing 34.6 grams of nickel nitrate hexahydrate. The impregnation was effected in a rotary evaporator in which the mixture was rolled for a period of 0.5 hours with no heat.
The evaporator was then heated with steam for a period of two hours at which time the water phase was evaporated. The catalyst base was then loaded into a tube furnace and air was passed through the catalyst bed at a rate of 600 cc per minute. Following this, the temperature of the bed was raised to 2~0C during a period of two hours and thereafter the bed was maintained at this temperature for an additional period of three hours.
At the end of this time, the bed was allowed to cool to room temperature and thereafter the bed was calcined by raising the temperature to 400C
during a two-hour period. The 400C calcination temperature was maintained for an additional period of three hours following which heating was dis-2~ continued and the impregnated base was recovered.
An activating solution was prepared by adding 3.91 grams of an-hydrous aluminum chloride to 174 cc of toluene in a 500 cc flask along with 18 grams of diethyl aluminum chloride as a S0 weight percent solution in toluene. The addition ~f the solutions was accomplished in a glove box while maintaining a nitrogen atmosphere for the addition. After thorough admixture, 67~
the solution was allowed to stand for a period of 3.5 hours with intermit-tent swirl;ing thereof.
The impregnated base was placed in a 500 cc flask along with 240 cc of toluene. The activating solution containing the aluminum chlo-~ 5 ride and diethyl aluminum chloride was slowly added during a period of 15 ; minutes to avoid overheating of the catalyst due to the exothermic nature of the reaction. After addition of the activating solution to the sup-port, the resulting solution was slightly warm with a concurrent emission of some gas bubbles. The solution was allowed to stand for a period of 18.5 hours at the end of which time thP impregnated liquors were decanted and the catalyst was washed with six portions of isopentane utilizing 100 to 115 cc per wash. The resulting catalyst compos;te was then allowed to dry in a glove box under nitrogen atmosphere until it became free-flowing.
This catalyst was designated as "A."
EXAMPLE II
A second catalyst composite was prepared in a manner similar to that set forth in Example I above. The catalyst base comprised 250 cc of alumina containing 5% by weight of nickel, said impregnated base again be-ing calcined at a temperature of 400C. The catalyst support was placed in a ~00 cc ftask along with 250 cc of toluene. A solution prepared in a manner similar to that set forth in Example I above from 18 grams of diethyl aluminum chloride as a 50 weight percent solution in toluene and 174 cc of toluene (no aluminum chloride being present) was slowly added during a period of 15 minutes to prevent overheating of the catalyst.
Again, it was noted that the solution was slightly warm following the addi-tion with the evolution of some gas bubbles. The solution was again al-lowed to stand for a period of 18.5 hours following which the impregnation liquors were decanted and the solid catalyst washed with six portions of isopentane using 115 to 120 cc per wash. This catalyst was then allowed to dry in a glove box under nitrogen until it was free-flowing in nature.
The catalyst was designated as "B."
~ Z~ t~3 EXAMPLE III
;- ~he catalysts prepared according to the methods set forth in Ex-amples I and II above were utilized in the oligomerization of butene-l.
The oligomerization was effected by placing 100 cc of l;he catalysts in a tubular reactor having an outside diameter of 0.5". A feedstock compris-ing a mixture of 60% butene-l and 40% n-butane was charged to the reac-tor at a LHSV of 1.0 hours 1 based upon the otefin. Reaction conditions which were employed for the oligomerization included a reactor inlet tem-perature of 35C and a pressure of 700 psig ~4827 kPag). The oligomerization was allowed to proceed for a period of 100 hours, samples being taken and analyzed at various points during the react;on period. The results of these analyses are set forth in Table 1 below:
Table 1 -Catalyst A Catalyst B
Unreacted Olefin %
Hours - ~8 11.5 12.5 31.5 12.0 - 32.5 100 13.0 37.5 Butene Conversion %
EXAMPLE IV
To illustrate the difference in selectivity factors which may be obtained by calcining the impregnated catalyst base at various tempera-tures, three different catalysts were prepared. The calcination of the alumina base was effected in a manner similar to that set forth in Example
3~;2676`'~
I above utilizing a nickel nitrate hydrate solution which resulted in a base containin~ 5~0 by weight of nickel. After drying the impregnated base at a tempe~ature of 250C for a period of three hours, the base was then cal-cined by raising the temperature at which each base was calcined to dif-ferent levels. After calcining the bases at the different temperatures, the bases were then treated with an activating solution of diethyl alu-minum chloride and aluminum chloride in a manner also similar in nature to that set forth in Example I above to prepare the three ~inished catalyst composites.
The three catalyst bases were calcined at temperatures of 350, lD 400, and 450C respectively, the finished catalyst composites which re-sulted from the use of these bases being labeled C, D and E respectively.
The finished catalyst composites were then utilized in an oligomerization reaction involving a feedstock comprising 60% butene-2 and 400~ n-butane, said reaction being effected at a reactant inlet temDerature of 70C, a pressure of 700 psig (4827 kPag) and an olefin LHSV of 0.6 for C and 1.0 for D
and E hrs. 1.
The weight loss which each catalyst base underwent during the calcination period as well as the selectivity to isomeric octenes at a conversion rate of 50% of the butene-2 are set forth in Table 2 below:
Table 2 2D Catalyst C D E
Calcination Temp. C 350 400 450 Wt. Loss % 2.9 1.5 0.8 C8 = Selectivity 88 76 54 It is apparent from the above Table that the temperature at which the impregnated catalyst base is calcined will have an effect upon the se-lectivity of the olefin oligomerization process, the lower calcination temperature providing the greatest percentage of selectivity.
In like manner, it is also evident from the results obtained 3~ when using two catalysts, one of which did not contain an aluminum halide as one component thereof, that a catalyst co~posite comprising a combina-tion of a catalytically effective amount of an alkyl aluminum compound and an aluminum halide on a porous support which contains a catalytically effective amount of an iron group metal hydrate will result in obtaining a greater amount of oligomer than will be obtained when ut;lizing a cata-lyst which does not contain the aforesaid aluminum halide.
EXAMPLE V
An oligomerization catalyst was prepared by impregnating 250 cc of alumina spheres with an aqueous solution of 250 cc of water containing 34.6 grams of nickel nitrate hexahydrate. The impregnation was effected 1~ in a rotary evaporator in which the mixture was rolled for a period of 0.5 hours without heating, followed by heating with steam for a period of two hours at which time the water was evaporated. The catalyst base was then calcined in a manner set forth in the above example by loading into a tube furnace, heating to 250C for a period of two hours, cooling to room tem-perature followed by raising the temperature to 400DC and maintaining the temperature for a period of three hours.
An activating solution was prepared by adding 1.5 grams of an-hydrous aluminum chloride to 62 grams of toluene in a S00 cc flask along with 5.45 grams of diethyl aluminum chloride in 33 cc of hexane. The addi-tion of the solutions was effected in a glove box wh;le maintaining a nitrogen atmosphere and after thorough admixture, the solution was allowed to stand for a period of 3.5 hours.
To prepare the desired catalyst, 125 cc of the catalyst base was placed in a 500 cc flask along with 125 cc of toluene. The act;vator solution was then slowly added to the catalyst base over a period of 30 minutes in order to avoid overheating. The solution was warm and in addi-tion, gas bubbles were formed after the addition. After allowing the sol-ution to stand for a period of 18 hours, the solvents were decanted and the catalyst was washed with six 80 cc portions o~ isopentane. The cata-lyst composite was allowed to dry in a glo~e box under a nitrogen atmo-~z~
sphere and designated as "F."
EXAMPLE VI
In this example, 250 cc of alumina spheres were impregnated with an aqueous solution of 250 cc of water containing 34.6 grams of nickel ni-trate hexahydrate in a manner similar to that set forth in Example V above.
The catalyst base was then divided into six separate portions, loaded into a tube furnace, and treated in a manner similar to that set forth in the above example by calcining at a temperature of 400C for a period of three hours.
Six batches of activating solution were prepared by adding 3.9 grams of anhydrous aluminum chloride and 16.9 grams of diethyl aluminum chloride as a 50 wt. % solution and 39 cc of toluene to 174 cc of toluene.
The mixing was effected in a glove box under a nitrogen atmosphere and after 3.5 hours all of the solid had dissolved. Each batch of the solu-tion was used to activate the six 250 cc catalyst bases prepared accord-ing to the above paragraph. Each portion of the catalyst base was placed in a 500 cc flask along with 250 cc of toluene, the addition of the acti-~ator solution being accomplished over a 15 minute period. After allo~-ing the solution to stand for a period of 18.5 hours, the solvent was decanted and each catalyst was washed with six 100-115 cc portions of iso-pentane. Thereafter, the catalyst portions were allowed to dry in a glove box under nitrogen and combined, this catalyst being designated "G."
EXAMPLE VII
To vary the ratio of nickel to aluminum halide, a catalyst was prepared by impregnating 250 cc of alumina spheres with an aqueous solu-tion comprising 250 cc of water containing 71.3 grams o~ nickel nitrate hexahydrate. After impregnation, the catalyst base was treated in a man-ner similar to that hereinbefore set ~orth and loaded into a tube furnace during which air was passed through the catalyst bed at a rate of 600 cc per minute. Following this, the temperature of the bed was raised to ~2676~5 250~C du~ing a period of two hours and maintained thereat for an addi-tional period of three hours. At the end of this time, the bed was al-lowed to cool to room temperature and thereafter, the catalyst was cal-cined by raising the temperature of the furnace to 350~C during a two-hour period. The 350C calcination temperature was maintained for an addi-tional period of two hours following which heating was discontinued and the impregnated base was recovered.
An activating solution was prepared by adding 5.87 grams of an-hydrous aluminum chloride to 80 cc of toluene in a 500 cc flask along with 58.1 cc of a 50 wt. % diethyl aluminum chloride in a toluene solution ~27.0 grams of diethyl aluminum chloride). A portion (125 cc) of the im-pregnated catalyst base was then placed in a 500 cc flask along with 120 cc of toluene. The activating solution was slowly added during a period of 15 minutes and allowed to stand for 18.5 hours. At the end of th;s time, the impregnating liquors were decanted and the catalyst was washed with six portions of isopentane utilizing 100 to 115 cc per wash. The catalyst com-posite was allowed to dry in a glove box under a nitrogen atmosphere until it became free-flowing, this catalyst being designated ~F.
EXAMPLE VIII
Catalysts F, G and H which were prepared according to the above examples were used in a propylene oligomerizatiDn test. Each catalyst in an amount of 50 cc was placed in a tube reactor and a charge comprising 90% by weight of propylene and 10% by weight of propane was charged to each reactor at olefin Liquid Hourly Space Velocities ranging from 2.0 to 3.0 hours 1. The reactors were maintained at a pressure of 700 psig (4827 kPag) while the bath temperatures were maintained at from 35D to 50~C. A fract;onation column was used to separate unreacted C3's from the oligomers and a portion of the unreacted C3's (both propylene and propane) was recycled to the reactor inlet. The results of the runs are set forth in Table 3 below:
~2~i7~
Table 3 ;
Catalyst "F''Catalyst "G" Catal~st l'H"
Run Length (hrs.) 1385 1042 36 Overall Propylene 88.7 - 99.8 92.6 - 99.9 61.3 - 91.7 Conversion (wt.%) 5 C - selectivity 70.7 - 81.5 77.4 - 92.6 6 (wt. %) Research Octane No. 95 - 96 95 - 96 Motor Octane No. 80 - 81 80 - 81
I above utilizing a nickel nitrate hydrate solution which resulted in a base containin~ 5~0 by weight of nickel. After drying the impregnated base at a tempe~ature of 250C for a period of three hours, the base was then cal-cined by raising the temperature at which each base was calcined to dif-ferent levels. After calcining the bases at the different temperatures, the bases were then treated with an activating solution of diethyl alu-minum chloride and aluminum chloride in a manner also similar in nature to that set forth in Example I above to prepare the three ~inished catalyst composites.
The three catalyst bases were calcined at temperatures of 350, lD 400, and 450C respectively, the finished catalyst composites which re-sulted from the use of these bases being labeled C, D and E respectively.
The finished catalyst composites were then utilized in an oligomerization reaction involving a feedstock comprising 60% butene-2 and 400~ n-butane, said reaction being effected at a reactant inlet temDerature of 70C, a pressure of 700 psig (4827 kPag) and an olefin LHSV of 0.6 for C and 1.0 for D
and E hrs. 1.
The weight loss which each catalyst base underwent during the calcination period as well as the selectivity to isomeric octenes at a conversion rate of 50% of the butene-2 are set forth in Table 2 below:
Table 2 2D Catalyst C D E
Calcination Temp. C 350 400 450 Wt. Loss % 2.9 1.5 0.8 C8 = Selectivity 88 76 54 It is apparent from the above Table that the temperature at which the impregnated catalyst base is calcined will have an effect upon the se-lectivity of the olefin oligomerization process, the lower calcination temperature providing the greatest percentage of selectivity.
In like manner, it is also evident from the results obtained 3~ when using two catalysts, one of which did not contain an aluminum halide as one component thereof, that a catalyst co~posite comprising a combina-tion of a catalytically effective amount of an alkyl aluminum compound and an aluminum halide on a porous support which contains a catalytically effective amount of an iron group metal hydrate will result in obtaining a greater amount of oligomer than will be obtained when ut;lizing a cata-lyst which does not contain the aforesaid aluminum halide.
EXAMPLE V
An oligomerization catalyst was prepared by impregnating 250 cc of alumina spheres with an aqueous solution of 250 cc of water containing 34.6 grams of nickel nitrate hexahydrate. The impregnation was effected 1~ in a rotary evaporator in which the mixture was rolled for a period of 0.5 hours without heating, followed by heating with steam for a period of two hours at which time the water was evaporated. The catalyst base was then calcined in a manner set forth in the above example by loading into a tube furnace, heating to 250C for a period of two hours, cooling to room tem-perature followed by raising the temperature to 400DC and maintaining the temperature for a period of three hours.
An activating solution was prepared by adding 1.5 grams of an-hydrous aluminum chloride to 62 grams of toluene in a S00 cc flask along with 5.45 grams of diethyl aluminum chloride in 33 cc of hexane. The addi-tion of the solutions was effected in a glove box wh;le maintaining a nitrogen atmosphere and after thorough admixture, the solution was allowed to stand for a period of 3.5 hours.
To prepare the desired catalyst, 125 cc of the catalyst base was placed in a 500 cc flask along with 125 cc of toluene. The act;vator solution was then slowly added to the catalyst base over a period of 30 minutes in order to avoid overheating. The solution was warm and in addi-tion, gas bubbles were formed after the addition. After allowing the sol-ution to stand for a period of 18 hours, the solvents were decanted and the catalyst was washed with six 80 cc portions o~ isopentane. The cata-lyst composite was allowed to dry in a glo~e box under a nitrogen atmo-~z~
sphere and designated as "F."
EXAMPLE VI
In this example, 250 cc of alumina spheres were impregnated with an aqueous solution of 250 cc of water containing 34.6 grams of nickel ni-trate hexahydrate in a manner similar to that set forth in Example V above.
The catalyst base was then divided into six separate portions, loaded into a tube furnace, and treated in a manner similar to that set forth in the above example by calcining at a temperature of 400C for a period of three hours.
Six batches of activating solution were prepared by adding 3.9 grams of anhydrous aluminum chloride and 16.9 grams of diethyl aluminum chloride as a 50 wt. % solution and 39 cc of toluene to 174 cc of toluene.
The mixing was effected in a glove box under a nitrogen atmosphere and after 3.5 hours all of the solid had dissolved. Each batch of the solu-tion was used to activate the six 250 cc catalyst bases prepared accord-ing to the above paragraph. Each portion of the catalyst base was placed in a 500 cc flask along with 250 cc of toluene, the addition of the acti-~ator solution being accomplished over a 15 minute period. After allo~-ing the solution to stand for a period of 18.5 hours, the solvent was decanted and each catalyst was washed with six 100-115 cc portions of iso-pentane. Thereafter, the catalyst portions were allowed to dry in a glove box under nitrogen and combined, this catalyst being designated "G."
EXAMPLE VII
To vary the ratio of nickel to aluminum halide, a catalyst was prepared by impregnating 250 cc of alumina spheres with an aqueous solu-tion comprising 250 cc of water containing 71.3 grams o~ nickel nitrate hexahydrate. After impregnation, the catalyst base was treated in a man-ner similar to that hereinbefore set ~orth and loaded into a tube furnace during which air was passed through the catalyst bed at a rate of 600 cc per minute. Following this, the temperature of the bed was raised to ~2676~5 250~C du~ing a period of two hours and maintained thereat for an addi-tional period of three hours. At the end of this time, the bed was al-lowed to cool to room temperature and thereafter, the catalyst was cal-cined by raising the temperature of the furnace to 350~C during a two-hour period. The 350C calcination temperature was maintained for an addi-tional period of two hours following which heating was discontinued and the impregnated base was recovered.
An activating solution was prepared by adding 5.87 grams of an-hydrous aluminum chloride to 80 cc of toluene in a 500 cc flask along with 58.1 cc of a 50 wt. % diethyl aluminum chloride in a toluene solution ~27.0 grams of diethyl aluminum chloride). A portion (125 cc) of the im-pregnated catalyst base was then placed in a 500 cc flask along with 120 cc of toluene. The activating solution was slowly added during a period of 15 minutes and allowed to stand for 18.5 hours. At the end of th;s time, the impregnating liquors were decanted and the catalyst was washed with six portions of isopentane utilizing 100 to 115 cc per wash. The catalyst com-posite was allowed to dry in a glove box under a nitrogen atmosphere until it became free-flowing, this catalyst being designated ~F.
EXAMPLE VIII
Catalysts F, G and H which were prepared according to the above examples were used in a propylene oligomerizatiDn test. Each catalyst in an amount of 50 cc was placed in a tube reactor and a charge comprising 90% by weight of propylene and 10% by weight of propane was charged to each reactor at olefin Liquid Hourly Space Velocities ranging from 2.0 to 3.0 hours 1. The reactors were maintained at a pressure of 700 psig (4827 kPag) while the bath temperatures were maintained at from 35D to 50~C. A fract;onation column was used to separate unreacted C3's from the oligomers and a portion of the unreacted C3's (both propylene and propane) was recycled to the reactor inlet. The results of the runs are set forth in Table 3 below:
~2~i7~
Table 3 ;
Catalyst "F''Catalyst "G" Catal~st l'H"
Run Length (hrs.) 1385 1042 36 Overall Propylene 88.7 - 99.8 92.6 - 99.9 61.3 - 91.7 Conversion (wt.%) 5 C - selectivity 70.7 - 81.5 77.4 - 92.6 6 (wt. %) Research Octane No. 95 - 96 95 - 96 Motor Octane No. 80 - 81 80 - 81
Claims (14)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A catalytic composite comprising d combination of a cata-lytically effective amount of an alkyl aluminum compound on a porous sup-port containing a catalytically effective amount of an iron group metal hydrate in which the mole ratio of water of hydration to iron group metal is greater than 0.5:1.
2. The catalytic composite as set forth in Claim 1 further characterized in that said composite contains in combination therewith a catalytically effective amount of an aluminum halide.
3. The catalytic composite as set forth in Claim 1 in which said iron group metal is present in said composite, on an elemental basis, in an amount in the range of from about 1% to about 20% by weight of said composite.
4. The catalytic composite as set forth in Claim 1 in which said alkyl aluminum compound is present in said composite in a mole ratio in the range of from about 0.05:1 to about 6:1 moles of alkyl aluminum compound per mole of iron group metal.
5. The catalytic composite as set forth in Claim 1 in which the mole ratio of water of hydration to iron group metal in said iron group metal hydrate is in a range of from about 0.5:1 to about 6:1 prior to reaction with said alkyl aluminum compound.
6. The catalytic composite as set forth in Claim 3 in which said iron group metal is nickel or cobalt.
7. The catalytic composite as set forth in Claim 1 in which said alkyl aluminum compound comprises an alkyl aluminum halide.
8. A process for the oligomerization of an olefinic hydrocar-bon which comprises treating said hydrocarbon in the presence of the cata-lyst of Claim 1 at oligomerization conditions and recovering the resultant oligomer.
9. The process as set forth in Claim 8 in which said oligo-merization conditions include a temperature in the range of from about -20° to about 120°C and a pressure in the range of from about 350 to about 1000 psig (2410 to 6895 kPag).
10. The process as set forth in Claim 8 in which said ole-finic hydrocarbon contains from 2 to about 6 carbon atoms.
11. The process as set forth in Claim 8 in which said ole-finic hydrocarbon is propylene and said oligomer is a mixture of hexene, methyl hentene and dimethyl butene.
12. The process as set forth in Claim 8 in which said ole-finic hydrocarbon is butylene and said oligomer is a mixture of octene, methyl heptene and dimethyl hexene.
13. A process for the oligomerization of an olefinic hydrocarbon which comprises treating said hydrocarbon in the presence of the catalyst of Claim 2, 3 or 4 at oligomerization conditions and recovering the resultant oligomer.
14. A process for the oligomerization of an olefinic hydrocarbon which comprises treating said hydrocarbon in the presence of the catalyst of Claim 5, 6 or 7 at oligomerization conditions and recovering the resultant oligomer.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US06/737,320 US4613580A (en) | 1985-05-23 | 1985-05-23 | Process for the oligomerization of olefins and a catalyst thereof |
US737,320 | 1985-05-23 |
Publications (1)
Publication Number | Publication Date |
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CA1267645A true CA1267645A (en) | 1990-04-10 |
Family
ID=24963443
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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CA000509427A Expired - Fee Related CA1267645A (en) | 1985-05-23 | 1986-05-16 | Process and catalyst for the oligomerization of olefins |
Country Status (14)
Country | Link |
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US (1) | US4613580A (en) |
EP (1) | EP0202670B1 (en) |
JP (1) | JPS61278355A (en) |
KR (1) | KR890002861B1 (en) |
CN (1) | CN1003912B (en) |
AR (1) | AR241478A1 (en) |
AT (1) | ATE55279T1 (en) |
AU (1) | AU577695B2 (en) |
BR (1) | BR8602344A (en) |
CA (1) | CA1267645A (en) |
DE (1) | DE3673238D1 (en) |
EG (1) | EG18249A (en) |
FI (1) | FI862163A (en) |
ZA (1) | ZA863716B (en) |
Families Citing this family (14)
Publication number | Priority date | Publication date | Assignee | Title |
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US4737480A (en) * | 1986-03-25 | 1988-04-12 | Uop Inc. | Process for the oligomerization of olefins and a catalyst thereof |
EP0333940A1 (en) * | 1988-03-17 | 1989-09-27 | Uop Inc. | Process and catalyst for the oligomerization of olefins |
AU598114B2 (en) * | 1986-03-25 | 1990-06-14 | Uop Inc. | Process and catalyst for the oligomerization of olefins |
JPH01242150A (en) * | 1988-03-18 | 1989-09-27 | Uop Inc | Method and catalyst for oligomerization of olefin |
US5324799A (en) * | 1990-03-06 | 1994-06-28 | Akihiro Yano | Polyethylene and process of production thereof |
KR910018412A (en) * | 1990-04-16 | 1991-11-30 | 야마구찌 도시아끼 | Method for producing polyolefin |
DE4339713A1 (en) * | 1993-11-22 | 1995-05-24 | Basf Ag | Process for oligomerization of olefins to highly linear oligomers and catalysts therefor |
US5561095A (en) * | 1994-03-31 | 1996-10-01 | Exxon Chemical Patents Inc. | Supported lewis acid catalysts for hydrocarbon conversion reactions |
KR19990056183A (en) * | 1997-12-29 | 1999-07-15 | 정몽혁 | Low Olefin Low Polymerization Catalyst |
US8604260B2 (en) * | 2010-05-18 | 2013-12-10 | Kior, Inc. | Biomass pyrolysis conversion process with high olefin production and upgrade |
CN104001546A (en) * | 2014-06-09 | 2014-08-27 | 浙江科技学院 | Supported catalyst for preparing hexa-olefin by dimerization of propylene and preparation method of supported catalyst |
US10882028B2 (en) * | 2018-03-14 | 2021-01-05 | Evonik Operations Gmbh | Ni-containing catalyst for the oligomerization of olefins |
CN108479792B (en) * | 2018-03-23 | 2020-10-13 | 安徽理工大学 | Microwave-assisted catalyst for preparing high-carbon olefin by using alumina as carrier and catalytic process |
CN110935434A (en) * | 2019-12-09 | 2020-03-31 | 北京石油化工学院 | Catalyst for preparing nonene and dodecene by propylene oligomerization and preparation method and application thereof |
Family Cites Families (20)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3170904A (en) * | 1959-11-28 | 1965-02-23 | Bridgestone Tire Co Ltd | Production of cis-1, 4 polybutadiene with a ni-bf3 etherate-air3 catalyst |
US3354235A (en) * | 1963-10-28 | 1967-11-21 | Phillips Petroleum Co | Olefin polymerization with a supported nickel oxide catalyst and an organometal compound |
US3736308A (en) * | 1965-02-20 | 1973-05-29 | Showa Denko Kk | Method for the preparation of polyepoxides by polymerizing 1,2-epoxides by the use of a novel catalyst |
FR1540270A (en) * | 1966-11-15 | 1968-09-27 | Inst Francais Du Petrole | Olefin dimerization process |
BE789431Q (en) * | 1966-11-15 | 1973-03-29 | Inst Francais Du Petrole | DIMERIZATION AND CODIMERIZATION PROCESS |
US3483269A (en) * | 1967-09-27 | 1969-12-09 | Shell Oil Co | Olefin oligomerization |
US3562351A (en) * | 1967-11-16 | 1971-02-09 | Exxon Research Engineering Co | Dimerization process |
GB1240731A (en) * | 1968-01-31 | 1971-07-28 | Ici Ltd | Process for the manufacture of aliphatic diamines |
US3592869A (en) * | 1968-10-03 | 1971-07-13 | Shell Oil Co | Olefin oligomerization |
GB1256913A (en) * | 1969-01-30 | 1971-12-15 | ||
US3755490A (en) * | 1969-05-01 | 1973-08-28 | Atlantic Richfield Co | Olefin polymerization catalyzed by a supported black amorphous nickelcomplex |
FR2041668A5 (en) * | 1969-05-20 | 1971-01-29 | Inst Francais Du Petrole | |
US3679772A (en) * | 1969-08-04 | 1972-07-25 | Atlantic Richfield Co | Chemical process |
US3697617A (en) * | 1969-08-25 | 1972-10-10 | Atlantic Richfield Co | Oligomerization process |
US4000211A (en) * | 1969-10-29 | 1976-12-28 | Phillips Petroleum Company | Dimerization of monoolefins with catalysts on solid supports |
US3644564A (en) * | 1969-12-19 | 1972-02-22 | Shell Oil Co | Ethylene oligomerization in the presence of complex nickel-fluorine-containing catalysts |
US3954668A (en) * | 1972-05-30 | 1976-05-04 | Atlantic Richfield Company | Nickel containing olefin oligomerization catalyst |
GB1390530A (en) * | 1972-11-02 | 1975-04-16 | Akad Wissenschaften Ddr | Oligomerisation and co-oligomerisation catalysts |
US4176086A (en) * | 1977-08-25 | 1979-11-27 | Phillips Petroleum Company | Catalyst preparation |
JPS61151136A (en) * | 1984-12-25 | 1986-07-09 | Mitsui Petrochem Ind Ltd | Process for oligomerization of olefin |
-
1985
- 1985-05-23 US US06/737,320 patent/US4613580A/en not_active Expired - Fee Related
-
1986
- 1986-05-16 CA CA000509427A patent/CA1267645A/en not_active Expired - Fee Related
- 1986-05-19 ZA ZA863716A patent/ZA863716B/en unknown
- 1986-05-21 EP EP86106899A patent/EP0202670B1/en not_active Expired - Lifetime
- 1986-05-21 DE DE8686106899T patent/DE3673238D1/en not_active Expired - Fee Related
- 1986-05-21 AT AT86106899T patent/ATE55279T1/en active
- 1986-05-22 BR BR8602344A patent/BR8602344A/en unknown
- 1986-05-22 AU AU57813/86A patent/AU577695B2/en not_active Ceased
- 1986-05-22 AR AR86304056A patent/AR241478A1/en active
- 1986-05-22 FI FI862163A patent/FI862163A/en not_active Application Discontinuation
- 1986-05-22 EG EG304/86A patent/EG18249A/en active
- 1986-05-23 CN CN86103976.9A patent/CN1003912B/en not_active Expired
- 1986-05-23 KR KR1019860004022A patent/KR890002861B1/en not_active IP Right Cessation
- 1986-05-23 JP JP61119004A patent/JPS61278355A/en active Pending
Also Published As
Publication number | Publication date |
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JPS61278355A (en) | 1986-12-09 |
FI862163A (en) | 1986-11-24 |
US4613580A (en) | 1986-09-23 |
KR890002861B1 (en) | 1989-08-05 |
EP0202670A3 (en) | 1987-11-19 |
FI862163A0 (en) | 1986-05-22 |
AU5781386A (en) | 1986-11-27 |
ATE55279T1 (en) | 1990-08-15 |
DE3673238D1 (en) | 1990-09-13 |
ZA863716B (en) | 1986-12-30 |
KR860008799A (en) | 1986-12-18 |
CN86103976A (en) | 1987-03-04 |
BR8602344A (en) | 1987-01-21 |
AU577695B2 (en) | 1988-09-29 |
AR241478A1 (en) | 1992-07-31 |
EG18249A (en) | 1992-12-30 |
EP0202670A2 (en) | 1986-11-26 |
EP0202670B1 (en) | 1990-08-08 |
CN1003912B (en) | 1989-04-19 |
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