AU5190486A - Cracking catalysts and process using mixed catalyst systems - Google Patents
Cracking catalysts and process using mixed catalyst systemsInfo
- Publication number
- AU5190486A AU5190486A AU51904/86A AU5190486A AU5190486A AU 5190486 A AU5190486 A AU 5190486A AU 51904/86 A AU51904/86 A AU 51904/86A AU 5190486 A AU5190486 A AU 5190486A AU 5190486 A AU5190486 A AU 5190486A
- Authority
- AU
- Australia
- Prior art keywords
- catalyst
- sapo
- silicoaluminophosphate
- weight
- percent
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- 239000003054 catalyst Substances 0.000 title claims description 255
- 238000000034 method Methods 0.000 title claims description 69
- 238000005336 cracking Methods 0.000 title claims description 63
- 230000008569 process Effects 0.000 title claims description 56
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 87
- 239000010457 zeolite Substances 0.000 claims description 62
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 58
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 51
- 239000000203 mixture Substances 0.000 claims description 51
- 229910021536 Zeolite Inorganic materials 0.000 claims description 50
- 229910000323 aluminium silicate Inorganic materials 0.000 claims description 42
- 238000006243 chemical reaction Methods 0.000 claims description 32
- 239000011159 matrix material Substances 0.000 claims description 32
- 239000000377 silicon dioxide Substances 0.000 claims description 29
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 claims description 28
- 239000002808 molecular sieve Substances 0.000 claims description 27
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 27
- 238000004523 catalytic cracking Methods 0.000 claims description 22
- 229910052761 rare earth metal Inorganic materials 0.000 claims description 21
- 238000001179 sorption measurement Methods 0.000 claims description 21
- ZMANZCXQSJIPKH-UHFFFAOYSA-N Triethylamine Chemical compound CCN(CC)CC ZMANZCXQSJIPKH-UHFFFAOYSA-N 0.000 claims description 18
- 239000010779 crude oil Substances 0.000 claims description 18
- 229910052809 inorganic oxide Inorganic materials 0.000 claims description 18
- 239000011148 porous material Substances 0.000 claims description 17
- 150000001768 cations Chemical class 0.000 claims description 15
- 239000001282 iso-butane Substances 0.000 claims description 14
- 150000002910 rare earth metals Chemical class 0.000 claims description 14
- 238000009835 boiling Methods 0.000 claims description 13
- 229910052681 coesite Inorganic materials 0.000 claims description 12
- 229910052906 cristobalite Inorganic materials 0.000 claims description 12
- 239000003921 oil Substances 0.000 claims description 12
- 229910052682 stishovite Inorganic materials 0.000 claims description 12
- 229910052905 tridymite Inorganic materials 0.000 claims description 12
- 229930195733 hydrocarbon Natural products 0.000 claims description 11
- 150000002430 hydrocarbons Chemical class 0.000 claims description 11
- 230000000694 effects Effects 0.000 claims description 10
- 238000002360 preparation method Methods 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 8
- 239000003795 chemical substances by application Substances 0.000 claims description 7
- 229910052698 phosphorus Inorganic materials 0.000 claims description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 6
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 6
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 6
- 229910052782 aluminium Inorganic materials 0.000 claims description 6
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 6
- 238000010586 diagram Methods 0.000 claims description 6
- 239000011574 phosphorus Substances 0.000 claims description 6
- 229910052710 silicon Inorganic materials 0.000 claims description 6
- 239000010703 silicon Substances 0.000 claims description 6
- 239000012013 faujasite Substances 0.000 claims description 5
- 229910052777 Praseodymium Inorganic materials 0.000 claims description 4
- PUDIUYLPXJFUGB-UHFFFAOYSA-N praseodymium atom Chemical compound [Pr] PUDIUYLPXJFUGB-UHFFFAOYSA-N 0.000 claims description 4
- PCTMTFRHKVHKIS-BMFZQQSSSA-N (1s,3r,4e,6e,8e,10e,12e,14e,16e,18s,19r,20r,21s,25r,27r,30r,31r,33s,35r,37s,38r)-3-[(2r,3s,4s,5s,6r)-4-amino-3,5-dihydroxy-6-methyloxan-2-yl]oxy-19,25,27,30,31,33,35,37-octahydroxy-18,20,21-trimethyl-23-oxo-22,39-dioxabicyclo[33.3.1]nonatriaconta-4,6,8,10 Chemical compound C1C=C2C[C@@H](OS(O)(=O)=O)CC[C@]2(C)[C@@H]2[C@@H]1[C@@H]1CC[C@H]([C@H](C)CCCC(C)C)[C@@]1(C)CC2.O[C@H]1[C@@H](N)[C@H](O)[C@@H](C)O[C@H]1O[C@H]1/C=C/C=C/C=C/C=C/C=C/C=C/C=C/[C@H](C)[C@@H](O)[C@@H](C)[C@H](C)OC(=O)C[C@H](O)C[C@H](O)CC[C@@H](O)[C@H](O)C[C@H](O)C[C@](O)(C[C@H](O)[C@H]2C(O)=O)O[C@H]2C1 PCTMTFRHKVHKIS-BMFZQQSSSA-N 0.000 claims description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 3
- 229910052684 Cerium Inorganic materials 0.000 claims description 3
- 229910052779 Neodymium Inorganic materials 0.000 claims description 3
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 claims description 3
- 239000003245 coal Substances 0.000 claims description 3
- 229910052746 lanthanum Inorganic materials 0.000 claims description 3
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 claims description 3
- QEFYFXOXNSNQGX-UHFFFAOYSA-N neodymium atom Chemical compound [Nd] QEFYFXOXNSNQGX-UHFFFAOYSA-N 0.000 claims description 3
- 238000000634 powder X-ray diffraction Methods 0.000 claims description 3
- 229910052692 Dysprosium Inorganic materials 0.000 claims description 2
- 229910052691 Erbium Inorganic materials 0.000 claims description 2
- 229910052693 Europium Inorganic materials 0.000 claims description 2
- 229910052688 Gadolinium Inorganic materials 0.000 claims description 2
- 229910052689 Holmium Inorganic materials 0.000 claims description 2
- 229910052765 Lutetium Inorganic materials 0.000 claims description 2
- 229910052773 Promethium Inorganic materials 0.000 claims description 2
- 229910052772 Samarium Inorganic materials 0.000 claims description 2
- 229910052771 Terbium Inorganic materials 0.000 claims description 2
- 229910052775 Thulium Inorganic materials 0.000 claims description 2
- 229910052769 Ytterbium Inorganic materials 0.000 claims description 2
- KBQHZAAAGSGFKK-UHFFFAOYSA-N dysprosium atom Chemical compound [Dy] KBQHZAAAGSGFKK-UHFFFAOYSA-N 0.000 claims description 2
- UYAHIZSMUZPPFV-UHFFFAOYSA-N erbium Chemical compound [Er] UYAHIZSMUZPPFV-UHFFFAOYSA-N 0.000 claims description 2
- OGPBJKLSAFTDLK-UHFFFAOYSA-N europium atom Chemical compound [Eu] OGPBJKLSAFTDLK-UHFFFAOYSA-N 0.000 claims description 2
- UIWYJDYFSGRHKR-UHFFFAOYSA-N gadolinium atom Chemical compound [Gd] UIWYJDYFSGRHKR-UHFFFAOYSA-N 0.000 claims description 2
- KJZYNXUDTRRSPN-UHFFFAOYSA-N holmium atom Chemical compound [Ho] KJZYNXUDTRRSPN-UHFFFAOYSA-N 0.000 claims description 2
- OHSVLFRHMCKCQY-UHFFFAOYSA-N lutetium atom Chemical compound [Lu] OHSVLFRHMCKCQY-UHFFFAOYSA-N 0.000 claims description 2
- VQMWBBYLQSCNPO-UHFFFAOYSA-N promethium atom Chemical compound [Pm] VQMWBBYLQSCNPO-UHFFFAOYSA-N 0.000 claims description 2
- KZUNJOHGWZRPMI-UHFFFAOYSA-N samarium atom Chemical compound [Sm] KZUNJOHGWZRPMI-UHFFFAOYSA-N 0.000 claims description 2
- GZCRRIHWUXGPOV-UHFFFAOYSA-N terbium atom Chemical compound [Tb] GZCRRIHWUXGPOV-UHFFFAOYSA-N 0.000 claims description 2
- NAWDYIZEMPQZHO-UHFFFAOYSA-N ytterbium Chemical compound [Yb] NAWDYIZEMPQZHO-UHFFFAOYSA-N 0.000 claims description 2
- 239000000395 magnesium oxide Substances 0.000 claims 2
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims 2
- 241000269350 Anura Species 0.000 description 42
- 150000001336 alkenes Chemical class 0.000 description 27
- 239000012188 paraffin wax Substances 0.000 description 23
- 239000002002 slurry Substances 0.000 description 18
- 238000010998 test method Methods 0.000 description 17
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 15
- 239000007789 gas Substances 0.000 description 13
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 239000004927 clay Substances 0.000 description 11
- 238000002156 mixing Methods 0.000 description 11
- -1 rare earth metal cations Chemical class 0.000 description 11
- 239000005995 Aluminium silicate Substances 0.000 description 10
- 235000012211 aluminium silicate Nutrition 0.000 description 10
- 238000001354 calcination Methods 0.000 description 10
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 10
- 229910052593 corundum Inorganic materials 0.000 description 8
- 239000007787 solid Substances 0.000 description 8
- 229910001845 yogo sapphire Inorganic materials 0.000 description 8
- 238000002441 X-ray diffraction Methods 0.000 description 7
- 238000009826 distribution Methods 0.000 description 7
- 239000000571 coke Substances 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 6
- 238000010335 hydrothermal treatment Methods 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 230000009849 deactivation Effects 0.000 description 5
- 239000000017 hydrogel Substances 0.000 description 5
- 238000005342 ion exchange Methods 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- 239000007921 spray Substances 0.000 description 5
- 238000007669 thermal treatment Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 125000003118 aryl group Chemical group 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- 238000011065 in-situ storage Methods 0.000 description 4
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 4
- 229910001404 rare earth metal oxide Inorganic materials 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 3
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 3
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000000654 additive Substances 0.000 description 3
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- 238000001125 extrusion Methods 0.000 description 3
- 239000000499 gel Substances 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- LIKMAJRDDDTEIG-UHFFFAOYSA-N 1-hexene Chemical compound CCCCC=C LIKMAJRDDDTEIG-UHFFFAOYSA-N 0.000 description 2
- HNRMPXKDFBEGFZ-UHFFFAOYSA-N 2,2-dimethylbutane Chemical compound CCC(C)(C)C HNRMPXKDFBEGFZ-UHFFFAOYSA-N 0.000 description 2
- BZHMBWZPUJHVEE-UHFFFAOYSA-N 2,4-dimethylpentane Chemical compound CC(C)CC(C)C BZHMBWZPUJHVEE-UHFFFAOYSA-N 0.000 description 2
- AFABGHUZZDYHJO-UHFFFAOYSA-N 2-Methylpentane Chemical compound CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 2
- WWUVJRULCWHUSA-UHFFFAOYSA-N 2-methyl-1-pentene Chemical compound CCCC(C)=C WWUVJRULCWHUSA-UHFFFAOYSA-N 0.000 description 2
- GXDHCNNESPLIKD-UHFFFAOYSA-N 2-methylhexane Chemical compound CCCCC(C)C GXDHCNNESPLIKD-UHFFFAOYSA-N 0.000 description 2
- VLJXXKKOSFGPHI-UHFFFAOYSA-N 3-methylhexane Chemical compound CCCC(C)CC VLJXXKKOSFGPHI-UHFFFAOYSA-N 0.000 description 2
- PFEOZHBOMNWTJB-UHFFFAOYSA-N 3-methylpentane Chemical compound CCC(C)CC PFEOZHBOMNWTJB-UHFFFAOYSA-N 0.000 description 2
- WSSSPWUEQFSQQG-UHFFFAOYSA-N 4-methyl-1-pentene Chemical compound CC(C)CC=C WSSSPWUEQFSQQG-UHFFFAOYSA-N 0.000 description 2
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 2
- 229920000168 Microcrystalline cellulose Polymers 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 2
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- 239000002243 precursor Substances 0.000 description 2
- 241000894007 species Species 0.000 description 2
- 238000001694 spray drying Methods 0.000 description 2
- WGECXQBGLLYSFP-UHFFFAOYSA-N (+-)-2,3-dimethyl-pentane Natural products CCC(C)C(C)C WGECXQBGLLYSFP-UHFFFAOYSA-N 0.000 description 1
- OTTZHAVKAVGASB-HWKANZROSA-N (E)-Hept-2-ene Chemical compound CCCC\C=C\C OTTZHAVKAVGASB-HWKANZROSA-N 0.000 description 1
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- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000011959 amorphous silica alumina Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000005341 cation exchange Methods 0.000 description 1
- CETPSERCERDGAM-UHFFFAOYSA-N ceric oxide Chemical compound O=[Ce]=O CETPSERCERDGAM-UHFFFAOYSA-N 0.000 description 1
- 229910000422 cerium(IV) oxide Inorganic materials 0.000 description 1
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- 150000003841 chloride salts Chemical class 0.000 description 1
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- 239000002131 composite material Substances 0.000 description 1
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- 238000007796 conventional method Methods 0.000 description 1
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- 150000002500 ions Chemical group 0.000 description 1
- MRELNEQAGSRDBK-UHFFFAOYSA-N lanthanum oxide Inorganic materials [O-2].[O-2].[O-2].[La+3].[La+3] MRELNEQAGSRDBK-UHFFFAOYSA-N 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
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- 150000004682 monohydrates Chemical class 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- PLDDOISOJJCEMH-UHFFFAOYSA-N neodymium oxide Inorganic materials [O-2].[O-2].[O-2].[Nd+3].[Nd+3] PLDDOISOJJCEMH-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- KTUFCUMIWABKDW-UHFFFAOYSA-N oxo(oxolanthaniooxy)lanthanum Chemical compound O=[La]O[La]=O KTUFCUMIWABKDW-UHFFFAOYSA-N 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 150000003013 phosphoric acid derivatives Chemical class 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
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- 229910001388 sodium aluminate Inorganic materials 0.000 description 1
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- 229910001948 sodium oxide Inorganic materials 0.000 description 1
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 1
- 229910052911 sodium silicate Inorganic materials 0.000 description 1
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- 239000011269 tar Substances 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
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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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/82—Phosphates
- B01J29/84—Aluminophosphates containing other elements, e.g. metals, boron
- B01J29/85—Silicoaluminophosphates [SAPO compounds]
-
- 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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/005—Mixtures of molecular sieves comprising at least one molecular sieve which is not an aluminosilicate zeolite, e.g. from groups B01J29/03 - B01J29/049 or B01J29/82 - B01J29/89
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
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Description
Cracking catalysts and process using mixed catalyst systems
FIELD OF THE INVENTION
The present invention relates to cracking catalysts derived from mixtures of zeolitic aluminosilicates and a specific class the silicoaluminophosphate molecular sieves of U.S. Patent No. 4,440,871. The novel catalyst mixtures are employed in cracking processes to provide product mixtures substantially more valuable than products obtained by use of zeolite based cracking catalysts.
BACKGROUND OF THE INVENTION
The prior art dealing with catalytic cracking catalysts has in large part evolved by the preparation of modified zeolites for use as components in cracking catalysts. The following patents are representative of the prior art dealing with zeolites and matrices.
The use of conversion catalysts formed from a zeolite dispersed in a siliceous matrix has been disclosed in U.S. Pat. No. 3,140,249 and U.S. Pat. No. 3,352,796.
The use of blended matrix components, e.g., a catalyst comprising a zeolite, an inorganic oxide matrix and inert fines, which may be alpha alumina, is disclosed in U.S. Pat. No. 3,312,615. Catalysts comprising an amorphous silica-alumina, separately added alumina and a zeolite are disclosed in U.S. Pat. No. 3,542,670 and catalyst comprising a zeolite, an amorphous hydrous alumina and alumina monohydrate are disclosed in U.S. Pat. No. 3,428,550.
It has been disclosed that the steam and thermal stability of Y zeolites can be improved by the use of zeolites having a low level of alkali metal content and a unit cell size less than about 24.45 Angstroms (See: U.S. Pat. Nos. 3,293,192 and Re. 28,629 (Reissue of U.S. Pat. No. 3,402,996)).
Further, it has been disclosed (U.S. Pat. No. 3,591,488) that the hydrogen or ammonium form of a zeolite may be treated with H2O at a temperature ranging from about 800° to about 1500°F, and then subsequently cation exchange the steam and water treated zeolite with cations which may be rare earth metal cations. U.S. Pat. No. 3,676,368 discloses a rare earth exchanged-hydrogen faujasite containing from 6 to 14 percent rare earth oxides. U.S. Pat. No. 3,957,623 discloses a rare earth exchanged zeolite having a total of 1 to 10 weight percent rare earth metal oxide. U.S. Pat. No. 3,607,043 discloses a process for preparing a zeolite having a rare earth content of 0.3 to 10 weight percent.
U.S. Pat. No. 4,036,739 discloses hydrothermally stable and ammonia stable Y zeolite in which a sodium Y zeolite is ion exchanged to partially exchange sodium ions for ammonium ions, followed by steam calcination and a further ion exchange with ammonium to reduce the final sodium oxide content to below 1 weight percent, followed by calcination of the reexchanged product, or according to U.S. Pat. No. 3,781,199, the second calcination may be conducted after the zeolite is admixed with a refractory oxide.
The products obtained by use of such aforementioned catalysts may not be the most desirable in all instances. Accordingly, catalysts and processes have been developed to modify the products of cracking processes. Several patents have disclosed the use of various additives as components in cracking catalysts to modify product distributions. U.S. Patent No. 4,284,529 discloses the use of a catalyst additive comprising a zeolite having an alpha value not less than about 5 and having substantially no activity for cracking n-hexane. U.S. Patent No. 4,239,654 discloses a catalyst composition comprising an ultrastable Y-type crystalline aluminosilicate zeolite, a catalytic inorganic oxide matrix and a small pore crystalline ZSM-type zeolite. U.S. Patent No. 4,289,606 is similar to U.S. Patent No. 4,239,654 in that a small pore crystalline ZSM-5 type zeolite is employed with an ultrastable Y-type crystalline aluminosilicate zeolite as the catalyst. U.S. Patent Nos. 4,309,279 and 4,309,280 relate to the use of a zeolite additive to cracking processes wherein the zeolite is characterized by a Constraint Index of about 1 to 12 and a silica to alumina ratio greater than about 12. The above processes relate to the use of zeolite mixtures and are necessarily limited to zeolites.
U.S. Patent No. 4,440,871 discloses a novel class of crystalline microporous silicoalumino¬phosphate molecular sieves. These silicoalumino¬phosphates are generally disclosed as being useful for various hydrocarbon conversion processes,
including catalytic cracking processes. The use of the silicoaluminophosphates of U.S. Patent No. 4,440,871 as components in conventional cracking catalysts for the conversion of crude oil feedstocks containing carbon-hydrogen fragmentation compounds is disclosed in copending U.S. Serial No. 490,952, filed May 2, 1983. Although the above generally disclose the use of the silicoaluminophosphates in cracking processes such do not disclose the use of specific silicoaluminophosphates to provide improved product distribution, as hereinafter discussed.
The use of silicoaluminophosphate molecular sieves as cracking catalysts is disclosed in copending U.S. Serial No. (Attorney Docket No. 14,698), filed concurrently herewith and commonly assigned.
The instant invention relates to the use of specific silicoaluminophosphate molecular sieves as components in cracking catalysts and to catalytic cracking processes. When such silicoaluminophosphate molecular sieves are added to cracking catalysts and employed in catalytic cracking processes such processes give products having product distributions substantially different and more valuable from that obtained in the absence of such silicoaluminophosphate molecular sieves. SUMMARY OF THE INVENTION
The instant process relates to the catalytic cracking of crude oil feedstocks to produce lower boiling hydrocarbons and comprises contacting said feedstocks at effective catalytic cracking conditions with a catalyst comprising
particles having catalytic activity for cracking crude oil feedstocks, e.g., at least one zeolitic aluminosilicate of the type generally employed in cracking catalysts, and at least one silicoaluminophosphate molecular sieve of U.S. Patent No. 4,440,871 characterized in its calcined form by an adsorption of isobutane of at least 2 percent by weight at a partial pressure of 500 torr and a temperature of 20°C. The zeolitic aluminosilicate is characterized as being a zeolitic cracking component, such as heretofore traditionally employed in such cracking catalysts, e.g., the various forms of zeolite Y. The silicoaluminophosphate molecular sieves employed in this invention are unique in that such are not zeolitic aluminosilicates, as heretofore employed in the prior art, but are members of the class of novel silicoaluminophosphate molecular sieves of U.S. Patent No. 4,440,871.
DETAILED DESCRIPTION OF THE INVENTION
The present invention relates to new catalytic cracking catalysts, the process for their preparation and to the process of their use in catalytic cracking processes for the conversion of crude oil feedstocks. The catalytic cracking catalysts of the instant invention are derived from a special class of a novel class of silicoaluminophosphate molecular sieves and any suitable cracking catalyst known in the art to have cracking activity at effective catalytic cracking conditions. The silicoaluminophosphates employed in the instant invention are a special class of the
silicoaluminophosphates denominated as "SAPOs" in U.S. Patent No. 4,440,871, incorporated herein by reference thereto.
It has been found that the use of specific silicoaluminophosphates provide an improved distribution of products when such silicoaluminophosphates are employed in conjunction with conventional zeolitic aluminosilicate cracking catalysts. Heretofore, the catalysts of the prior art have required that certain penalties be endured for the optimization of a particular process variables or product characteristic, e.g., octane. For example, an improvement in gasoline octane of the products as indicated by an increased ratio of branched to linear olefins and isoparaffin to normal paraffins has been observed to occur with a concurrent decrease in gasoline yield and in feed conversion when zeolitic aluminosilicate based catalysts are employed. As aforementioned, the presence of isoparaffins and branched olefins have long been employed as indications of higher octane products and their increase or decrease used as a relative indication of the octane of the gasoline product. The instant process is characterized by improved production of isoparaffins and branched olefins and also by a decrease in the relative amount of normal paraffins and linear olefins while minimizing the loss in gasoline yield and feed conversion.
The silicoaluminophosphate molecular sieves of U.S. Patent No. 4,440,871 are described as microporous crystalline silicoaluminophosphates the
pores of which are uniform and have nominal diameters of greater than about 3 Angstroms and whose essential empirical chemical composition in the as-synthesized and anhydrous form is mR:(SixAlyPz)O2 wherein "R" represents at least one organic templating agent present in the intracrystalline pore system; "m" represents the moles of "R" present per mole of (SixAlyPz)O2; "m" has a value of from 0.02 to 0.3; "x", "y" and "z" represent the mole fractions of silicon, aluminum and phosphorus respectively, present as tetrahedral oxides, said mole fractions being such that they are within the pentagonal compositional area defined by points ABCD and E of the ternary diagram which is FIG. 1 of the drawings of U.S. Patent No. 4,440,871. The SAPO molecular sieves of U.S. Patent No. 4,440,871 are also described as silicoaluminophosphates having a three-dimensional microporous framework structure of
PO2 +, AlO2- and SiO2 tetrahedral units, and whose essential empirical chemical composition on an anhydrous basis is: mR:(SixAlyPz)O2 wherein "R" represents at least one organic templating agent present in the intracrystalline pore system; "m" represents the moles of "R" present per mole of (SixAlyPz)O2 and has a value of from zero to 0.3; "x" , "y" and "z" represent respectively, the mole fractions of silicon, aluminum and phosphorus present in the oxide moiety, said mole fractions being within the compositional area bounded by points A, B, C, D and E on the
ternary diagram which is FIG. 1, said silicoaluminophosphate having a characteristic X-ray powder diffraction pattern which contains at least the d-spacings set forth below in any one of Tables I, III, V, VII, IX, XII, XVII, XXI, XXIII or XXV of U.S. Patent No. 4,440,871. Further, such crystalline silicoaluminophosphates may be calcined at a temperature sufficiently high to remove at least some of any organic templating agent present in the intracrystalline pore system. The silicoaluminophosphates of U.S. Patent No. 4,440,871 are generally referred to therein as "SAPO-n", as a class, or as "SAPO-n" wherein "n" is an interger denoting a particular SAPO as its preparation is reported in U.S. Patent No. 4,440,871. The specific SAPOs employed in the instant invention are further characterized in their calcined form by an adsorption of isobutane of at least 2 percent by weight at a partial pressure of 500 torr and a temperature of 20°C. Further, and more preferably such SAPOs are also characterized in their calcined form by an adsorption of triethylamine of less than 5 percent by weight at a partial pressure of 2.6 torr and a temperature of 22°C. SAPO's employable herein include, but are not limited to, SAPO-5, SAPO-11, SAPO-31, SAPO-37, SAPO-40 and SAPO-41.
The above characterization of the silicoaluminophosphates (SAPOs) employed in the instant invention relates to an adsorption characterization that is carried out on a SAPO which has been subjected to a post synthesis treatment, e.g., calcination or chemical treatment, to remove a
substantial portion of the template "R" which is present as a result of synthesis. Although a particular SAPO is characterized herein by its adsorption of isobutane and optionally lack of adsorption of that of triethylamine as being a SAPO in its calcined form, the instant invention necessarily includes the use of a non-calcined SAPO which is characterized by such adsorption in its calcined form, since upon use of such a non-calcined SAPO in the instant process at catalytic cracking conditions the SAPO will be calcined or hydrothermally treated in situ so as to have the characteristic minimum adsorption of isobutane. Thus, the SAPO will be rendered in situ to a form characterized by the aforementioned adsorption characteristics. For example, an as-synthesized SAPO-11 is not characterized by the aforementioned adsorption of isobutane due to the presence of template "R" which is present as a result of synthesis, although the calcined form of SAPO-11 is characterized by the aforementioned adsorption of isobutane or triethylamine. Thus, reference to a SAPO as having a particular adsorption characteristic in its calcined form is not intended to exclude the use of the SAPO in its as-synthesized form which upon calcination, hydrothermal treatment and/or other treatment, e.g., ion exchange with suitable cations, would have such adsorption characteristics.
It has been found that this class of silicoaluminophosphates provides product distributions not formed by cracking catalysts
containing zeolitic aluminosilicates without a silicoaluminophosphate. Heretofore, the catalysts of the prior art have exhibited a decrease in gasoline yield and/or conversion for the optimization of a particular process variable or product characteristic e.g., octane of the gasoline product. Such penalties are reduced by use of the instant catalysts. Further, improved production of isoparaffins and branched olefins and also by the decreased amount of normal paraffins and linear olefins by use of the instant catalysts are indications of higher octane products.
The term "crude oil feedstock" is used herein to denominate any crude oil feedstock or portion thereof and includes full range crude oils from primary, secondary or tertiary recovery from conventional or offshore oil fields and feedstocks derived therefrom. "Crude oil feedstocks" may also be "syncrudes" such as those that can be derived from coal, shale oil, tar sands and bitumens. The crude oil feedstock may be virgin (straight run) or generated synthetically by blending. Such crude oil feedstocks are traditionally desalted prior to use since sodium chloride is known to be a poison in many cracking operations. Further, the term "crude oil feedstocks" is intended to include component parts of crude oils which have heretofore been generally employed as catalytic cracking feeds or potential feeds and includes feeds such as distillate gas oils, heavy vacuum gas oils, VGO, atmospheric and vacuum resids, syncrudes, pulverized coal and fractions boiling above the traditional end
of the gasoline boiling range which generally includes compounds containing greater than about eleven carbon atoms and combinations thereof.
Cracking catalysts are in particulate form and generally comprise an inorganic, porous refractory oxide such as silica-alumina and also alumina and/or silica and/or clays. Such catalysts also generally contain at least one aluminosilicate. The zeolitic aluminosilicate cracking component of such catalysts may be any aluminosilicate heretofore employed as a component in cracking catalysts. Representative of the zeolitic aluminosilicates disclosed heretofore as employable as component parts of cracking catalysts are Zeolite Y, Zeolite X, Zeolite beta (U.S. Patent No. 3,308,069), Zeolite KZ-20 (U.S. Patent No. 3,445,727), Zeolite ZSM-3 (U.S. Patent No. 3,415,736), faujasite, LZ-10 (U.K. Patent 2,014,970, June 9, 1982), ZSM-type zeolites and mixtures thereof. Traditional cracking catalysts containing amounts of Na2O less than about 6 percent by weight are generally preferred with less than 1 percent by weight Na2O being generally employed in traditional cracking catalysts, based on the total catalyst weight.
Representative Y-type zeolites believed employable herein include, but are not limited to, those disclosed in U.S. Patent Nos.: 3,130,007; 3,835,032; 3,830,725; 3,293,192; 3,449,070; 3,839,539; 3,867,310; 3,929,620; 3,929,621: 3,933,983; 4,058,484; 4,085,069; 4,175,059: 4,192,778; 3,676,368; 3,595,611; 3,594,331:
3,536,521; 3,293,192; 3,966,643; 3,966,882 and 3,957,623.
Another zeolitic aluminosilicate employable herein is "LZ-210", as described in E.P.C. Publication No. 82,211 published June 29, 1983.
The term "ZSM-type" zeolites is generally employed in the art to refer to those zeolites denominated by the nomenclature "ZSM-n" where "n" is an integer. The ZSM-type aluminosilicates include but are not limited to ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38, ZSM-48; and other similar materials.
ZSM-5 is described in greater detail in U.S. Patent No. 3,702,886 and Re 29,948. The entire descriptions contained within those patents, particularly the X-ray diffraction pattern of therein disclosed ZSM-5, are incorporated herein by reference.
ZSM-11 is described in U.S. Patent No. 3,709,979. That description, and in particular the X-ray diffraction pattern of said ZSM-11, is incorporated herein by reference. ZSM-12 is described in U.S. Patent No. 3,832,449. That description, and in particular the X-ray diffraction pattern disclosed therein, is incorporated herein by reference.
ZSM-23 is described in U.S. Patent No. 4,076,842. The entire content thereof, particularly the specification of the X-ray diffraction pattern of the disclosed zeolite, is incorporated herein by reference.
ZSM-35 is described in U.S. Patent No. 4,016,245. The description of that zeolite, and particularly the X-ray diffraction pattern thereof, is incorporated herein by reference.
ZSM-38 is more particularly describing U.S. Patent No. 4,046,859. The description of that zeolite, and particularly the specified X-ray diffraction pattern hereof, is incorporated herein by reference.
ZSM-48 is more particularly described in U.S. Patent No. 4,423,021. The description of that zeolite, and particularly the specified X-ray diffraction pattern thereof, is incorporated herein by reference.
CRACKING CATALYSTS The catalysts of the instant invention comprise at least one zeolitic aluminosilicate cracking component and at least one SAPO molecular sieve component. The relative amount of each component will depend at least in part, on the selected crude oil feedstock and on the desired product distribution obtained therefrom but in instances an effective amount of at least one SAPO is employed to provide a different product distribution as compared to that obtained by use of the zeolitic aluminosilicate without the SAPO molecular sieve component. The relative weight ratio of the zeolitic aluminosilicate to the SAPO is generally between about 1:10 and about 500:1, desirably between about 1:10 and about 200:1, preferably between about 1:2 and about 50:1, and
most preferably is between about 1:1 and about 20:1. The zeolitic aluminosilicate and/or SAPO may be ion-exchanged with a selected cation(s) and/or thermally treated either before or after mixture with each other or after such have been added separately or concurrently mixed with one or more inorganic oxide matrix components. When exchanged the SAPO molecular sieves are preferably exchanged with a hydrogen-forming cation species, e.g. NH+ 4, H+ , quaternary ammonium cations , etc . The SAPO preferably has at least part of its cations as hydrogen-forming cation species.
The term "thermal treatment" is employed here to denominate both a thermal calcination in the presence of air or inert gas, e.g., nitrogen, and a hydrothermal calcination (thermal calcination in the presence of steam). The thermal treatment is carried out at an effective temperature and time and when a hydrothermal treatment in the presence of an effective amount of steam. The thermal treatment is typically carried out at a temperature in excess of 300°C for a period in excess of 0.25 hours and when the thermal treatment is a hydrothermal treatment it is typically carried out in the presence of at least about 20 percent steam by volume in air and up to about 100 percent steam. The source of the steam is not important and may be provided from an external source or may be generated in situ at the temperatures employed for the hydrothermal treatment. As aforementioned a SAPO may be employed in the instant process in its as-synthesized form since in situ hydrothermal treatment will be
provided upon introduction of the SAPO to the process under catalytic cracking conditions.
Any ion-exchange of the zeolitic aluminosilicate(s) and SAPO(s), which aluminosilicate or SAPO may have been subjected to thermal treatment, may be carried out by contacting such with a solution of at least one cation, including those selected from the group of cations consisting of ammonium, Group IIA, Group IIIA, Group IIIB to VIIB and rare earth cations selected from the group consisting of cerium, lanthanum, praseodymium, neodymium, promethium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium and mixtures thereof. At present, the presence of rare earth cations with the SAPO molecular sieves has not been observed to be beneficial to the activity of the SAPO component. The exact nature of the relationship of rare earth cations and SAPOs is not clearly understood at present. As a result of ion-exchange the cation(s), e.g., rare earth cation, may replace at least a portion of the cations initially present in the zeolitic aluminosilicate or SAPO. The cations provided by ion-exchange may be present in an effective amount which may be between about 0.1 weight percent and about 20 weight percent, typically between about 0.5 and about 10 weight percent, based on the weight of the starting zeolitic aluminosilicate or SAPO.
The cracking catalysts of this invention are typically employed with an inorganic oxide matrix component which may be any of the inorganic
oxide matrix components which have been employed heretofore in the formulation of FCC catalysts including: amorphous catalytic inorganic oxides, e.g., catalytically active silica-aluminas, clays, silicas, aluminas, silica-aluminas, silica-zirconias, silica-magnesias, alumina-borias, alumina-titanias and the like and mixtures thereof. The zeolite and SAPO may be mixed separately with the matrix component and then mixed or the zeolite and SAPO may be mixed and then formed with the matrix component.
The inorganic oxide matrix component may be in the form of a sol, hydrogel or gel and is typically an alumina, silica, clay and/or silica-alumina component such as employed a conventional silica-alumina cracking catalyst, several types and compositions of which are commercially available. The matrix component may itself provide a catalytic effect or it may be essentially inert. The matrix may act as a "binder" in some instances, although in some instances the final catalyst may be spray dried or formed without the need of a binder. These materials may be prepared as a cogel of silica and alumina or as alumina precipitated on a preformed and preaged hydrogel. The silica may be present as a component in the solids present in such gels, e.g. present in an amount between about 5 and about 40 weight percent and preferably between about 10 and about 30 weight percent. Silica may also be employed in the form of a cogel comprising about 75 weight percent silica and about 25 weight percent alumina or
comprising about 87 weight percent silica and about 13 weight percent alumina. The inorganic oxide matrix component will typically be present in the catalyst in an amount between about 0 and about 99 weight percent, preferably between about 5 and about 95 weight percent, based on the total catalyst weight. It is also within the scope of the instant invention to employ other materials in addition to the zeolitic aluminosilicate, SAPO molecular sieve and inorganic oxide matrix components in the final cracking catalysts, including various other types of zeolites, clays, carbon monoxide oxidation promoters, etc.
Representative of matrix systems employable herein are disclosed in British Patent Specification No. 1,315,553, published May 2, 1973 and U.S. Patents Nos. 3,446,727 and 4,086,187, such being incorporated herein by reference thereto.
As above mentioned, the catalysts of the present invention may be employed with a matrix component and this may be an alumina component. The alumina component may comprise discrete particles of various aluminas, e.g., pseudobeohmite. The alumina component may be in the form of discrete particles having a total surface area, as measured by the method of Brunauer, Emmett and Teller (BET), greater than about 20 square meters per gram (M2/g), preferably greater than 145 M2/g, for example, from about 145 to about 300 M2/g. The pore volume of the alumina component is typically be greater than 0.35 cc/g. The average particle size of the alumina particles is generally less than 10 microns
and preferably less than 3 microns. The alumina may be employed alone as the matrix or composited with the other matrix components. The alumina component may be any alumina and has preferably been preformed and placed in a physical form such that its surface area and pore structure are stabilized so that when the alumina is added to an impure, inorganic gel containing considerable amounts of residual soluble salts, the salts will not alter the surface and pore characteristics measurably nor will they promote chemical attack on the preformed porous alumina which could undergo change. For example, the alumina may be any an alumina which has been formed by suitable chemical reaction, the slurry aged, filtered, dried, washed free of residual salt and then heated to reduce its volatile content to less than about 15 weight percent. Further, an alumina hydrosol or hydrogel or hydrous alumina slurry may be used in the catalyst preparation.
The inorganic oxide matrix components, e.g. aluminas, silicas, clays, etc., may be present in the final catalyst in an amount ranging between about 5 and about 99 weight percent, preferably between about 5 and about 95 weight percent and more preferably between about 10 and about 85 weight percent, based on the total catalyst weight.
Mixtures of the zeolitic aluminosilicate, SAPO molecular sieve and the inorganic matrix may be formed into the final form for the catalyst by standard catalyst forming techniques including spray-drying, pelleting, extrusion and other suitable conventional means. Such catalysts are
typically prepared by spray drying, such procedures being well known to those skilled in the art of preparing catalytic cracking catalysts. Although the exact reason for such is not presently understood, the instant catalysts have been observed to provide different results in some instances when employed in cracking processes depending on whether the zeolitic aluminosilicate and SAPO are coincidentally or separately mixed with the matrix component.
Catalytic cracking catalysts may be prepared by any one of several conventional methods. One method of preparing such catalysts employing silica-alumina and porous alumina is to react sodium silicate with a solution of aluminum sulfate to form a silica/alumina hydrogel slurry which is then aged to give the desired pore properties, filtered to remove a considerable amount of the extraneous and undesired sodium and sulfate ions and then reslurried in water. The alumina may be prepared by reacting solutions of sodium aluminate and aluminum sulfate under suitable conditions, aging the slurry to give the desired pore properties of the alumina, filtering drying, reslurry in water to remove sodium and sulfate ions and drying to reduce volatile matter content to less than 15 weight percent. The alumina may then be slurried in water and blended in proper amounts, with a slurry of impure silica-alumina hydrogel. The zeolitic aluminosilicate and SAPO molecular sieve may then be added to this blend. A sufficient amount of each component is utilized to give the desired final composition. The resulting mixture is then filtered to remove a portion of the remaining
extraneous soluble salts therefrom. The filtered mixture is then dried to produce dried solids. The dried solids are subsequently reslurried in water and washed substantially free of the undesired soluble salts. The catalyst is then dried to a residual water content of less than about 15 weight percent. The catalyst is typically recovered after calcination.
Catalytic cracking with the catalyst of the present invention can be conducted in any catalytic cracking process under effective catalytic cracking conditions. Suitable catalytic cracking conditions include a temperature ranging between about 400°F and about 1600°F, preferably between about 700°F and about 1600°F and a pressure ranging from about subatmospheric to several atmospheres, typically from about atmospheric to about 100 psig. The process may be carried out in a fixed fluidized bed, moving bed, ebullating bed, slurry, transferline, riser reactor or fluidized bed operation. The catalyst of the present invention can be used to convert any of the conventional hydrocarbon feeds used in catalytic cracking, that is, it can be used to crack naphthas, gas oil and residual oils having a high content of metal contaminants. It is especially suited for cracking hydrocarbons boiling in the gas oil range, that is, hydrocarbon oils having an atmospheric pressure boiling point ranging from about 420°F to about 1800°F to naphthas to yield not only products having a lower boiling point than the initial feed and gasoline products having an improved octane number.
The mixture of a traditional cracking and a SAPO may be carried out in any manner which results in the coincident presence of such in contact with the crude oil feedstock under catalytic cracking conditions. For example, a catalyst may be employed containing both the traditional cracking catalyst and a SAPO in single catalyst particles or SAPO, with or without a matrix component, may be added as a discrete component to a traditional cracking catalyst. In one embodiment, a SAPO may be added to a cracking process as a make-up catalyst to replace the traditional cracking catalyst that has been lost through attrition.
The following examples were carried out to illustrate the instant invention and are not intended to be limiting thereof. The zeolite LZ-210 was prepared in each example according to the disclosure of E.P.C. Publication No. 82,211, published June 29, 1983. SAPO molecular sieves were prepared according to U.S. Patent No. 4,440,871. The SAPO molecular sieves were calcined in air prior to use in the following examples. Calcination procedures for the removal of template are disclosed in U.S. Patent No. 4,440,871. The catalysts prepared in the following examples were evaluated by a procedure substantially the same as D-3907. Accordingly, reference to ASTM test method D-3907, hereinafter is meant to generally refer to the procedure of the ASTM test method with the following four modifications. First, the end boiling point of the products identified as gasoline products was 431°F. Second, the nitrogen post stripping of the
catalyst was at 30 milliliteres/min for a period of 23 minutes to 27 minutes. Third, the conversion is the measured conversion and not the standardized conversion of the ASTM test method. Fourth, the feedstock employed in the test method had an API gravity of 24.0°, an IBP (Initial Boiling Point) of 354°F, FBP (Final Boiling Point) of 1077°F and a UOP K Factor of 11.8.
Example 1 A cracking catalyst was prepared according to the invention employing a mixture of SAPO-5 and LZ-210. In addition, a cracking catalyst containing LZ-210 was prepared as a reference catalyst. The catalysts were prepared using LZ-210, having a SiO2/Al2O3 ratio of 9.0, and SAPO-5. Two catalysts were prepared. Catalyst A was the reference catalyst and Catalyst B was a catalyst according to this invention. Catalyst A was prepared by slurrying 18% by weight LZ-210, 18% by weight of pseudobeohmite alumina, 60% by weight of a kaolin clay; 4% by weight of a silica and enough water to form a slurry having a 25% by weight solids content. The aforementioned percentages for the solid components are given on a dry basis. The slurry was then spray dried to obtain a fluidizable catalyst composite that would pass through a 150 micron sieve (U.S. Standard). The catalyst was then calcined at 600°C for 1 hour and then steam deactivated at 740°C for 2 hours in 100% steam. Catalyst B was prepared by mixing Catalyst A and SAPO-5. The SAPO-5 was steam deactivated at 760°C
for 2 hours in 100% steam prior to mixing with Catalyst A. The steam deactivation procedures are provided to simulate the environment experienced by commercial cracking catalysts. Catalyst B contained 10 percent by weight of SAPO-5 based on the total weight of Catalyst B.
Catalysts A and B were each evaluated according to ASTM test method D-3907. In this and in the subsequent examples the "wt.% Conversion" is the measured weight percent conversion as defined in ASTM test method D-3907 and as above discussed. The "Wt.% Gasoline" is defined as those hydrocarbons in the product from C5 hydrocarbons to hydrocarbons boiling below 431°F expressed as a weight percent of feed. The term "alkylate" herein denominates propylene, butylenes and isobutane. The "Wt.% Gas" is defined as those hydrocarbons boiling below C4 in the product as a weight percent of feed. The "Wt.% Coke" is defined as the residue left on the used catalyst after post stripping and is given as a weight percent of the feed. The "Wt.% C4's" is defined as the weight percent of isobutane, n-butane and butylenes of the product. The "wt.% C6-C8 Aromatics" is defined herein as the weight percent of benzene, ethyl benzene, toluene and xylenes in the gasoline product. The results were as follows:
Catalyst
Catalyst A Catalyst B
Wt.% Conversion 70.3 71.0
Wt.% Gasoline 50.0 49.3
Wt.% Gasoline + Aklylate 60.9 61.6
Wt.% C6-C8 Aromatics 14.6 15.4
Wt.% Coke 4.9 4.8
Wt.% Gas 6.2 6.7
Wt.% C4s 9.1 10.2
The above data demonstrate that Catalyst B was comparable to Catalyst A as to Wt.% Conversion and Wt.% Gasoline while making more aromatic products which are useful in enhancing the octane of the gasoline products.
Example 2 Two catalysts were prepared wherein Catalyst C was a reference catalyst containing LZ-210 having a SiO2/Al2O3 ratio of 9.0 and Catalyst D was a catalyst according to the invention and contained LZ-210 and SAPO-11. Catalyst C was prepared by preparing a slurry containing 15% by weight LZ-210, 18% by weight of a pseudobeohmite alumina, 60% by weight kaolin clay and 4% by weight silica in enough water to obtain a slurry having 25 percent by weight solids. The slurry was then spray dried to obtain a fluidizable catalyst having its size characterized by passing through a 150 micron sieve (U.S. Standard). The catalyst was calcined at 600°C for 1 hour and then steam deactivated at 765°C for 2 hours in 100% steam.
Catalyst D was prepared according to the procedure employed for Catalyst C, except that 10 percent by weight kaolin clay was replaced by 10 percent by weight of SAPO-11, i.e. 50% by weight kaolin clay was employed.
Catalyst C and Catalyst D were evaluated according to ASTM test method D-3907, except that the run temperature was 850°F instead of the 900°F suggested by ASTM test method D-3907. The results were as follows:
Catalyst
Catalyst C Catalyst D
Conversion: 61.9 62.9
Wt.% Gasoline: 46.5 47.6
Wt.% Gasoline + Alkylate 55.3 56.7
Wt.% Paraffin Analysis1: Iso/normal C4 4.8 5.7 Iso/normal C6 13.6 17.1 Iso/normal C7 15.6 16.8
Iso/normal C 8 7.1 8.1
Wt.% Gas Product Analysis2 Olefin/paraffin C3 2.8 3.8 Olefin/paraffin C4 0.55 0.66
Wt.% Coke 4.1 4.0
1 Iso paraffin to normal paraffin ratios of compounds having the indicated number of carbons.
2 Olefin to paraffin ratio of compounds having the indicated number of carbons.
The above results demonstrate that the addition of SAPO-11 as a component of Catalyst D provided products having comparable Wt.% Gasoline and Wt.% Gasoline + Alkylate while also providing for an increase in the iso to normal ratio of the paraffin products, thus indicating higher octane products. The increase in the olefin content of the gas product, as indicated by the Gas Product Analysis, indicates a gas product having more useful and valuable olefin products.
Example 3 Two catalysts were prepared wherein
Catalyst E was a reference catalyst containing LZ-210 (SiO2/Al2O3 ratio of 9.0) and Catalyst F was a catalyst according to this invention containing LZ-210 and SAPO-5.
Catalyst E was prepared by forming a slurry of 15% by weight LZ-210, 18% by weight .of a pseudobeohmite alumina, 63% by weight kaolin clay, 4% by weight silica and enough water to form a slurry containing 25 percent by weight solids. The slurry was then spray dried calcined and treated by the procedure employed for Catalyst C in example 2.
Catalyst F was prepared by forming a slurry of 15% by weight LZ-210, 10% by weight SAPO-5, 18% by weight of a pseudobeohmite alumina, 53% by weight kaolin clay, 4% by weight silica and enough water to form a slurry containing 25% by weight solids. The slurry was. then .spray dried, calcined and treated by the procedure employed for Catalyst C in example 2.
Catalyst E and Catalyst F were each evaluated according to ASTM test method D-3907. The results were as follows:
Catalyst
Catalyst E Catalyst F
Wt.% Conversion 77.2 76.8
Wt.% Gasoline + Alkylate 63.8 60.3
Wt.% C6-C8 Aromatics 33.4 37.8
Wt.% Coke 7.7 7.9
Catalyst/Oil Ratio (Weight) 5 3
The above data indicate that Catalyst F, according to this invention, was considerably more
active than Catalyst E requiring only a Catalyst/Oil ratio of 3 to achieve a conversion comparable to Catalyst E employed at a Catalyst/Oil ratio of 5. This use of forty percent less catalyst to achieve comparable conversion demonstrates the surprising increase in activity of the catalyst comprising LZ-210 and SAPO-5. Further, Catalyst F formed products containing about 4.4 percent more C6-C8 aromatic products in the gasoline product with about a 3.5% reduction in the Wt.% Gasoline + Alkylate. The presence of increased amounts of aromatic products is an indication of higher octane products. Further, aromatic components are valuable as components in other chemical processes.
The above data also demonstrate that the order of mixing of the components in Catalyst F resulted in changes in the mixed catalyst, as compared to the mixed catalysts of example 1. The addition of SAPO-5 to the slurry, instead of physically mixing SAPO-5 with a Y zeolite/matrix mixture resulted in a more active catalyst than above described in example 1 for Catalyst B. The exact reasons for this change in activity as a result of the mixing order is not clearly understood at this time.
Example 4 Two catalysts were prepared wherein Catalyst G was a reference catalyst containing ZSM-5 (SiO2 to Al2O3 ratio of 30), as described in U.S. Patent No. 4,239,654, and Catalyst H was a catalyst according to this invention containing SAPO-5.
A catalyst base was prepared by rare earth exchanging LZ-210 by use of a solution of a mixture of rare earth chlorides. The rare earth solution contained about 46.0% by weight, expressed on rare earth oxides, with the rare earth component comprising 60.0% lanthanum (La2O3), 21.5% neodymium (Nd2O3), 10.0% cerium (CeO2), 7.5% praseodymium (Pr6O11) and about 1.0% other rare earths. The final rare earth exchanged LZ-210 had 9.9% by weight rare earth, measured as the oxide (RE2O3 where "RE" denotes rare earth cations). A mixture was formed by blending 14.3% by weight of the rare earth LZ-210, 80.7% of a silica-alumina (sold by Davison Division of W..R. Grace under the trademark MS13/110 and containing 86 wt. % SiO2 and 13 wt. % Al2O3) and 5.0% by weight of a microcrystalline cellulose extrusion aid. This mixture was extruded, dried at 110°C in air for 16 hours and then steam deactivated for 5 hours at 760°C in 100% steam. The extrudates were then crushed and sized to 60 to 200 mesh (U.S. Standard).
Catalyst G and Catalyst H were prepared by mixing, respectively, 5 percent by weight of ZSM-5 and SAPO-5 with 95 percent by weight of the catalyst base, as above prepared. The two catalysts were evaluated according to ASTM test method D-3907. The results were as follows:
Catalyst
Catalyst G Catalyst H
Wt.% Conversion: 65.2 66.8 Wt.% Gasoline : 42.8 47.3 Wt.% C6-C8 Aromatics in Gasoline: 11.5 14.1 Iso/Normal (C6 paraffin) 7.3 11.2
14 t
The above data demonstrate the significant improvements in Wt.% Conversion, Wt.% Gasoline, Wt.% C6-C8 Aromatics in Gasoline and the iso to normal ratio (weight ratio) of C6 paraffins when SAPO-5 is employed as a component of the cracking catalyst as compared to the use of ZSM-5.
Example 5 Two catalysts were prepared according to the procedure employed in example 2 for Catalyst C and Catalyst D, except that the steam deactivation temperatures were as set forth below in Table I. Catalysts derived from the non-steam deactivated precursor of Catalyst C by changing the steam deactivation temperature are denominated "Catalyst C-n" wherein "n" is an integer. Catalysts derived from the non-steam deactivated precursor of Catalyst D are similarly denominated. The catalysts were evaluated according to ASTM test method D-3907 and the following results obtained:
The above data demonstrate that catalysts containing SAPOs retain their selective nature after hydrothermal treatment. The branched to linear olefin weight ratio and the iso to normal paraffin weight ratios were higher at comparable conversions and gasoline yield for the catalysts containing SAPO-11 as compared to catalysts containing no SAPO-11, thus indicating higher octane products. Thus, the advantages derived from use of SAPOs is not significantly affected by hydrothermal deactivation conditions.
Example 6 Two catalysts were prepared wherein reference Catalyst J contained a steam stabilized Y zeolite denominated as LZ-10 and a Catalyst K contained LZ-10 and SAPO-11. LZ-10 was prepared according to U.K. Patent 2,014,970 and was then ammonium exchanged.
Catalyst J was prepared by preparing a mixture containing 18% by weight LZ-10, 62% by weight kaolin clay and 20% by weight silica in enough water to form an extrudable mass. This mixture had a paste consistency and was mulled, extruded and calcined at 500°C for 16 hours in air. The extrudates were crushed and sized so as to pass through a 60 mesh screen (U.S. Standard) and not pass through a 200 mesh (U.S. Standard) screen.
Catalyst K was prepared as was Catalyst J, except that the initial mixture was 18% by weight LZ-10, 6% by weight SAPO-11, 56% by weight kaolin clay and 20% by weight silica.
The two catalysts were evaluated according to ASTM test method D-3907 except the run temperature was 866°F. All product ratios are given as weight ratios. The results were as follows:
Catalyst
Catalyst J Catalyst K
Wt.% Conversion 70.2 69.1
Wt.% Gasoline 50.7 50.1
C3 Olefin/C3 paraffin 1.76 1.86
C4 Olefin/C4 paraffin .402 .382
C4 Iso/C4 Normal paraffin 4.12 4.64
Wt.% Alkylate 10.9 10.9
C6 olefin/ C6 paraffin .154 .166
C6 iso/C6 normal paraffin1 13.4 15.4
C6 Branched/ C6 Linear Olefin1 1.18 1.67
C7 llefin/ C7 paraffin .0769 .086
C7 iso/C7 normal -paraffin2 16.9 18.6
C7 Branched/C7 Linear Olefin 2 .739 .799
1 C6 isoparaffins measured were 2-methyl pentane, 3-methyl pentane and 2,2 dimethyl butane. C6 normal paraffin measured was n-hexane. C6 branched olefins measured were 3-methyl-1-pentene, 4-methyl-1-pentene, 2-methyl-1-pentene, 2-methyl-2-ρentene and trans-3-methyl-2-pentene. C6 linear olefins measured were 1-hexene, trans-2-hexene, cis-2-hexene and trans-3-hexene. 2 C7 iso-paraffins measured were 3-methyl hexane, 2-methyl hexane and 2,4-dimethyl pentane. C7 normal paraffin measured was n-heptane. C7 branched olefins measured were determined by
measuring all C7 olefins and subtracting from that factor the C7 linear olefins measured.
C7 linear olefins measured were 1-heρtene, cis-2-heptene, trans-2-heptene, cis-3-heptene and trans-3-heptene.
The above data demonstrate that Catalyst K, according to this invention, provided at comparable activity and gasoline yield a gasoline product having higher iso/normal paraffin and branched/ linear olefin ratios in the C6 and C7 hydrocarbons which are indicative of higher octane products and such were formed at comparable gasoline yield and conversion.
Comparative Example 7
Two catalysts were prepared wherein reference Catalyst L contained LZ-210 and comparative Catalyst M contained AlPO4-5 and Catalyst L. AlPO4-5 was prepared according to U.S. Patent No. 4,310,440.
Catalyst L was prepared by forming a mixture of 15% by weight LZ-210 (SiO2 to Al2O3 ratio of 9.0), 63% by weight kaolin clay, 18% by weight alumina and 4% by weight silica. The catalyst was extruded and treated similar to the catalysts of example 3 except that the steam deactivation was at 765°C.
Catalyst M was prepared by blending 10% by weight of a calcined AlPO4-5 with 90% by weight of Catalyst L.
Catalyst L and Catalyst M were evaluated by ASTM test method D-3907 The olefin/paraffin and
iso/normal ratios are given as weight-ratios. The results were as follows:
Catalyst
Catalyst L Catalyst M
Wt.% Conversion 69.9 67.1
Wt.% Gasoline 50.8 48.6
C3 Olefin/Paraffin 2.87 2.68
C4 Olefin/Paraffin 0.59 0.57
C4 Iso/Normal Paraffin 4.36 4.36
The above data demonstrate that AlPO4-5, having a similar framework topology to SAPO-5 but lacking SiO2 tetrahedral components, does not provide the benefits observed from the use of SAPO-5 in conjunction with a traditional cracking catalyst.
Comparative Example 8 Three catalysts (N, O and P) were prepared. Catalysts N and P are comparative catalysts and catalyst O is a catalyst prepared according to the instant invention. The catalysts were formed according to the procedure employed in example 1 except that Catalysts O and P employed 54 weight percent kaolin clay and the zeolite and SAPO components were as follows. Catalyst N contained 18 weight percent of an LZ-210 having a SiO2 to Al2O3 ratio of 9.0. Catalyst O contained 18 weight percent of the LZ-210 employed in Catalyst N and 6 weight percent of SAPO-11. Catalyst P contained 18 weight percent of the LZ-210 employed in Catalyst N and 6 weight percent of SAPO-34.
Catalysts N, O and P were steam deactivated in 100 percent steam for 2 hours and at 740°C, 740°C and 760°C, respectively, and evaluated according to ASTM test method D-3907. The results of this evaluation were as follows:
Catalyst
Catalyst Catalyst Catalyst
N O P
Wt.% Conversion 72.7 71.5 72.0
Wt.% Gasoline 52.7 51.2 47.7
Wt .% Gas + C4 ' s 15 .6 15.8 19. 5
Wt.% Coke 4.05 4.27 - -
The above results demonstrate the reduced gasoline yield of catalysts containing SAPO-34. SAPO-34 is not characterized by an adsorption of isobutane of at least 2 percent by weight at a pressure of 500 torr and a temperature of 20°C as are the SAPOs of the instant invention.
Comparative Example 9
Two comparative catalysts were prepared for evaluation according to ASTM test method D-3907. The two catalysts were prepared using the silicoaluminophosphate molecular sieve SAPO-5 and the zeolite LZ-210 (SiO2 to Al2O3 ratio of 9.0).
After preparation of SAPO-5 the material was steam deactivated in 100 percent steam at 760°C for 2 hours to simulate the effect of actual use in a cracking process. The LZ-210 component was then rare earth exchanged with a mixture of rare earth
chlorides, as described in example 4, to give a rare earth exchanged LZ-210 containing 9.9 weight percent rare earth, expressed as the oxide.
A matrix for the SAPO-5 and LZ-210 was prepared by mixing 90 percent by weight of a silica/alumina, sold by the Davison Division of W.R. Grace under the trade designation MS13/110, and 10 percent by weight of a microcrystalline cellulose extrusion aid. The mixture was extruded in the form of 1/16 inch pellets and dried in air at 110°C for about 16 hours and then steam deactivated in 100 percent steam at 760°C for 2 hours. The steam deactivated material was then crushed and sized to 60 to 200 mesh (U.S. Standard).
The SAPO-5 and LZ-210 catalysts were each prepared by mixing 15 percent by weight of the selected material with 85 percent by weight of the matrix. The LZ-210 was steam deactivated in 100% steam at 760°C for 2 hours prior to use in the preparation of the catalyst. The final catalyst mixtures were then calcined at 590°C in air for 3 hours. Each catalyst was evaluated for conversion according to ASTM test method D-3907. The results of the evaluation were as follows:
Catalyst
SAPO-5 LZ-210
Wt.% Conversion 57.7 57.2 Wt.% Gasoline 37.2 41.4 Wt.% Gas 6.6 5.5 Wt.% Coke 3.9 3.1 Wt.% C4 10.0 7.33
The above results demonstrate the individual activity of SAPO-5 and LZ-210 as cracking catalysts. Although LZ-210 showed a higher wt.% Gasoline SAPO-5 formed more gas products and C4 products under the conditions of ASTM test method D-3907. As observable from the above examples according to the instant invention, the use of a catalyst comprising a traditional cracking catalyst and a SAPO provide products having different components than the products obtained by use of a SAPO or LZ-210 separately.
Claims (42)
1. The process for cracking a crude oil feedstock to produce lower boiling hydrocarbons comprising contacting at effective catalytic cracking conditions a crude oil feedstock with a conversion catalyst comprising effective amounts of at least one zeolitic aluminosilicate and at least one silicoaluminophosphate molecular sieve of U.S. Patent No. 4,449,871 characterized in its calcined form by an adsorption of isobutane of at least 2 percent by weight at a pressure of 500 torr and a temperature of 20°C.
2. The process of claim 1 wherein said silicoaluminophosphate is further characterized in its calcined form by an adsorption of triethylamine of less than 5 percent by weight at a pressure of 2.6 torr and a temperature of 22°C.
3. The process of claim 1 wherein said catalyst comprises a weight ratio between about 1:10 and about 500:1 of said zeolitic aluminosilicate cracking component to said silicoaluminophosphate molecular sieve and from 0 and about 99 weight percent of at least one inorganic oxide matrix component, based on the total weight of said catalyst.
4. The process of claim 3 wherein the weight ratio of zeolitic aluminosilicate to said silicoaluminophosphate is between about 1:2 and about 50:1.
5. The process of claim 4. wherein the weight ratio of zeolitic aluminosilicate to said silicoaluminophosphate is between about 1:1 and about 20:1.
6. The process of claim 3 wherein inorganic oxide component is present in an amount between about 5 and about 95 percent by weight, based on the total weight of said catalyst.
7. The process according to claim 1 wherein said zeolite component of the conversion catalyst contains an effective amount of a cation selected from the group consisting of ammonium, Group IIA, Group IIIA, Groups IIIB to VIIB, cerium, lanthanum, praseodymium, neodymium, promethium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium and mixtures thereof.
8. The process of claim 1 wherein said silicoaluminophosphate has at least part of its cations as hydrogen-forming species.
9. The process of claim 8 wherein said hydrogen-forming species is NH4 + or H+.
10. The cracking process of claim 1 wherein the process is carried out by contacting crude oil feedstock boiling between 420°F and about 1800°F with the conversion catalyst at a temperature between about 400°F and about 1300°F, at a pressure between about 14.7 psia to about 100 psia.
11. The process of claim 7 wherein said conversion catalyst contains between about 0.1 percent and about 20 weight percent of said multivalent cations.
12. The process of claim 6 wherein said inorganic oxide matrix component is selected from the group consisting of clays, silicas, aluminas, silica-aluminas, silica-zirconias, silica-magnesia, alumina-borias, alumina-titanias and mixtures thereof.
13. The process of claim 1 or 2 wherein said silicoaluminophosphate is characterized as microporous crystalline silicoaluminophosphates the pores of which are uniform and have nominal diameters of greater than about 3 Angstroms and whose essential empirical chemical composition in the as-synthesized and anhydrous form is mR:(SixAlyPz)O2 wherein "R" represents at least one organic templating agent present in the intracrystalline pore system; "m" represents the moles of "R" present per mole of (SixAlyPz)O2; "m" has a value of from 0.02 to 0.3; "x", "y" and "z" represent the mole fractions of silicon, aluminum and phosphorus respectively, present as tetrahedral oxides, said mole fractions being such that they are within the pentagonal compositional area defined by points ABCD and E of the ternary diagram which is FIG. 1 of the drawings of U.S. Patent No. 4,440,871.
14. The process of claim 1 or 2 wherein said silicoaluminophosphate is characterized as having a three-dimensional microporous framework structure of PO+ 2, AlO2- and SiO2 tetrahedral units, and whose essential empirical chemical composition on an anhydrous basis is: mR:(SixAlyPz)O2 wherein "R" represents at least one organic templating agent present in the intracrystalline pore sys.tem; "m" represents the moles of "R" present per mole of (SixAlyPz)O2 and has a value of from zero to 0.3; "x", "y" and "z" represent respectively, the mole fractions of silicon, aluminum and phosphorus present in the oxide moiety, said mole fractions being within the compositional area bounded by points A, B, C, D and E on the ternary diagram which is FIG. 1, said silicoaluminophosphate having a characteristic X-ray powder diffraction pattern which contains at least the d-spacings set forth below in any one of Tables I, III, V, VII, IX, XII, XVII, XXI, XXIII or XXV of U.S. Patent No. 4,440,871.
15. The process of claim 1 or 2 wherein said silicoaluminophosphate is at least one selected from the group consisting of SAPO-5, SAPO-11, SAPO-31, SAPO-37, SAPO-40 and SAPO-41.
16. The process of claim 15 wherein the silicoaluminophosphate is SAPO-5.
17. The process of claim 15 wherein the silicoaluminophosphate is SAPO-11.
18. The process of claim 15 wherein the silicoaluminophosphate is SAPO-31.
19. The process of claim 15 wherein the silicoaluminophosphate is SAPO-40.
20. The process of claim 15 wherein the silicoaluminophosphate is SAP0-41.
21. The process of claim 1 wherein said crude oil feedstock is selected from the group consisting of distillate gas oils, heavy vacuum gas oils, VGO, atmospheric resids, vacuum resids, syncrudes, pulverized coal and mixtures thereof.
22. The process of claim 1 wherein said zeolitic aluminosilicate is selected from the group consisting of zeolite Y, zeolite X, zeolite beta, zeolite KZ-20, faujasite, LZ-210, LZ-10, ZSM-type zeolites and mixtures thereof.
23. The process of claim 3 wherein said zeolitic aluminosilicate is selected from the group consisting of zeolite Y, zeolite X, zeolite beta, zeolite KZ-20, faujasite, LZ-210, LZ-10, ZSM-type zeolities and mixtures thereof.
24. The process for the preparation of a catalyst comprising: a) forming a mixture of at least one zeolitic aluminosilicate and at least one silicoaluminophosphate of U.S. Patent No. 4,449,871 characterized in its calcined form by an adsorption of isobutane of at least 2 percent by weight at a pressure of 500 torr and a temperature of 20°C at a weight ratio of between about 1:10 and about 500:1, respectively; b) forming a mixture of the product of step a) and at least one inorganic oxide matrix component to form a catalyst.
25. The process for the preparation of a catalyst comprising: a) forming a mixture of at least one inorganic oxide matrix component and at least one zeolitic aluminosilicate; b) forming a mixture of at least one inorganic oxide matrix component and at least one silicoaluminophosphate of U.S. Patent No. 4,449.871 characterized in its calcined form by an adsorption of isobutane of at least 2 percent by weight at a pressure of 500 torr and a temperature of 20°C; and c) forming a mixture of the products of steps a) and b) to form a catalyst having a weight ratio of zeolitic aluminosilicate to silicoaluminophosphate between about 1:10 and about 500:1.
26. The catalyst prepared by the process of claim 24.
27. The catalyst prepared by the process of claim 25.
28. A cracking catalyst comprising at least one zeolitic aluminosilicate having cracking activity at effective cracking conditions and at least one silicoaluminophosphate molecular sieve of U.S. Patent No. 4, 449, 871, characterized in its calcined form by an adsorption of isobutane of at least 2 percent by weight at a pressure of 500 torr and a temperature of 20°C, wherein the weight ratio of said aluminosilicate to silicialuminophosphate is between about 1:10 and about 500:1.
29. The catalyst of claim 28 wherein said silicoaluminophosphate molecular sieve is further characterized in its calcined form by an adsorption of triethylamine of less than 5 percent by weight at a pressure of 2.6 torr and a temperature of 22°C.
30. The catalyst of claim 27 or 28 wherein said silicoaluminophosphate is characterized as microporous crystalline silicoaluminophosphates the pores of which are uniform and have nominal diameters of greater than about 3 Angstroms and whose essential empirical chemical composition in the as-synthesized and anhydrous form is mR: (SiχAlyPz)O2 wherein "R" represents at least one organic templating agent present in the intracrystalline pore system; "m" represents the moles of "R" present per mole of (SixAlyPz)O2; "m" has a value of from 0.02 to 0.3; "x" , "y" and "z" represent the mole fractions of silicon, aluminum and phosphorus respectively, present as tetrahedral oxides, said mole fractions being such that they are within the pentagonal compositional area defined by points ABCD and E of the ternary diagram which is FIG. 1 of the drawings of U.S. Patent No. 4,440,871.
31. The catalyst of claim 28 or 29 wherein said silicoaluminophosphate is characterized as having a three-dimensional microporous framework structure of PO2 +, AlO2- and SiO2 tetrahedral units, and whose essential empirical chemical composition on an anhydrous basis is: mR:(SixAlyPz)O2 wherein "R" represents at least one organic templating agent present in the intracrystalline pore system; "m" represents the moles of "R" present per mole of (SixAlyPx)O2 and has a value of from zero to 0.3; "x", "y" and "z" represent respectively, the mole fractions of silicon, aluminum and phosphorus present in the oxide moiety, said mole fractions being within the compositional area bounded by points A, B, C, D and E on the ternary diagram which is FIG. 1, said silicoaluminophosphate having a characteristic X-ray powder diffraction pattern which contains at least the d-spacings set forth below in any one of Tables I, III, V, VII, IX, XII, XVII, XXI, XXIII or XXV of U.S. Patent No. 4,440,871.
32. The catalyst of claim 28 or 29 wherein said zeolitic aluminosilicate is selected from the group consisting of zeolite Y, zeolite X, zeolite beta, zeolite KZ-20, faujasite, LZ-210, LZ-10, ZSM-type zeolites and mixtures thereof.
33. The catalyst of claim 32 wherein said catalyst contains from 0 to 99 percent by weight of at least inorganic oxide matrix component.
34. The catalyst of claim 33 wherein the inorganic oxide matrix component is selected from the group consisting of clays, silicas, aluminas, silica-aluminas, silicas-zirconias, silica-magnesia, alumina-borias, alumina-titanias and mixtures thereof.
35. The catalyst of claim 28 wherein said silicoaluminophosphate is selected from the group consisting of SAPO-5, SAPO-11, SAPO-31, SAPO-37, SAPO-40, SAPO-41 and mixtures thereof.
36. The catalyst of claim 28 wherein said zeolitic aluminosilicate is selected from the group consisting of Y zeolite, LZ-210, LZ-10 and mixtures thereof and said silicoaluminophosphate is selected from the group consisting of SAPO-5, SAPO-11, SAPO-31, SAPO-41 and mixtures thereof.
37. The catalyst of claim 28 wherein said zeolitic aluminosilicate contains between about 0.1 and about 20 percent by weight of a cation selected from the group consisting of ammonium, Group IIA, Group IIA, Groups II B to VII B, rare earth and mixtures thereof.
38. A cracking catalyst comprising of at least one cracking catalyst having cracking activity at effective cracking conditions and an effective amount of at least one silicoaluminophosphate molecular sieve of U.S. Patent No. 4,449,871 characterized in its calcined form by an adsorption of isobutane of at least 2 percent by weight at a pressure of 500 torr and a temperature of 20°C.
39. The catalyst of claim 38 wherein the weight ratio of said cracking catalyst to said silicoaluminophosphate is between about 1:10 and about 500:1.
40. The catalyst of claim 38 wherein said cracking catalyst consists at least one zeolitic aluminosilicate.
41. The catalyst of claim 38 wherein said cracking catalyst consists essentially of a silica-alumina.
42. The catalyst of claim 38 wherein said silicoaluminophosphate is further characterized in its calcined form by an adsoption of triethylamine of less than 5 percent by weight at a pressure of 2.6 torr and a temperature of 22°C.
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---|---|
EP (1) | EP0202325A1 (en) |
CN (1) | CN1006687B (en) |
AU (1) | AU5190486A (en) |
DK (1) | DK486386D0 (en) |
FI (1) | FI863823A0 (en) |
WO (1) | WO1986003138A1 (en) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0230005A3 (en) * | 1985-12-23 | 1987-08-26 | W.R. Grace & Co.-Conn. | Cracking catalyst |
US4708786A (en) * | 1986-03-26 | 1987-11-24 | Union Oil Company Of California | Process for the catalytic cracking of nitrogen-containing feedstocks |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2286393A1 (en) * | 1974-09-27 | 1976-04-23 | Labo Electronique Physique | AUTOMATIC PERMANENT CALIBRATION SYSTEM FOR SCINTILLATION CAMERA |
DK230481A (en) * | 1981-05-26 | 1982-11-27 | Gen Electric Nuclear Medical A | DEVICE BY AN OLD CAMERA FOR AUTOMATIC REINFORCEMENT CONTROL |
US4440871A (en) * | 1982-07-26 | 1984-04-03 | Union Carbide Corporation | Crystalline silicoaluminophosphates |
DE3370469D1 (en) * | 1982-11-16 | 1987-04-30 | Hoechst Ag | Aluminium silicates with a zeolite structure and process for their preparation |
US4512875A (en) * | 1983-05-02 | 1985-04-23 | Union Carbide Corporation | Cracking of crude oils with carbon-hydrogen fragmentation compounds over non-zeolitic catalysts |
ATE24542T1 (en) * | 1983-05-02 | 1987-01-15 | Union Carbide Corp | CATALYST AND PROCESS FOR CATALYTIC CRACKING. |
-
1985
- 1985-11-26 AU AU51904/86A patent/AU5190486A/en not_active Abandoned
- 1985-11-26 CN CN 85109361 patent/CN1006687B/en not_active Expired
- 1985-11-26 EP EP86900380A patent/EP0202325A1/en not_active Withdrawn
- 1985-11-26 WO PCT/US1985/002325 patent/WO1986003138A1/en not_active Application Discontinuation
-
1986
- 1986-09-22 FI FI863823A patent/FI863823A0/en not_active Application Discontinuation
- 1986-10-10 DK DK486386A patent/DK486386D0/en unknown
Also Published As
Publication number | Publication date |
---|---|
FI863823A (en) | 1986-09-22 |
EP0202325A1 (en) | 1986-11-26 |
CN85109361A (en) | 1986-08-27 |
WO1986003138A1 (en) | 1986-06-05 |
CN1006687B (en) | 1990-02-07 |
FI863823A0 (en) | 1986-09-22 |
DK486386D0 (en) | 1986-10-10 |
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