CA2371225A1 - Catalyst selectivation - Google Patents
Catalyst selectivation Download PDFInfo
- Publication number
- CA2371225A1 CA2371225A1 CA002371225A CA2371225A CA2371225A1 CA 2371225 A1 CA2371225 A1 CA 2371225A1 CA 002371225 A CA002371225 A CA 002371225A CA 2371225 A CA2371225 A CA 2371225A CA 2371225 A1 CA2371225 A1 CA 2371225A1
- Authority
- CA
- Canada
- Prior art keywords
- zeolite
- component
- toluene
- agent
- para
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 72
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 23
- 239000010457 zeolite Substances 0.000 claims description 145
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 118
- 229910021536 Zeolite Inorganic materials 0.000 claims description 104
- 238000000034 method Methods 0.000 claims description 61
- 239000000203 mixture Substances 0.000 claims description 61
- 229910052751 metal Inorganic materials 0.000 claims description 20
- 239000002184 metal Substances 0.000 claims description 20
- 229910000323 aluminium silicate Inorganic materials 0.000 claims description 19
- 229910044991 metal oxide Inorganic materials 0.000 claims description 15
- 238000002156 mixing Methods 0.000 claims description 14
- 150000002739 metals Chemical class 0.000 claims description 13
- 125000002524 organometallic group Chemical group 0.000 claims description 12
- 239000002904 solvent Substances 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 4
- 150000002891 organic anions Chemical class 0.000 claims description 3
- 150000004760 silicates Chemical class 0.000 claims description 3
- 125000000524 functional group Chemical group 0.000 claims description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol group Chemical group C1(=CC=CC=C1)O ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 2
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 abstract description 255
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 abstract description 144
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 87
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 abstract description 63
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 24
- 229910002091 carbon monoxide Inorganic materials 0.000 abstract description 24
- 239000012022 methylating agents Substances 0.000 abstract description 11
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 10
- 150000002902 organometallic compounds Chemical class 0.000 abstract description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 5
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 5
- 239000001257 hydrogen Substances 0.000 abstract description 5
- 230000004048 modification Effects 0.000 abstract description 5
- 238000012986 modification Methods 0.000 abstract description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 4
- 150000001491 aromatic compounds Chemical class 0.000 abstract description 4
- 238000000151 deposition Methods 0.000 abstract description 3
- 239000001569 carbon dioxide Substances 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 description 75
- 238000006555 catalytic reaction Methods 0.000 description 73
- 239000000463 material Substances 0.000 description 72
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 40
- IJKVHSBPTUYDLN-UHFFFAOYSA-N dihydroxy(oxo)silane Chemical compound O[Si](O)=O IJKVHSBPTUYDLN-UHFFFAOYSA-N 0.000 description 30
- 230000008569 process Effects 0.000 description 25
- 239000008096 xylene Substances 0.000 description 23
- 230000015572 biosynthetic process Effects 0.000 description 22
- 239000000243 solution Substances 0.000 description 22
- 239000011701 zinc Substances 0.000 description 22
- 150000001875 compounds Chemical class 0.000 description 21
- 239000000843 powder Substances 0.000 description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 19
- 238000003786 synthesis reaction Methods 0.000 description 18
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 17
- 229910003455 mixed metal oxide Inorganic materials 0.000 description 17
- 239000013078 crystal Substances 0.000 description 16
- 150000004706 metal oxides Chemical class 0.000 description 16
- 239000011651 chromium Substances 0.000 description 14
- 230000011987 methylation Effects 0.000 description 14
- 238000007069 methylation reaction Methods 0.000 description 14
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 13
- 230000009849 deactivation Effects 0.000 description 13
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 13
- 239000000047 product Substances 0.000 description 13
- 239000000377 silicon dioxide Substances 0.000 description 13
- 238000012360 testing method Methods 0.000 description 13
- 229910052725 zinc Inorganic materials 0.000 description 13
- 238000005804 alkylation reaction Methods 0.000 description 12
- 229910052710 silicon Inorganic materials 0.000 description 12
- 150000003738 xylenes Chemical class 0.000 description 12
- 230000029936 alkylation Effects 0.000 description 11
- -1 polyethylene terephthalate Polymers 0.000 description 11
- 238000011282 treatment Methods 0.000 description 11
- 230000000694 effects Effects 0.000 description 10
- 239000011777 magnesium Substances 0.000 description 10
- 239000000376 reactant Substances 0.000 description 10
- 230000002378 acidificating effect Effects 0.000 description 9
- 229910052804 chromium Inorganic materials 0.000 description 9
- 229910052749 magnesium Inorganic materials 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 9
- 239000002245 particle Substances 0.000 description 9
- 239000010703 silicon Substances 0.000 description 9
- 239000011148 porous material Substances 0.000 description 8
- 150000001336 alkenes Chemical class 0.000 description 7
- 239000000571 coke Substances 0.000 description 7
- 238000011066 ex-situ storage Methods 0.000 description 7
- 239000000543 intermediate Substances 0.000 description 7
- 229910052698 phosphorus Inorganic materials 0.000 description 7
- 239000002244 precipitate Substances 0.000 description 7
- 150000003839 salts Chemical class 0.000 description 7
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 6
- 125000003118 aryl group Chemical group 0.000 description 6
- 229910052796 boron Inorganic materials 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 6
- YIXJRHPUWRPCBB-UHFFFAOYSA-N magnesium nitrate Chemical compound [Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O YIXJRHPUWRPCBB-UHFFFAOYSA-N 0.000 description 6
- 239000011572 manganese Substances 0.000 description 6
- 229910052680 mordenite Inorganic materials 0.000 description 6
- 238000002360 preparation method Methods 0.000 description 6
- 238000003756 stirring Methods 0.000 description 6
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 5
- 229910017974 NH40H Inorganic materials 0.000 description 5
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 5
- 229910052787 antimony Inorganic materials 0.000 description 5
- WATWJIUSRGPENY-UHFFFAOYSA-N antimony atom Chemical compound [Sb] WATWJIUSRGPENY-UHFFFAOYSA-N 0.000 description 5
- ONDPHDOFVYQSGI-UHFFFAOYSA-N zinc nitrate Inorganic materials [Zn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ONDPHDOFVYQSGI-UHFFFAOYSA-N 0.000 description 5
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 4
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 4
- 238000007792 addition Methods 0.000 description 4
- 239000011230 binding agent Substances 0.000 description 4
- 230000003247 decreasing effect Effects 0.000 description 4
- 239000012153 distilled water Substances 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 150000002681 magnesium compounds Chemical class 0.000 description 4
- 230000001035 methylating effect Effects 0.000 description 4
- 239000011574 phosphorus Substances 0.000 description 4
- XNGIFLGASWRNHJ-UHFFFAOYSA-N phthalic acid Chemical compound OC(=O)C1=CC=CC=C1C(O)=O XNGIFLGASWRNHJ-UHFFFAOYSA-N 0.000 description 4
- 238000007086 side reaction Methods 0.000 description 4
- 238000006467 substitution reaction Methods 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical group N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 150000001768 cations Chemical class 0.000 description 3
- PHFQLYPOURZARY-UHFFFAOYSA-N chromium nitrate Inorganic materials [Cr+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O PHFQLYPOURZARY-UHFFFAOYSA-N 0.000 description 3
- 238000000975 co-precipitation Methods 0.000 description 3
- 238000000227 grinding Methods 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 238000011065 in-situ storage Methods 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- 238000006317 isomerization reaction Methods 0.000 description 3
- 229910052746 lanthanum Inorganic materials 0.000 description 3
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000395 magnesium oxide Substances 0.000 description 3
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 229910052748 manganese Inorganic materials 0.000 description 3
- 239000004570 mortar (masonry) Substances 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- 241000269350 Anura Species 0.000 description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 230000003466 anti-cipated effect Effects 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical group [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 150000001555 benzenes Chemical class 0.000 description 2
- GZUXJHMPEANEGY-UHFFFAOYSA-N bromomethane Chemical compound BrC GZUXJHMPEANEGY-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 229910052793 cadmium Inorganic materials 0.000 description 2
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 238000005520 cutting process Methods 0.000 description 2
- 238000007323 disproportionation reaction Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- FYDKNKUEBJQCCN-UHFFFAOYSA-N lanthanum(3+);trinitrate Chemical compound [La+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O FYDKNKUEBJQCCN-UHFFFAOYSA-N 0.000 description 2
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 2
- 239000000347 magnesium hydroxide Substances 0.000 description 2
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 2
- 235000012254 magnesium hydroxide Nutrition 0.000 description 2
- MFUVDXOKPBAHMC-UHFFFAOYSA-N magnesium;dinitrate;hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MFUVDXOKPBAHMC-UHFFFAOYSA-N 0.000 description 2
- MIVBAHRSNUNMPP-UHFFFAOYSA-N manganese(II) nitrate Inorganic materials [Mn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MIVBAHRSNUNMPP-UHFFFAOYSA-N 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- 150000001457 metallic cations Chemical class 0.000 description 2
- BKBMACKZOSMMGT-UHFFFAOYSA-N methanol;toluene Chemical compound OC.CC1=CC=CC=C1 BKBMACKZOSMMGT-UHFFFAOYSA-N 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 2
- 230000007935 neutral effect Effects 0.000 description 2
- 229920000139 polyethylene terephthalate Polymers 0.000 description 2
- 239000005020 polyethylene terephthalate Substances 0.000 description 2
- 229930195734 saturated hydrocarbon Natural products 0.000 description 2
- 229910002027 silica gel Inorganic materials 0.000 description 2
- 239000000741 silica gel Substances 0.000 description 2
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 2
- 229910052814 silicon oxide Inorganic materials 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- LSPHULWDVZXLIL-UHFFFAOYSA-N (+/-)-Camphoric acid Chemical compound CC1(C)C(C(O)=O)CCC1(C)C(O)=O LSPHULWDVZXLIL-UHFFFAOYSA-N 0.000 description 1
- GHOKWGTUZJEAQD-ZETCQYMHSA-N (D)-(+)-Pantothenic acid Chemical compound OCC(C)(C)[C@@H](O)C(=O)NCCC(O)=O GHOKWGTUZJEAQD-ZETCQYMHSA-N 0.000 description 1
- QNLZIZAQLLYXTC-UHFFFAOYSA-N 1,2-dimethylnaphthalene Chemical class C1=CC=CC2=C(C)C(C)=CC=C21 QNLZIZAQLLYXTC-UHFFFAOYSA-N 0.000 description 1
- JRLPEMVDPFPYPJ-UHFFFAOYSA-N 1-ethyl-4-methylbenzene Chemical compound CCC1=CC=C(C)C=C1 JRLPEMVDPFPYPJ-UHFFFAOYSA-N 0.000 description 1
- BRRSNXCXLSVPFC-UHFFFAOYSA-N 2,3,4-Trihydroxybenzoic acid Chemical compound OC(=O)C1=CC=C(O)C(O)=C1O BRRSNXCXLSVPFC-UHFFFAOYSA-N 0.000 description 1
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 1
- KRKNYBCHXYNGOX-UHFFFAOYSA-K Citrate Chemical compound [O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O KRKNYBCHXYNGOX-UHFFFAOYSA-K 0.000 description 1
- 101100348017 Drosophila melanogaster Nazo gene Proteins 0.000 description 1
- 101100117236 Drosophila melanogaster speck gene Proteins 0.000 description 1
- 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 1
- NHTMVDHEPJAVLT-UHFFFAOYSA-N Isooctane Chemical compound CC(C)CC(C)(C)C NHTMVDHEPJAVLT-UHFFFAOYSA-N 0.000 description 1
- 229910020854 La(OH)3 Inorganic materials 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical group [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- 208000012868 Overgrowth Diseases 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical class OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 1
- 241001197925 Theila Species 0.000 description 1
- WGLPBDUCMAPZCE-UHFFFAOYSA-N Trioxochromium Chemical compound O=[Cr](=O)=O WGLPBDUCMAPZCE-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910001413 alkali metal ion Inorganic materials 0.000 description 1
- 229910001420 alkaline earth metal ion Inorganic materials 0.000 description 1
- 150000004996 alkyl benzenes Chemical class 0.000 description 1
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical group [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- 239000003637 basic solution Substances 0.000 description 1
- 229910052790 beryllium Inorganic materials 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052810 boron oxide Inorganic materials 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- NEHMKBQYUWJMIP-NJFSPNSNSA-N chloro(114C)methane Chemical compound [14CH3]Cl NEHMKBQYUWJMIP-NJFSPNSNSA-N 0.000 description 1
- 229910000423 chromium oxide Inorganic materials 0.000 description 1
- 229940001468 citrate Drugs 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical group [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 230000000536 complexating effect Effects 0.000 description 1
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- 238000009833 condensation Methods 0.000 description 1
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- JKWMSGQKBLHBQQ-UHFFFAOYSA-N diboron trioxide Chemical compound O=BOB=O JKWMSGQKBLHBQQ-UHFFFAOYSA-N 0.000 description 1
- AJNVQOSZGJRYEI-UHFFFAOYSA-N digallium;oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Ga+3].[Ga+3] AJNVQOSZGJRYEI-UHFFFAOYSA-N 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- 229940077445 dimethyl ether Drugs 0.000 description 1
- JVSWJIKNEAIKJW-UHFFFAOYSA-N dimethyl-hexane Natural products CCCCCC(C)C JVSWJIKNEAIKJW-UHFFFAOYSA-N 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
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- ZVBWPVOCTORPLM-UHFFFAOYSA-N formylsilicon Chemical compound [Si]C=O ZVBWPVOCTORPLM-UHFFFAOYSA-N 0.000 description 1
- 229910052733 gallium Inorganic materials 0.000 description 1
- 229910001195 gallium oxide Inorganic materials 0.000 description 1
- 229910052732 germanium Inorganic materials 0.000 description 1
- YBMRDBCBODYGJE-UHFFFAOYSA-N germanium oxide Inorganic materials O=[Ge]=O YBMRDBCBODYGJE-UHFFFAOYSA-N 0.000 description 1
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052738 indium Inorganic materials 0.000 description 1
- 229910003437 indium oxide Inorganic materials 0.000 description 1
- PJXISJQVUVHSOJ-UHFFFAOYSA-N indium(iii) oxide Chemical compound [O-2].[O-2].[O-2].[In+3].[In+3] PJXISJQVUVHSOJ-UHFFFAOYSA-N 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000003446 ligand Substances 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- IVSZLXZYQVIEFR-UHFFFAOYSA-N m-xylene Chemical group CC1=CC=CC(C)=C1 IVSZLXZYQVIEFR-UHFFFAOYSA-N 0.000 description 1
- APLYTANMTDCWTA-UHFFFAOYSA-L magnesium;phthalate Chemical compound [Mg+2].[O-]C(=O)C1=CC=CC=C1C([O-])=O APLYTANMTDCWTA-UHFFFAOYSA-L 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 229910000000 metal hydroxide Inorganic materials 0.000 description 1
- 150000004692 metal hydroxides Chemical class 0.000 description 1
- 239000002923 metal particle Substances 0.000 description 1
- 229940102396 methyl bromide Drugs 0.000 description 1
- 239000003607 modifier Substances 0.000 description 1
- KYTZHLUVELPASH-UHFFFAOYSA-N naphthalene-1,2-dicarboxylic acid Chemical compound C1=CC=CC2=C(C(O)=O)C(C(=O)O)=CC=C21 KYTZHLUVELPASH-UHFFFAOYSA-N 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 238000006384 oligomerization reaction Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- PVADDRMAFCOOPC-UHFFFAOYSA-N oxogermanium Chemical compound [Ge]=O PVADDRMAFCOOPC-UHFFFAOYSA-N 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 229910001392 phosphorus oxide Inorganic materials 0.000 description 1
- XNGIFLGASWRNHJ-UHFFFAOYSA-L phthalate(2-) Chemical compound [O-]C(=O)C1=CC=CC=C1C([O-])=O XNGIFLGASWRNHJ-UHFFFAOYSA-L 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- YGSDEFSMJLZEOE-UHFFFAOYSA-M salicylate Chemical compound OC1=CC=CC=C1C([O-])=O YGSDEFSMJLZEOE-UHFFFAOYSA-M 0.000 description 1
- 229960001860 salicylate Drugs 0.000 description 1
- MOODSJOROWROTO-UHFFFAOYSA-N salicylsulfuric acid Chemical compound OC(=O)C1=CC=CC=C1OS(O)(=O)=O MOODSJOROWROTO-UHFFFAOYSA-N 0.000 description 1
- 238000011935 selective methylation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 238000002444 silanisation Methods 0.000 description 1
- 150000003377 silicon compounds Chemical class 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 239000008279 sol Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 229940071103 sulfosalicylate Drugs 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- VSAISIQCTGDGPU-UHFFFAOYSA-N tetraphosphorus hexaoxide Chemical compound O1P(O2)OP3OP1OP2O3 VSAISIQCTGDGPU-UHFFFAOYSA-N 0.000 description 1
- XOLBLPGZBRYERU-UHFFFAOYSA-N tin dioxide Chemical compound O=[Sn]=O XOLBLPGZBRYERU-UHFFFAOYSA-N 0.000 description 1
- 229910001887 tin oxide Inorganic materials 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- 235000009492 vitamin B5 Nutrition 0.000 description 1
- 239000011675 vitamin B5 Substances 0.000 description 1
- 239000011787 zinc oxide Substances 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
- 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
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/061—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof containing metallic elements added to the zeolite
-
- 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
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
-
- 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
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
- B01J29/405—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
-
- 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
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/08—Heat treatment
- B01J37/082—Decomposition and pyrolysis
- B01J37/086—Decomposition of an organometallic compound, a metal complex or a metal salt of a carboxylic acid
-
- 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
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/12—After treatment, characterised by the effect to be obtained to alter the outside of the crystallites, e.g. selectivation
-
- 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
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/32—Reaction with silicon compounds, e.g. TEOS, siliconfluoride
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/34—Reaction with organic or organometallic compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
- B01J37/0203—Impregnation the impregnation liquid containing organic compounds
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
Abstract
It has been discovered that catalysts may be modified by depositing an agent derivative from an agent such as an organometallic compound upon them. Such a modification gives a catalyst useful in increased selectivity to para- substituted alkyl benzenes, such as para-xylene (PX), through reacting an aromatic compound such as toluene and/or benzene with a methylating agent fr om hydrogen and carbon monoxide and/or carbon dioxide and/or methanol. Using these selectivated catalysts, para-substituted alkyl benzenes can be recover ed in a selectivity of 80 % or greater, significantly better than the equilibri um concentration of 24 %.
Description
CATALYST SELECTIVATION
FIELD OF THE INVENTION
The present invention relates to methods for modifying zeolite catalysts and catalysts so modified, and more particularly relates, in one embodiment, to methods for modifying zeolite catalysts to make them more selective to the synthesis of para-substituted dialkylbenzenes relative to other dialkylbenzene isomers, as well as useful in other reactions, and catalysts so modified.
BACKGROUND OF THE INVENTION
Of the para-substituted dialkylbenzenes, para-xylene (PX) is of particular value as a large volume chemical intermediate in a number of applications being useful in the manufacture of terephthalates which are intermediates for the manufacture of polyethylene terephthalate (PET).
One source of feedstocks for manufacturing PX is by disproportionation of toluene into xylenes. One of the disadvantages of this process is that large quantities of benzene are also produced. Another source of feedstocks used to obtain PX involves the isomerization of a feedstream that contains non-equilibrium quantities of mixed ortho- and meta-xylene isomers (OX
and MX, respectively) and is lean with respect to PX content. A
disadvantage of this process is that the separation of the PX from the other isomers is expensive.
Zeolites are known to catalyze the reaction of toluene with other reactants to make xylenes. Some zeolites are silicate based materials which are comprised of a silica lattice and, optionally, alumina combined with exchangeable cations such as alkali or alkaline earth metal ions.
Although the term "zeolites" includes materials containing silica and optionally alumina, it is recognized that the silica and alumina portions may be replaced in whole or in part with other oxides. For example, germanium oxide, tin oxide, phosphorus oxide, and mixtures thereof can replace the silica portion. Boron oxide, iron oxide, gallium oxide, indium oxide, and mixtures thereof can replace the alumina portion. Accordingly, the terms "zeolite", "zeolites" and "zeolite material", as used therein, shall mean not only materials containing silicon and, optionally, aluminum atoms in the crystalline lattice structure thereof, but also materials which contain suitable replacement atoms for such silicon and aluminum, such as gallosilicates, borosilicates, ferrosilicates, and the like.
The term "zeolite, "zeolites", and "zeolite materials" as used herein, besides encompassing the materials discussed above, shall also include aluminophosphate-based materials. Aluminophosphate zeolites are made of alternating A104 and P04 tetrahedra. Aluminophosphate-based materials have lower acidity compared to aluminosilicates. The lower acidity eliminates many side reactions, raises reactants' utilization, and extends catalyst life. Aluminophosphate-based zeolites are often abbreviated as ALPO. Substitution of silicon for P and/or a P-AI pair produces silicoaluminophosphate zeolites, abbreviated as SAPO.
Processes have been proposed for the production of xylenes by the methylation of toluene using a zeolite catalyst. For instance, U.S. Pat. No.
FIELD OF THE INVENTION
The present invention relates to methods for modifying zeolite catalysts and catalysts so modified, and more particularly relates, in one embodiment, to methods for modifying zeolite catalysts to make them more selective to the synthesis of para-substituted dialkylbenzenes relative to other dialkylbenzene isomers, as well as useful in other reactions, and catalysts so modified.
BACKGROUND OF THE INVENTION
Of the para-substituted dialkylbenzenes, para-xylene (PX) is of particular value as a large volume chemical intermediate in a number of applications being useful in the manufacture of terephthalates which are intermediates for the manufacture of polyethylene terephthalate (PET).
One source of feedstocks for manufacturing PX is by disproportionation of toluene into xylenes. One of the disadvantages of this process is that large quantities of benzene are also produced. Another source of feedstocks used to obtain PX involves the isomerization of a feedstream that contains non-equilibrium quantities of mixed ortho- and meta-xylene isomers (OX
and MX, respectively) and is lean with respect to PX content. A
disadvantage of this process is that the separation of the PX from the other isomers is expensive.
Zeolites are known to catalyze the reaction of toluene with other reactants to make xylenes. Some zeolites are silicate based materials which are comprised of a silica lattice and, optionally, alumina combined with exchangeable cations such as alkali or alkaline earth metal ions.
Although the term "zeolites" includes materials containing silica and optionally alumina, it is recognized that the silica and alumina portions may be replaced in whole or in part with other oxides. For example, germanium oxide, tin oxide, phosphorus oxide, and mixtures thereof can replace the silica portion. Boron oxide, iron oxide, gallium oxide, indium oxide, and mixtures thereof can replace the alumina portion. Accordingly, the terms "zeolite", "zeolites" and "zeolite material", as used therein, shall mean not only materials containing silicon and, optionally, aluminum atoms in the crystalline lattice structure thereof, but also materials which contain suitable replacement atoms for such silicon and aluminum, such as gallosilicates, borosilicates, ferrosilicates, and the like.
The term "zeolite, "zeolites", and "zeolite materials" as used herein, besides encompassing the materials discussed above, shall also include aluminophosphate-based materials. Aluminophosphate zeolites are made of alternating A104 and P04 tetrahedra. Aluminophosphate-based materials have lower acidity compared to aluminosilicates. The lower acidity eliminates many side reactions, raises reactants' utilization, and extends catalyst life. Aluminophosphate-based zeolites are often abbreviated as ALPO. Substitution of silicon for P and/or a P-AI pair produces silicoaluminophosphate zeolites, abbreviated as SAPO.
Processes have been proposed for the production of xylenes by the methylation of toluene using a zeolite catalyst. For instance, U.S. Pat. No.
3,965,207 involves the methylation of toluene using a zeolite catalyst such as a ZSM-5. U.S. Pat. No. 4,670,616 involves the production of xylenes by the methylation of toluene with methanol using a borosilicate zeolite which is bound by a binder such as alumina, silica, or alumina-silica. One of the disadvantages of such processes is that catalysts deactivate rapidly due to build up of carbonaceous material and heavy by-products. Another disadvantage is that methanol selectivity to para-xylene, the desirable product, has been low, in the range of 50 to 60%. The balance is wasted on the production of coke and other undesirable compounds.
It has been further demonstrated that alkylaromatic compounds can be synthesized by reacting an aromatic compound such as toluene with a mixture of carbon dioxide (C02), and carbon monoxide (CO) and hydrogen (H2) (synthesis gas) at alkylation conditions in the presence of a catalyst system, which comprises (1 ) a composite of oxides of zinc, copper, chromium, and/or cadmium; and (2) an aluminosilicate material, either crystalline or amorphous, such as zeolites or clays; as disclosed in U.S.
Pat. Nos. 4,487,984 and 4,665,238. Such catalyst systems, however, are not capable of producing greater than equilibrium concentrations of para-xylene (PX) in the xylene-fraction product. Typically, the xylene-fraction product contains a mixture of xylene isomers at or near the equilibrium concentration, i.e., 24% PX, 54% MX, and 22% OX. The lack of para-xylene selectivity in alkylation of toluene with syngas can be caused by (1 ) the acidic sites on the surface outside the zeolite channels, and/or (2) the channel structure not being able to differentiate para-xylene from its isomers. It would be desirable for the toluene alkylation to be more para-selective due to the much higher value of PX compared to that of MX and OX. Furthermore, such processes suffer from catalyst deactivation as well.
In addition, the prior art disclosed neither syngas alkylation to alkyl aromatic compounds nor syngas selective alkylation to high purity PX
using aluminophosphate-based materials.
It has been recognized that certain zeolites can be modified to enhance their molecular-sieving or shape-selective capability. Such modification treatments are usually called zeolite selectivation.
Selectivated zeolites can more accurately differentiate molecules on the basis of molecular dimension or steric characteristics than the unselectivated precursors. For example, silanized ZSM-5 zeolites adsorbed PX much more preferentially over MX than untreated ZSM-5. It is believed that the deposition of silicon oxide onto zeolite surfaces from the silanization treatment has (1 ) passivated the active sites on the external surface of zeolite crystals, and (2) narrowed zeolitic pores to facilitate the passage of the smaller PX molecules and prevent the bigger MX and OX molecules from entering or exiting the pores. In this application, the term "para-alkyl selectivation" refers to modifying a catalyst or catalytic reaction system so that it preferentially forms more 08-06-2001 1 07:41A DI.M-Madan Mossman& Sriram 915 392 8805 US 00001300 pare-substituted dialkylbenzenes than the expected equilibrium proportions relative to the other isomers.
Zeolite selectivation can be accomplished using many techniques.
Reports of using compounds of silicon, phosphorous, boron, antimony, coke, magnesium, etc. for selectivation have been documented.
Unfortunately many, if not most of the zeolites used in the prior art have undesirably short active lifetimes before they deactivate and have to be reactivated or replaced.
U.S. Pat. No. 4,034,053 discusses a catalytic process for the selective production of pare-xylene by contacting, under conversion conditions, a charge stock containing, as a major reactant, at least one hydrocarbon selected from the group consisting of toluene, a C3-Coo olefin, and mixtures of the foregoing with a catalyst. The catalyst is a crystalline aluminosilicate zeolite having a silica to alumina ratio of at least about 12, a constraint index within the approximate range of 1 to 12 and which has combined therewith magnesium in an amount of at least about 0.5 percent by weight.
WPI Abstract AN 2000-114955 of RU-C-2119470 mentions increased selectivity in respect to dimethylnaphthalenes, andlor p-xylene and p-ethyltoluene when a toluenel2-methylnaphthalenelsynthesis gas mixture is brought into contact with a catalyst in the gas phase. The catalyst may be a zeolite of ZSM-5 type or ZSM-5 modified by silicon and magnesium compounds and metal oxide component containing 65-70%
zinc oxide, 29-34% chromium oxide, and 1 % tungsten at a zeolite/metal oxide ratio of 30-70:70-30.
WPI Abstract AN 1987-305992 of SU-A-1301485 discusses a catalyst that contains, in wt.%: Lanthanum 0.1-2.0 and decationised high silica-zeolite 98.0-99.9. The catalyst is prepared as follows: first the zeolite containing, in wt.%: AI203 3.1, SiOZ 91.2 and Na20 1.59 at SiOz/A1203 ratio equals 50.0; or AI203.3.65, Si02 90.4 and NazO 3.32, at SiOZ/A1203 ratio of 42.1, is subjected to two stage (first catalyst) or three-stage ~o isr~,v~rt. ~:'~~.~_~;~:o.i!E.t: :~:~
AMENDED SHEET
Cmnf,~vnsni~ Q Inni 1~~~Q
.08-06-2001 l 07:42A DLM-Madan Mossman& Sriram 915 392 8805 ~JS 00001300 4a (second catalyst) ion-exchange treatment with 1 N solution of ammonium chloride 96 ml NH;CI per 1 g of zeolite), to produce NH4 form of zeolite.
The obtained zeofite is washed with distilled water, dried and impregnated with a solution of lanthanum nitrate containing 0.0312 g La(N03)3.9H20 in 10 ml water for 1 day, dried in air.over 24 hours., then at 100°C for 2 hours and calcined at 500°C. Tests show that the proposed catalyst increases xylene conversion to 45% and selectivity of the process to 100%, as compared to 42 and 90% for the known catalyst containing no lanthanum.
Further, WO-A-90 09845 describes a mordenite-based cataiyzer for the isomerization of an aromatic C8 fraction characterized in that said mordenite contains at least one metal from the Ila, IVb, Ilb or IVa groups and is such that: its global atomic ratio SilAl is between 6 and 15, its sodium content by weight in relation to the dry mordenite weight is less than 2,000 ppm, its basic grain size volume is between 2,725 nm, its n-hexane adsorption capacity is above 0.065 cm~ liquid/gram, its isooctane adsorption capacity is less than 0.068 cm3 liquid/gram. The publication also concerns the preparation of mordenite by grafting on an H-shaped mordenite at least one organometallic composition of said metal.
A catalyst composition, a process for producing the catalyst composition, and a hydrocarbon conversion process for converting a fluid stream comprising at least one saturated hydrocarbon to C6 to C8 aromatic hydrocarbons such as benzene, toluene, and xylenes are disclosed in U.S.
Pat. No. 5,990,032. The catalyst composition comprises a zeolite and a promoter. The process for. producing the composition comprises the steps of: (1) combining a zeolite with a complexing ligand and a promoter compound under a condition sufficient to produce a modified zeolite; and (2) heating the modified zeolite to produce a promoted zelite. The hydrocarbon conversion process comprises contacting a fluid stream with the catalyst composition under a condition sufficient to effect the conversion of a saturated hydrocarbon to a C6 to Cs aromatic hydrocarbon.
~!~a~rvus,..~. ~~-rEv_~:.v !t.;y~~.f:. .W, AMENDED SHEET
FmnfanRe~ait R..Inni lS;dR
08-Ufi-2UU1 1 07:42A DLM-Madan Mossman& Srirarn 915 392 8805 US 00001300:
4b There remains a need for still further improved processes for catalytic PX synthesis which minimizes or avoids the disadvantages of prior systems, which include low PX selectivity, low methanol selectivity, rapid catalyst deactivation, and the like.
SUMMARY Ot~ THE II~,IEINTION
It is an object of the present invention to provide a method for producing a modified catalyst capable of being more selective to para-substituted dialkyl benzenes in the synthesis of dialkylbenzenes.
Accordingly, it is another object of the present invention to provide a modified catalyst useful in a method for synthesizing para-substituted dialkyl benzenes in high product concentration via alkylation of toluene andlor benzene with a mixture of gases including H2, and CO andlor C02 andlor methanol.
In canying out these and other objects of the invention, there is provided, in one form, a method for modifying catalysts involving contacting first component, such as crystalline or amorphous aluminosilicates, substituted aluminosilicates, substituted silicates, crystalline or amorphous alurninophosphates, zeolite-bound zeolites, substituted aluminophosphates, and mixtures thereof with an agent which may be compounds of elements selected from Groups 1 through 16, and mixtures thereof.
Sl.!EiSri-!'UTF S~f=~~'';i~~tl.;i..::. . , AMENDED SHEET
Cmnfonpovci+ Q liini 1~~AQ
WO 00/74847 PCT/iJS00/13003 DETAILED DESCRIPTION OF THE INVENTION
It has been discovered that catalysts, particularly zeolite catalysts, may be modified using organometallic compounds in such a way to 5 enhance selectivity to para-substituted alkyl benzenes in the synthesis of alkyl benzenes. It will be appreciated that the modified catalysts of this invention will find utility in catalyzing other reactions.
The improvement in para-substituted selectivity is achieved by treating the catalysts with proper chemical compounds of elements selected from Groups 1-16, and mixtures thereof, to (1 ) inhibit the external acidic sites to minimize aromatic alkylation on the non-para positions, and/or the isomerization of the para-substituted compounds, and/or (2) impose more restrictions on the channel structure to facilitate the formation and transport of para-substituted aromatic compounds, in one non-limiting explanation of the mechanism of the invention. It must be understood that such treatment may be performed on aluminophosphate catalyst reaction systems of this invention, but that some aluminophosphate catalyst reaction systems do not require this para-substituted selectivation treatment to be effective at para-substituent selectivation.
The catalytic reaction systems suitable for this invention include (1 ) a first component of one or more than one silicate-based materials, including but not necessarily limited to, crystalline or amorphous aluminosilicates, substituted aluminosilicates, substituted silicates, zeolite-bound zeolites, and/or crystalline or amorphous aluminophosphates, and/or substituted aluminophosphates and mixtures thereof, and, optionally (2) a second component of one or more than one of the metals or oxides of the metals selected from Groups 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, and 16 (new IUPAC notation, e.g. zinc, copper, chromium, cadmium, palladium, ruthenium, manganese, etc.). The first and second components may be chemically mixed, physically mixed, and combinations thereof, as will be described.
It has been further demonstrated that alkylaromatic compounds can be synthesized by reacting an aromatic compound such as toluene with a mixture of carbon dioxide (C02), and carbon monoxide (CO) and hydrogen (H2) (synthesis gas) at alkylation conditions in the presence of a catalyst system, which comprises (1 ) a composite of oxides of zinc, copper, chromium, and/or cadmium; and (2) an aluminosilicate material, either crystalline or amorphous, such as zeolites or clays; as disclosed in U.S.
Pat. Nos. 4,487,984 and 4,665,238. Such catalyst systems, however, are not capable of producing greater than equilibrium concentrations of para-xylene (PX) in the xylene-fraction product. Typically, the xylene-fraction product contains a mixture of xylene isomers at or near the equilibrium concentration, i.e., 24% PX, 54% MX, and 22% OX. The lack of para-xylene selectivity in alkylation of toluene with syngas can be caused by (1 ) the acidic sites on the surface outside the zeolite channels, and/or (2) the channel structure not being able to differentiate para-xylene from its isomers. It would be desirable for the toluene alkylation to be more para-selective due to the much higher value of PX compared to that of MX and OX. Furthermore, such processes suffer from catalyst deactivation as well.
In addition, the prior art disclosed neither syngas alkylation to alkyl aromatic compounds nor syngas selective alkylation to high purity PX
using aluminophosphate-based materials.
It has been recognized that certain zeolites can be modified to enhance their molecular-sieving or shape-selective capability. Such modification treatments are usually called zeolite selectivation.
Selectivated zeolites can more accurately differentiate molecules on the basis of molecular dimension or steric characteristics than the unselectivated precursors. For example, silanized ZSM-5 zeolites adsorbed PX much more preferentially over MX than untreated ZSM-5. It is believed that the deposition of silicon oxide onto zeolite surfaces from the silanization treatment has (1 ) passivated the active sites on the external surface of zeolite crystals, and (2) narrowed zeolitic pores to facilitate the passage of the smaller PX molecules and prevent the bigger MX and OX molecules from entering or exiting the pores. In this application, the term "para-alkyl selectivation" refers to modifying a catalyst or catalytic reaction system so that it preferentially forms more 08-06-2001 1 07:41A DI.M-Madan Mossman& Sriram 915 392 8805 US 00001300 pare-substituted dialkylbenzenes than the expected equilibrium proportions relative to the other isomers.
Zeolite selectivation can be accomplished using many techniques.
Reports of using compounds of silicon, phosphorous, boron, antimony, coke, magnesium, etc. for selectivation have been documented.
Unfortunately many, if not most of the zeolites used in the prior art have undesirably short active lifetimes before they deactivate and have to be reactivated or replaced.
U.S. Pat. No. 4,034,053 discusses a catalytic process for the selective production of pare-xylene by contacting, under conversion conditions, a charge stock containing, as a major reactant, at least one hydrocarbon selected from the group consisting of toluene, a C3-Coo olefin, and mixtures of the foregoing with a catalyst. The catalyst is a crystalline aluminosilicate zeolite having a silica to alumina ratio of at least about 12, a constraint index within the approximate range of 1 to 12 and which has combined therewith magnesium in an amount of at least about 0.5 percent by weight.
WPI Abstract AN 2000-114955 of RU-C-2119470 mentions increased selectivity in respect to dimethylnaphthalenes, andlor p-xylene and p-ethyltoluene when a toluenel2-methylnaphthalenelsynthesis gas mixture is brought into contact with a catalyst in the gas phase. The catalyst may be a zeolite of ZSM-5 type or ZSM-5 modified by silicon and magnesium compounds and metal oxide component containing 65-70%
zinc oxide, 29-34% chromium oxide, and 1 % tungsten at a zeolite/metal oxide ratio of 30-70:70-30.
WPI Abstract AN 1987-305992 of SU-A-1301485 discusses a catalyst that contains, in wt.%: Lanthanum 0.1-2.0 and decationised high silica-zeolite 98.0-99.9. The catalyst is prepared as follows: first the zeolite containing, in wt.%: AI203 3.1, SiOZ 91.2 and Na20 1.59 at SiOz/A1203 ratio equals 50.0; or AI203.3.65, Si02 90.4 and NazO 3.32, at SiOZ/A1203 ratio of 42.1, is subjected to two stage (first catalyst) or three-stage ~o isr~,v~rt. ~:'~~.~_~;~:o.i!E.t: :~:~
AMENDED SHEET
Cmnf,~vnsni~ Q Inni 1~~~Q
.08-06-2001 l 07:42A DLM-Madan Mossman& Sriram 915 392 8805 ~JS 00001300 4a (second catalyst) ion-exchange treatment with 1 N solution of ammonium chloride 96 ml NH;CI per 1 g of zeolite), to produce NH4 form of zeolite.
The obtained zeofite is washed with distilled water, dried and impregnated with a solution of lanthanum nitrate containing 0.0312 g La(N03)3.9H20 in 10 ml water for 1 day, dried in air.over 24 hours., then at 100°C for 2 hours and calcined at 500°C. Tests show that the proposed catalyst increases xylene conversion to 45% and selectivity of the process to 100%, as compared to 42 and 90% for the known catalyst containing no lanthanum.
Further, WO-A-90 09845 describes a mordenite-based cataiyzer for the isomerization of an aromatic C8 fraction characterized in that said mordenite contains at least one metal from the Ila, IVb, Ilb or IVa groups and is such that: its global atomic ratio SilAl is between 6 and 15, its sodium content by weight in relation to the dry mordenite weight is less than 2,000 ppm, its basic grain size volume is between 2,725 nm, its n-hexane adsorption capacity is above 0.065 cm~ liquid/gram, its isooctane adsorption capacity is less than 0.068 cm3 liquid/gram. The publication also concerns the preparation of mordenite by grafting on an H-shaped mordenite at least one organometallic composition of said metal.
A catalyst composition, a process for producing the catalyst composition, and a hydrocarbon conversion process for converting a fluid stream comprising at least one saturated hydrocarbon to C6 to C8 aromatic hydrocarbons such as benzene, toluene, and xylenes are disclosed in U.S.
Pat. No. 5,990,032. The catalyst composition comprises a zeolite and a promoter. The process for. producing the composition comprises the steps of: (1) combining a zeolite with a complexing ligand and a promoter compound under a condition sufficient to produce a modified zeolite; and (2) heating the modified zeolite to produce a promoted zelite. The hydrocarbon conversion process comprises contacting a fluid stream with the catalyst composition under a condition sufficient to effect the conversion of a saturated hydrocarbon to a C6 to Cs aromatic hydrocarbon.
~!~a~rvus,..~. ~~-rEv_~:.v !t.;y~~.f:. .W, AMENDED SHEET
FmnfanRe~ait R..Inni lS;dR
08-Ufi-2UU1 1 07:42A DLM-Madan Mossman& Srirarn 915 392 8805 US 00001300:
4b There remains a need for still further improved processes for catalytic PX synthesis which minimizes or avoids the disadvantages of prior systems, which include low PX selectivity, low methanol selectivity, rapid catalyst deactivation, and the like.
SUMMARY Ot~ THE II~,IEINTION
It is an object of the present invention to provide a method for producing a modified catalyst capable of being more selective to para-substituted dialkyl benzenes in the synthesis of dialkylbenzenes.
Accordingly, it is another object of the present invention to provide a modified catalyst useful in a method for synthesizing para-substituted dialkyl benzenes in high product concentration via alkylation of toluene andlor benzene with a mixture of gases including H2, and CO andlor C02 andlor methanol.
In canying out these and other objects of the invention, there is provided, in one form, a method for modifying catalysts involving contacting first component, such as crystalline or amorphous aluminosilicates, substituted aluminosilicates, substituted silicates, crystalline or amorphous alurninophosphates, zeolite-bound zeolites, substituted aluminophosphates, and mixtures thereof with an agent which may be compounds of elements selected from Groups 1 through 16, and mixtures thereof.
Sl.!EiSri-!'UTF S~f=~~'';i~~tl.;i..::. . , AMENDED SHEET
Cmnfonpovci+ Q liini 1~~AQ
WO 00/74847 PCT/iJS00/13003 DETAILED DESCRIPTION OF THE INVENTION
It has been discovered that catalysts, particularly zeolite catalysts, may be modified using organometallic compounds in such a way to 5 enhance selectivity to para-substituted alkyl benzenes in the synthesis of alkyl benzenes. It will be appreciated that the modified catalysts of this invention will find utility in catalyzing other reactions.
The improvement in para-substituted selectivity is achieved by treating the catalysts with proper chemical compounds of elements selected from Groups 1-16, and mixtures thereof, to (1 ) inhibit the external acidic sites to minimize aromatic alkylation on the non-para positions, and/or the isomerization of the para-substituted compounds, and/or (2) impose more restrictions on the channel structure to facilitate the formation and transport of para-substituted aromatic compounds, in one non-limiting explanation of the mechanism of the invention. It must be understood that such treatment may be performed on aluminophosphate catalyst reaction systems of this invention, but that some aluminophosphate catalyst reaction systems do not require this para-substituted selectivation treatment to be effective at para-substituent selectivation.
The catalytic reaction systems suitable for this invention include (1 ) a first component of one or more than one silicate-based materials, including but not necessarily limited to, crystalline or amorphous aluminosilicates, substituted aluminosilicates, substituted silicates, zeolite-bound zeolites, and/or crystalline or amorphous aluminophosphates, and/or substituted aluminophosphates and mixtures thereof, and, optionally (2) a second component of one or more than one of the metals or oxides of the metals selected from Groups 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, and 16 (new IUPAC notation, e.g. zinc, copper, chromium, cadmium, palladium, ruthenium, manganese, etc.). The first and second components may be chemically mixed, physically mixed, and combinations thereof, as will be described.
The composition of the proposed catalyst reaction systems may range from 95 wt.% silicate-based material or aluminophosphate-based material first component/5 wt.% metals or metal oxides second component, if present, to 5 wt.% silicate-based material or aluminophosphate-based material first component/95 wt.% metals or metal oxides second component, if present.
It will be understood that the selectivation techniques of this invention may be practiced before or after the silicate-based materials or aluminophosphate-based materials are mixed with or combined chemically or physically with metals or metal oxides, if used. That is, in some embodiments, the silicate-based materials and aluminophosphate-based materials may be selectivated before combination with metals or metal oxides. In other embodiments, silicate-based materials and aluminophosphate-based materials may be selectivated after combination with metals or metal oxides. The former process might be termed "pre-selectivation", while the latter process may be termed "post-selectivation".
One type of the zeolite materials would be silicate-based zeolites such as faujasites, morden~ites, pentasils, etc.
Zeolite materials suitable for this invention include silicate-based zeolites and amorphous compounds. Silicate-based zeolites are made of alternating Si02 and MOX tetrahedra, where in the formula M is an element selected from the Groups 1 through 16 of the Periodic Table (new IUPAC).
These types of zeolites have 8-, 10-, or 12-membered oxygen ring channels. Silicate-based materials are generally acidic. The more preferred zeolites of this invention include 10- and 12-membered ring zeolites, such as ZSM-5, ZSM-11, ZSM-22, ZSM-48, ZSM-57, etc.
One of the disadvantages to the use of many unselectivated silicate-based materials for such para-substituted synthesis systems is the lack of product selectivity (i.e. an undesirably broad product distribution results). The acidity of many aluminosilicates are sufficiently high that they often promote many undesirable side reactions (e.g. dealkylation, multi-alkylation, oligomerization, and condensation) which deactivate the catalysts and lower the product value. It follows that silicate-based materials are typically not capable of delivering the shape selectivity for increasing the yield for high-value products such as para-xylene (PX).
Some of the silicate-based materials have one-dimensional channel structures, which are capable of generating higher-than-equilibrium PX
selectivity. These materials may optionally be para-substituent selectivated. Other silicate-based materials having two- or three-dimensional channel structures are preferably para- substituent selectivated or modified to be more selective through the use of certain chemical compounds, as will be described, such as organometallic compounds and compounds of elements selected from Groups 1-16. In one embodiment, the selectivation of the zeolite materials including the silicate-based materials can be accomplished using compounds including, but not necessarily limited to silicon, phosphorus, boron, antimony, magnesium compounds, coke, and the like, and mixtures thereof.
Other silicate-based materials suitable for the second component include zeolite bound zeolites as described in WO 97/45387. Zeolite bound zeolite catalysts useful in the present invention concern first crystals of an acidic intermediate pore size first zeolite and a binder comprising second crystals of a second zeolite. Unlike zeolites bound with amorphous material such as silica or alumina to enhance the mechanical strength of the zeolite, the zeolite bound zeolite catalyst suitable for use in the present process does not contain significant amounts of non-zeolitic binders.
The first zeolite used in the zeolite bound zeolite catalyst is an intermediate pore size zeolite. Intermediate pore size zeolites have a pore size from about 5 to about 7 A and include, for example, AEL, MFI, MEL, MFS, MEI, MTW, EUO, MTT, HEU, FER, and TON structure type zeolites.
These zeolites are described in Atlas of Zeolite Structure Types, eds. W.
H. Meier and D. H. Olson, Butterworth-Heineman, Third Edition, 1992.
Examples of specific intermediate pore size zeolites include, but are not limited to, ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-34, ZSM-35, ZSM-38, ZSM-48, ZSM-50, and ZSM-57. Preferred first zeolites are galliumsilicate zeolites having an MFI structure and aluminosilicate zeolites having an MFR structure.
The second zeolite will usually have an intermediate pore size and have less activity than the first zeolite. Preferably, the second zeolite will be substantially non-acidic and will have the same structure type as the first zeolite. The preferred second zeolites are aluminosilicate zeolites having a silica to alumina mole ratio greater than 100 such as low acidity ZSM-5. If the second zeolite is an aluminosilicate zeolite, the second zeolite will generally have a silica to alumina mole ratio greater than 200:1, e.g., 500:1; 1,000:1, etc., and in some applications will contain no more than trace amounts of alumina. The second zeolite can also be silicalite, i.e., a MFI type substantially free of alumina, or silicalite 2, a MEL type substantially free of alumina. The second zeolite is usually present in the zeolite bound zeolite catalyst in an amount in the range of from about 10%
to 60% by weight based on the weight of the first zeolite and, more preferably, from about 20% to about 50% by weight.
The second zeolite crystals preferably have a smaller size than the first zeolite crystals and more preferably will have an average particle size from about 0.1 to about 0.5 microns. The second zeolite crystals, in addition to binding the first zeolite particles and maximizing the performance of the catalyst will preferably intergrow and form an over-growth which coats or partially coats the first zeolite crystals. Preferably, the crystals will be resistant to attrition.
The zeolite bound zeolite catalyst suitable for the process of the present invention is preferably prepared by a three step procedure. The first step involves the synthesis of the first zeolite crystals prior to converting it to the zeolite bound zeolite catalyst. Next, a silica-bound aluminosilicate zeolite can be prepared preferably by mixing a mixture comprising the aluminosilicate crystals, a silica gel or sol, water and optionally an extrusion aid and, optionally, the metal component until a homogeneous composition in the form of an extrudable paste develops.
It will be understood that the selectivation techniques of this invention may be practiced before or after the silicate-based materials or aluminophosphate-based materials are mixed with or combined chemically or physically with metals or metal oxides, if used. That is, in some embodiments, the silicate-based materials and aluminophosphate-based materials may be selectivated before combination with metals or metal oxides. In other embodiments, silicate-based materials and aluminophosphate-based materials may be selectivated after combination with metals or metal oxides. The former process might be termed "pre-selectivation", while the latter process may be termed "post-selectivation".
One type of the zeolite materials would be silicate-based zeolites such as faujasites, morden~ites, pentasils, etc.
Zeolite materials suitable for this invention include silicate-based zeolites and amorphous compounds. Silicate-based zeolites are made of alternating Si02 and MOX tetrahedra, where in the formula M is an element selected from the Groups 1 through 16 of the Periodic Table (new IUPAC).
These types of zeolites have 8-, 10-, or 12-membered oxygen ring channels. Silicate-based materials are generally acidic. The more preferred zeolites of this invention include 10- and 12-membered ring zeolites, such as ZSM-5, ZSM-11, ZSM-22, ZSM-48, ZSM-57, etc.
One of the disadvantages to the use of many unselectivated silicate-based materials for such para-substituted synthesis systems is the lack of product selectivity (i.e. an undesirably broad product distribution results). The acidity of many aluminosilicates are sufficiently high that they often promote many undesirable side reactions (e.g. dealkylation, multi-alkylation, oligomerization, and condensation) which deactivate the catalysts and lower the product value. It follows that silicate-based materials are typically not capable of delivering the shape selectivity for increasing the yield for high-value products such as para-xylene (PX).
Some of the silicate-based materials have one-dimensional channel structures, which are capable of generating higher-than-equilibrium PX
selectivity. These materials may optionally be para-substituent selectivated. Other silicate-based materials having two- or three-dimensional channel structures are preferably para- substituent selectivated or modified to be more selective through the use of certain chemical compounds, as will be described, such as organometallic compounds and compounds of elements selected from Groups 1-16. In one embodiment, the selectivation of the zeolite materials including the silicate-based materials can be accomplished using compounds including, but not necessarily limited to silicon, phosphorus, boron, antimony, magnesium compounds, coke, and the like, and mixtures thereof.
Other silicate-based materials suitable for the second component include zeolite bound zeolites as described in WO 97/45387. Zeolite bound zeolite catalysts useful in the present invention concern first crystals of an acidic intermediate pore size first zeolite and a binder comprising second crystals of a second zeolite. Unlike zeolites bound with amorphous material such as silica or alumina to enhance the mechanical strength of the zeolite, the zeolite bound zeolite catalyst suitable for use in the present process does not contain significant amounts of non-zeolitic binders.
The first zeolite used in the zeolite bound zeolite catalyst is an intermediate pore size zeolite. Intermediate pore size zeolites have a pore size from about 5 to about 7 A and include, for example, AEL, MFI, MEL, MFS, MEI, MTW, EUO, MTT, HEU, FER, and TON structure type zeolites.
These zeolites are described in Atlas of Zeolite Structure Types, eds. W.
H. Meier and D. H. Olson, Butterworth-Heineman, Third Edition, 1992.
Examples of specific intermediate pore size zeolites include, but are not limited to, ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-34, ZSM-35, ZSM-38, ZSM-48, ZSM-50, and ZSM-57. Preferred first zeolites are galliumsilicate zeolites having an MFI structure and aluminosilicate zeolites having an MFR structure.
The second zeolite will usually have an intermediate pore size and have less activity than the first zeolite. Preferably, the second zeolite will be substantially non-acidic and will have the same structure type as the first zeolite. The preferred second zeolites are aluminosilicate zeolites having a silica to alumina mole ratio greater than 100 such as low acidity ZSM-5. If the second zeolite is an aluminosilicate zeolite, the second zeolite will generally have a silica to alumina mole ratio greater than 200:1, e.g., 500:1; 1,000:1, etc., and in some applications will contain no more than trace amounts of alumina. The second zeolite can also be silicalite, i.e., a MFI type substantially free of alumina, or silicalite 2, a MEL type substantially free of alumina. The second zeolite is usually present in the zeolite bound zeolite catalyst in an amount in the range of from about 10%
to 60% by weight based on the weight of the first zeolite and, more preferably, from about 20% to about 50% by weight.
The second zeolite crystals preferably have a smaller size than the first zeolite crystals and more preferably will have an average particle size from about 0.1 to about 0.5 microns. The second zeolite crystals, in addition to binding the first zeolite particles and maximizing the performance of the catalyst will preferably intergrow and form an over-growth which coats or partially coats the first zeolite crystals. Preferably, the crystals will be resistant to attrition.
The zeolite bound zeolite catalyst suitable for the process of the present invention is preferably prepared by a three step procedure. The first step involves the synthesis of the first zeolite crystals prior to converting it to the zeolite bound zeolite catalyst. Next, a silica-bound aluminosilicate zeolite can be prepared preferably by mixing a mixture comprising the aluminosilicate crystals, a silica gel or sol, water and optionally an extrusion aid and, optionally, the metal component until a homogeneous composition in the form of an extrudable paste develops.
The final step is the conversion of the silica present in the silica-bound catalyst to a second zeolite which serves to bind the first zeolite crystals together.
As noted, aluminophosphate-based materials may be used in conjunction with metal oxides for aromatic alkylation with syngas.
Aluminophosphate-based materials usually have lower acidity compared to silicate-based materials. The lower acidity eliminates many side reactions, raises reactants' utilization, and extends catalyst life.
Further catalytic reaction systems suitable for this invention include aluminophosphate-based materials and amorphous compounds.
Aluminophosphate-based materials are made of alternating A104 and P04 tetrahedra. Members of this family have 8- (e.g. AIP04-12, -17, -21, -25, -34, -42, etc.), 10- (e.g. AIP04-11, 41, etc.), or 12- (AIP04-5, -31, etc.) membered oxygen ring channels. Although AIP04s are neutral, substitution of AI and/or P by cations with lower charge introduces a negative charge in the framework, which is countered by cations imparting acidity.
By turn, substitution of silicon for P and/or a P-AI pair turns the neutral binary composition (i.e. AI, P) into a series of acidic-ternary-composition (Si, AI, P) based SAPO molecular sieves, such as SAPO-5, -11, -14, -17, -18, -20, -31, -34, -41, -46, etc. Acidic ternary compositions can also be created by substituting divalent metal ions for aluminum, generating the MeAPO materials. Me is a metal ion which can be selected from the group consisting of, but not limited to, Mg, Co, Fe, Zn and the like. Acidic materials such as MgAPO (magnesium substituted), CoAPO
(cobalt substituted), FeAPO (iron substituted), MnAPO (manganese substituted), ZnAPO (zinc substituted) etc. belong to this category.
Substitution can also create acidic quaternary-composition based materials such as the MeAPSO series, including FeAPSO (Fe, AI, P, and Si), MgAPSO (Mg, AI, P, Si), MnAPSO, CoAPSO, ZnAPSO (Zn, AI, P, Si), etc. Other substituted aluminophosphate-based materials include EIAPO
and EIAPSO (where EI = B, As, Be, Ga, Ge, Li, Ti, etc.) As mentioned above, these materials have the appropriate acidic strength for syngas/aromatic alkylation. Some preferred aluminophosphate-based materials of this invention include 10- and 12-membered ring molecular sieves (SAPO-11, -31, -41; MeAPO-11, -31, -41; MeAPSO-11, -31, 41;
5 EIAPO-11, -31, -41; EIAPSO-11, -31, -41, etc.) which already have significant shape selectivity due to their narrow channel structure.
These aluminophosphates may be para-alkyl selectivated or modified to be more selective through the use of certain chemical compounds, as will be described, such as organometallic compounds and 10 compounds of elements selected from Groups 1-16. In one embodiment, the para-alkyl selectivation of the zeolite materials including the aluminophosphate-based materials can be accomplished using compounds including, but not necessarily limited to silicon, phosphorus, boron, antimony, magnesium compounds, coke, and the like, and mixtures thereof.
The preparation of the catalytic reaction systems can be accomplished with several techniques known to those skilled in the art.
Some examples are given below.
Para-selectivation involves the treatment of the above mentioned catalytic reaction system materials with proper chemical compounds of elements selected from Groups 1-16, and mixtures thereof. The composition of the selectivated catalyst may range from 1 wt.% of the selectivating elements/99 wt.% of the first component to 99 wt.% of the selectivating elements/1 wt.% of the first component. By "selectivating elements" is meant the elemental portion of the elemental form or elemental oxide form of the selectivating chemical compounds.
Some para-substituent selectivation treatments are known, e.g.
using silicon compounds. Other compounds that may be used include, but are not limited to compounds of phosphorus, boron, antimony, magnesium, and the like, and coke, and the like. Para-substituent selectivation treatments of the materials of the above catalytic reaction systems can be carried out either prior to the selective formation of PX (ex situ) or during the PX formation (in situ), to use PX formation as a non-limiting example. In the in situ embodiment, the selectivating agents are added with the feed to the reactor containing a catalytic reaction system.
In more detail, in one non-limiting embodiment, the technique for selectivating the materials according to the method of this invention is based on the consideration that by depositing on a silicate-based material or aluminophosphate-based material one or more than one of the organometallic compounds which are too bulky to enter the channels (or other selectivating agent), one should be able to modify only the external surface and regions around channel mouth. The fact that the selectivation agent does not enter the channels preserves the active sites inside the channels. Since the channel active sites account for more the majority of the total active sites, their remaining active prevents any significant loss of reactivity or conversion.
One type of the bulky organometallic compounds suitable for selectivating 10-member-ring zeolites, such the ZSM family (e.g. ZSM-5, -11, -22, -48, etc.), mordenite, etc., is the salts of large organic anions and metallic cations. The organic anions can be selected from molecules containing carboxylic and/or phenolic functional groups, including but not limited to phthalate, ethylenediaminetetraacetic acid (EDTA), vitamin B-5, trihydroxy benzoic acid, pyrogallate, salicylate, sulfosalicylate, citrate, naphthalene dicarboxylate, anthradiolate, camphorate, and others. The metallic cations can be selected from the elements) of Groups 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, and 16 (new IUPAC notation). Other compounds for selectivating the silicate-based and aluminophosphate-based materials include, but are not necessarily limited to silicon, phosphorus, boron, antimony, magnesium compounds, coke, and the like, and mixtures thereof.
Selectivation of silicate-based materials and aluminophosphate-based materials with the above-mentioned organometallic salts can be accomplished by various means. For example, one can use impregnation of a solution of an organometallic salt onto a silicate-based material or aluminophosphate-based material. Either water or any suitable organic solvent can be used. Addition of non-metallic salts and/or adjustments of pH to facilitate the treatment are optional. Heat will be provided to drive off the solvent, leaving behind a material coated homogeneously with the organometallic salt. Drying and calcination of the coated zeolite or aluminophosphate-based material at appropriate temperatures will turn the salt into metal oxide form or elemental metal form (agent derivative).
Alternatively, one can use a dry-mix technique, which involves mixing directly a zeolite in the form of powder or particles with an organometallic salt also in the form of powder or particles without the use of any solvent.
The mixture will then be subjected to heat treatment, which facilitates the dispersion of the salt over the material and eventually turns the salt into elemental form or metal oxide form (agent derivative).
Known techniques for ex situ and in situ catalytic reaction system modification can be incorporated into producing the para-alkyl selectivated catalytic reaction systems of the present invention in addition to those herewith, such as those seen in U.S. Pat. Nos. 5,476,823 and 5,675,047.
In one embodiment, the same elemental metals and/or metal oxide second components used in the catalytic reaction system can be used alone or together to selectivate the silicate-based material or aluminophosphate-based material components.
The catalytic reaction systems can be prepared by adding solutions of elemental metal salts either in series to or as a mixture with the fine powder or particles such as extrudates, spheres, etc. of the unselectivated silicate-based materials having one dimensional channel structures, or optionally ex situ selectivated silicate-based materials, unselectivated aluminophosphate-based materials, or optionally ex situ selectivated aluminophosphate-based materials, until incipient wetness is reached. The solvent (water or other solvents) can be evacuated under heat or vacuum using typical equipment such as a rotary evaporator. The final product is dried, calcined, and pelletized, if necessary.
As noted, aluminophosphate-based materials may be used in conjunction with metal oxides for aromatic alkylation with syngas.
Aluminophosphate-based materials usually have lower acidity compared to silicate-based materials. The lower acidity eliminates many side reactions, raises reactants' utilization, and extends catalyst life.
Further catalytic reaction systems suitable for this invention include aluminophosphate-based materials and amorphous compounds.
Aluminophosphate-based materials are made of alternating A104 and P04 tetrahedra. Members of this family have 8- (e.g. AIP04-12, -17, -21, -25, -34, -42, etc.), 10- (e.g. AIP04-11, 41, etc.), or 12- (AIP04-5, -31, etc.) membered oxygen ring channels. Although AIP04s are neutral, substitution of AI and/or P by cations with lower charge introduces a negative charge in the framework, which is countered by cations imparting acidity.
By turn, substitution of silicon for P and/or a P-AI pair turns the neutral binary composition (i.e. AI, P) into a series of acidic-ternary-composition (Si, AI, P) based SAPO molecular sieves, such as SAPO-5, -11, -14, -17, -18, -20, -31, -34, -41, -46, etc. Acidic ternary compositions can also be created by substituting divalent metal ions for aluminum, generating the MeAPO materials. Me is a metal ion which can be selected from the group consisting of, but not limited to, Mg, Co, Fe, Zn and the like. Acidic materials such as MgAPO (magnesium substituted), CoAPO
(cobalt substituted), FeAPO (iron substituted), MnAPO (manganese substituted), ZnAPO (zinc substituted) etc. belong to this category.
Substitution can also create acidic quaternary-composition based materials such as the MeAPSO series, including FeAPSO (Fe, AI, P, and Si), MgAPSO (Mg, AI, P, Si), MnAPSO, CoAPSO, ZnAPSO (Zn, AI, P, Si), etc. Other substituted aluminophosphate-based materials include EIAPO
and EIAPSO (where EI = B, As, Be, Ga, Ge, Li, Ti, etc.) As mentioned above, these materials have the appropriate acidic strength for syngas/aromatic alkylation. Some preferred aluminophosphate-based materials of this invention include 10- and 12-membered ring molecular sieves (SAPO-11, -31, -41; MeAPO-11, -31, -41; MeAPSO-11, -31, 41;
5 EIAPO-11, -31, -41; EIAPSO-11, -31, -41, etc.) which already have significant shape selectivity due to their narrow channel structure.
These aluminophosphates may be para-alkyl selectivated or modified to be more selective through the use of certain chemical compounds, as will be described, such as organometallic compounds and 10 compounds of elements selected from Groups 1-16. In one embodiment, the para-alkyl selectivation of the zeolite materials including the aluminophosphate-based materials can be accomplished using compounds including, but not necessarily limited to silicon, phosphorus, boron, antimony, magnesium compounds, coke, and the like, and mixtures thereof.
The preparation of the catalytic reaction systems can be accomplished with several techniques known to those skilled in the art.
Some examples are given below.
Para-selectivation involves the treatment of the above mentioned catalytic reaction system materials with proper chemical compounds of elements selected from Groups 1-16, and mixtures thereof. The composition of the selectivated catalyst may range from 1 wt.% of the selectivating elements/99 wt.% of the first component to 99 wt.% of the selectivating elements/1 wt.% of the first component. By "selectivating elements" is meant the elemental portion of the elemental form or elemental oxide form of the selectivating chemical compounds.
Some para-substituent selectivation treatments are known, e.g.
using silicon compounds. Other compounds that may be used include, but are not limited to compounds of phosphorus, boron, antimony, magnesium, and the like, and coke, and the like. Para-substituent selectivation treatments of the materials of the above catalytic reaction systems can be carried out either prior to the selective formation of PX (ex situ) or during the PX formation (in situ), to use PX formation as a non-limiting example. In the in situ embodiment, the selectivating agents are added with the feed to the reactor containing a catalytic reaction system.
In more detail, in one non-limiting embodiment, the technique for selectivating the materials according to the method of this invention is based on the consideration that by depositing on a silicate-based material or aluminophosphate-based material one or more than one of the organometallic compounds which are too bulky to enter the channels (or other selectivating agent), one should be able to modify only the external surface and regions around channel mouth. The fact that the selectivation agent does not enter the channels preserves the active sites inside the channels. Since the channel active sites account for more the majority of the total active sites, their remaining active prevents any significant loss of reactivity or conversion.
One type of the bulky organometallic compounds suitable for selectivating 10-member-ring zeolites, such the ZSM family (e.g. ZSM-5, -11, -22, -48, etc.), mordenite, etc., is the salts of large organic anions and metallic cations. The organic anions can be selected from molecules containing carboxylic and/or phenolic functional groups, including but not limited to phthalate, ethylenediaminetetraacetic acid (EDTA), vitamin B-5, trihydroxy benzoic acid, pyrogallate, salicylate, sulfosalicylate, citrate, naphthalene dicarboxylate, anthradiolate, camphorate, and others. The metallic cations can be selected from the elements) of Groups 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, and 16 (new IUPAC notation). Other compounds for selectivating the silicate-based and aluminophosphate-based materials include, but are not necessarily limited to silicon, phosphorus, boron, antimony, magnesium compounds, coke, and the like, and mixtures thereof.
Selectivation of silicate-based materials and aluminophosphate-based materials with the above-mentioned organometallic salts can be accomplished by various means. For example, one can use impregnation of a solution of an organometallic salt onto a silicate-based material or aluminophosphate-based material. Either water or any suitable organic solvent can be used. Addition of non-metallic salts and/or adjustments of pH to facilitate the treatment are optional. Heat will be provided to drive off the solvent, leaving behind a material coated homogeneously with the organometallic salt. Drying and calcination of the coated zeolite or aluminophosphate-based material at appropriate temperatures will turn the salt into metal oxide form or elemental metal form (agent derivative).
Alternatively, one can use a dry-mix technique, which involves mixing directly a zeolite in the form of powder or particles with an organometallic salt also in the form of powder or particles without the use of any solvent.
The mixture will then be subjected to heat treatment, which facilitates the dispersion of the salt over the material and eventually turns the salt into elemental form or metal oxide form (agent derivative).
Known techniques for ex situ and in situ catalytic reaction system modification can be incorporated into producing the para-alkyl selectivated catalytic reaction systems of the present invention in addition to those herewith, such as those seen in U.S. Pat. Nos. 5,476,823 and 5,675,047.
In one embodiment, the same elemental metals and/or metal oxide second components used in the catalytic reaction system can be used alone or together to selectivate the silicate-based material or aluminophosphate-based material components.
The catalytic reaction systems can be prepared by adding solutions of elemental metal salts either in series to or as a mixture with the fine powder or particles such as extrudates, spheres, etc. of the unselectivated silicate-based materials having one dimensional channel structures, or optionally ex situ selectivated silicate-based materials, unselectivated aluminophosphate-based materials, or optionally ex situ selectivated aluminophosphate-based materials, until incipient wetness is reached. The solvent (water or other solvents) can be evacuated under heat or vacuum using typical equipment such as a rotary evaporator. The final product is dried, calcined, and pelletized, if necessary.
Alternatively, solutions of metal salts and the ex situ selectivated fine powder or particles such as extrudates, spheres, etc. of silicate-based and aluminophosphate-based materials are thoroughly mixed. A dilute basic solution (e.g. ammonia, sodium carbonate, potassium hydroxide, etc.) is used to adjust the pH value of the mixture to facilitate the precipitation of metal hydroxides and zeolites. The precipitate is filtered and washed thoroughly with water. The final product is dried, calcined, and pelletized, if necessary.
The catalytic reaction systems can also be prepared using physical mixing. Finely divided powders of metals) or metal oxide(s), or powders of metals) or metal oxides) supported on any inert materials, are mixed thoroughly with finely divided powder of the ex situ selectivated silicate-based materials, unselectivated aluminophosphate-based materials, or optionally ex situ selectivated aluminophosphate-based materials in a blending machine or a grinding mortar. The mixture is optionally pelletized before use.
If the catalytic reaction system is mixed with a binder, such as silica gel or sol or the like, an extrudable paste may be formed. The resulting paste can be molded, e.g. extruded, and cut into small strands which can then be dried and calcined.
The catalytic reaction system can also be prepared by mixing physically the particles of silicate-based material or aluminophosphate-based materials components and the particles of the metal and/or metal oxide second components, if present. The same metals and/or metal oxides can also be used alone or together to selectivate catalytic reaction systems and thus simultaneously catalyze syngas and/or other reactions.
The catalytic reaction system can also be formed by packing the first and the second components, if present, in a stacked-bed manner with some of the first component in front of the physical or chemical mixture of the first and second components.
Prior to exposing the catalysts to the feed components of toluene and/or benzene, H2, CO, and/or C02 and/or methanol, the catalyst reaction systems can optionally be activated under a reducing environment (e.g. 1-80% H2 in N2) at 150-500°C, and 1-200 atm (1.01 x 105 - 2.03 x 10' Pa) for 2-48 hours.
The average crystal size of the crystals in the silicate-based material or aluminophosphate-based materials is preferably from above 0.1 micron to about 100 microns, more preferably from about 1 micron to about 100 microns.
Procedures to determine crystal size are known to persons skilled in the art. For instance, crystal size may be determined directly by taking a suitable scanning electron microscope (SEM) picture of a representative sample of the crystals.
The catalysts of this invention may be used in a methylation process which can be carried out as a batch type, semi-continuous or continuous operation utilizing a fixed or moving bed catalyst system.
Multiple injection of the methylating agent may be employed. The methylating agent includes CO, C02 and H2 and/or CH30H and derivatives thereof. The methylating agent reacts with benzene to form toluene. Toluene reacts with the methylating agent to form a xylene, preferably PX in this invention.
Toluene and/or benzene and the methylating agents) are usually premixed and fed together into the reaction vessel to maintain the desired ratio between them with no local concentration of either reactant to disrupt reaction kinetics. Individual feeds can be employed, however, if care is taken to insure good mixing of the reactant vapors in the reaction vessel.
Optionally, instantaneous concentration of methylating agent can be kept low by staged additions thereof. By staged additions, the ratios of toluene and/or benzene to methylating agent concentrations can be maintained at optimum levels to give good toluene conversions. Hydrogen gas can also serve as an anticoking agent and diluent.
The method of this invention, particularly when using para-substituent selectivated catalytic reaction systems, stabilizes catalytic reaction system performance and increases catalytic reaction system life.
That is, catalytic reaction system deactivation is slowed and even prevented. With properly para- substituent selectivated catalytic reaction systems, it is expected that the catalytic reaction system may not have to be regenerated at all. This is in part due to the silicate-based materials 5 and aluminophosphate-based materials being para- substituent selectivated. With production selective to PX, in one non-limiting instance, less by-products, such as heavy aromatics, are formed which would deactivate the catalytic reaction systems. This characteristic is not shown or taught by the prior art.
10 Further, in one non-limiting embodiment of the invention, there is a belief that the catalytic reaction systems of this invention have the capability of preventing or reducing the side reactions of the methylating agents with themselves, and in particular that the para- substituent selectivated catalytic reaction systems function to catalyze more than one 15 reaction, that is, that a syngas reaction is catalyzed to form methylating agents which react with benzene and/or toluene to produce PX, e.g.
However, because the methylating agent is produced on a local, molecular scale, its concentrations are very low (as contrasted with feeding a methylating agent as a co-reactant). It has been demonstrated that feeding a blend of methylating agent and toluene to make PX
increases coke build-up and hence catalytic reaction system deactivation.
In one non-limiting embodiment of the invention, the catalyst activity decrease is less than 0.5% toluene and/or benzene conversion per day, preferably less than 0.1 %, In carrying out the PX synthesis process, the feed mixtures can be co-fed into a reactor containing one of the above mentioned catalytic reaction systems. The catalytic reaction system and reactants can be heated to reaction temperatures separately or together. Reaction can be carried out at a temperature from about 100-700°C, preferably from about 200-600°C; at a pressure from about 1-300 atm (1.01 x 105-3.04 x 10' Pa), preferably from about 1-200 atm (1.01 x 105-2.03 x 10' Pa); and at a flow rate from about 0.01-100 h-' LHSV, preferably from about 1-50 h-' LHSV on a liquid feed basis. The composition of the feed, i.e. the mole ratio of H2/CO(and/or C02)/aromatic can be from of about 0.01-10/0.01-10/0.01-10, preferably from about 0.1-10/0.1-10/0.1-10.
As noted, typical methylating agents include or are formed from, but are not necessarily limited to hydrogen together with carbon monoxide and/or carbon monoxide, and/or methanol, but also dimethylether, methylchloride, methylbromide, and dimethylsulfide.
It is conceivable that in the scenarios described above, the toluene can be pure, or in a mixture with benzene. The benzene may alkylate to toluene, and/or ultimately to PX, with or without recycle. The presence of benzene may also enhance heat and/or selectivity control.
The PX method is expected to tolerate many different kinds of feed.
Unextracted toluene, which is a mixture of toluene and similar boiling range olefins and paraffins, is preferred in one embodiment. For example, premium extracted toluene, essentially pure toluene, and extracted aromatics, essentially a relatively pure mixture of toluene and benzene, may also be used. Unextracted toluene and benzene which contains toluene, benzene, and olefins and paraffins that boil in a similar range to that of toluene or benzene, may also be employed. When unextracted feedstocks are used, it is important to crack the paraffins and olefins into lighter products that can be easily distilled. For example, the feed may contain one or more paraffins and/or olefins having at least 4 carbon atoms; the catalytic reaction systems have the dual function to crack the paraffins and/or olefins and methylate benzene or toluene to selectively produce PX.
Indeed, some of the catalytic reaction systems of this invention may be multifunctional in some embodiments, catalyzing a reaction or reactions of CO, H2, and/or C02 and/or methanol to produce a methylating agent, catalyzing the selective methylation of toluene and/or benzene to produce PX, and catalyzing the cracking of paraffins and olefins into relatively lighter products.
The catalytic reaction systems can also be prepared using physical mixing. Finely divided powders of metals) or metal oxide(s), or powders of metals) or metal oxides) supported on any inert materials, are mixed thoroughly with finely divided powder of the ex situ selectivated silicate-based materials, unselectivated aluminophosphate-based materials, or optionally ex situ selectivated aluminophosphate-based materials in a blending machine or a grinding mortar. The mixture is optionally pelletized before use.
If the catalytic reaction system is mixed with a binder, such as silica gel or sol or the like, an extrudable paste may be formed. The resulting paste can be molded, e.g. extruded, and cut into small strands which can then be dried and calcined.
The catalytic reaction system can also be prepared by mixing physically the particles of silicate-based material or aluminophosphate-based materials components and the particles of the metal and/or metal oxide second components, if present. The same metals and/or metal oxides can also be used alone or together to selectivate catalytic reaction systems and thus simultaneously catalyze syngas and/or other reactions.
The catalytic reaction system can also be formed by packing the first and the second components, if present, in a stacked-bed manner with some of the first component in front of the physical or chemical mixture of the first and second components.
Prior to exposing the catalysts to the feed components of toluene and/or benzene, H2, CO, and/or C02 and/or methanol, the catalyst reaction systems can optionally be activated under a reducing environment (e.g. 1-80% H2 in N2) at 150-500°C, and 1-200 atm (1.01 x 105 - 2.03 x 10' Pa) for 2-48 hours.
The average crystal size of the crystals in the silicate-based material or aluminophosphate-based materials is preferably from above 0.1 micron to about 100 microns, more preferably from about 1 micron to about 100 microns.
Procedures to determine crystal size are known to persons skilled in the art. For instance, crystal size may be determined directly by taking a suitable scanning electron microscope (SEM) picture of a representative sample of the crystals.
The catalysts of this invention may be used in a methylation process which can be carried out as a batch type, semi-continuous or continuous operation utilizing a fixed or moving bed catalyst system.
Multiple injection of the methylating agent may be employed. The methylating agent includes CO, C02 and H2 and/or CH30H and derivatives thereof. The methylating agent reacts with benzene to form toluene. Toluene reacts with the methylating agent to form a xylene, preferably PX in this invention.
Toluene and/or benzene and the methylating agents) are usually premixed and fed together into the reaction vessel to maintain the desired ratio between them with no local concentration of either reactant to disrupt reaction kinetics. Individual feeds can be employed, however, if care is taken to insure good mixing of the reactant vapors in the reaction vessel.
Optionally, instantaneous concentration of methylating agent can be kept low by staged additions thereof. By staged additions, the ratios of toluene and/or benzene to methylating agent concentrations can be maintained at optimum levels to give good toluene conversions. Hydrogen gas can also serve as an anticoking agent and diluent.
The method of this invention, particularly when using para-substituent selectivated catalytic reaction systems, stabilizes catalytic reaction system performance and increases catalytic reaction system life.
That is, catalytic reaction system deactivation is slowed and even prevented. With properly para- substituent selectivated catalytic reaction systems, it is expected that the catalytic reaction system may not have to be regenerated at all. This is in part due to the silicate-based materials 5 and aluminophosphate-based materials being para- substituent selectivated. With production selective to PX, in one non-limiting instance, less by-products, such as heavy aromatics, are formed which would deactivate the catalytic reaction systems. This characteristic is not shown or taught by the prior art.
10 Further, in one non-limiting embodiment of the invention, there is a belief that the catalytic reaction systems of this invention have the capability of preventing or reducing the side reactions of the methylating agents with themselves, and in particular that the para- substituent selectivated catalytic reaction systems function to catalyze more than one 15 reaction, that is, that a syngas reaction is catalyzed to form methylating agents which react with benzene and/or toluene to produce PX, e.g.
However, because the methylating agent is produced on a local, molecular scale, its concentrations are very low (as contrasted with feeding a methylating agent as a co-reactant). It has been demonstrated that feeding a blend of methylating agent and toluene to make PX
increases coke build-up and hence catalytic reaction system deactivation.
In one non-limiting embodiment of the invention, the catalyst activity decrease is less than 0.5% toluene and/or benzene conversion per day, preferably less than 0.1 %, In carrying out the PX synthesis process, the feed mixtures can be co-fed into a reactor containing one of the above mentioned catalytic reaction systems. The catalytic reaction system and reactants can be heated to reaction temperatures separately or together. Reaction can be carried out at a temperature from about 100-700°C, preferably from about 200-600°C; at a pressure from about 1-300 atm (1.01 x 105-3.04 x 10' Pa), preferably from about 1-200 atm (1.01 x 105-2.03 x 10' Pa); and at a flow rate from about 0.01-100 h-' LHSV, preferably from about 1-50 h-' LHSV on a liquid feed basis. The composition of the feed, i.e. the mole ratio of H2/CO(and/or C02)/aromatic can be from of about 0.01-10/0.01-10/0.01-10, preferably from about 0.1-10/0.1-10/0.1-10.
As noted, typical methylating agents include or are formed from, but are not necessarily limited to hydrogen together with carbon monoxide and/or carbon monoxide, and/or methanol, but also dimethylether, methylchloride, methylbromide, and dimethylsulfide.
It is conceivable that in the scenarios described above, the toluene can be pure, or in a mixture with benzene. The benzene may alkylate to toluene, and/or ultimately to PX, with or without recycle. The presence of benzene may also enhance heat and/or selectivity control.
The PX method is expected to tolerate many different kinds of feed.
Unextracted toluene, which is a mixture of toluene and similar boiling range olefins and paraffins, is preferred in one embodiment. For example, premium extracted toluene, essentially pure toluene, and extracted aromatics, essentially a relatively pure mixture of toluene and benzene, may also be used. Unextracted toluene and benzene which contains toluene, benzene, and olefins and paraffins that boil in a similar range to that of toluene or benzene, may also be employed. When unextracted feedstocks are used, it is important to crack the paraffins and olefins into lighter products that can be easily distilled. For example, the feed may contain one or more paraffins and/or olefins having at least 4 carbon atoms; the catalytic reaction systems have the dual function to crack the paraffins and/or olefins and methylate benzene or toluene to selectively produce PX.
Indeed, some of the catalytic reaction systems of this invention may be multifunctional in some embodiments, catalyzing a reaction or reactions of CO, H2, and/or C02 and/or methanol to produce a methylating agent, catalyzing the selective methylation of toluene and/or benzene to produce PX, and catalyzing the cracking of paraffins and olefins into relatively lighter products.
The PX method is capable of producing mixtures of xylenes where PX comprises at least 30 wt.% of the mixture, preferably at least 36 wt.%, and most preferably at least 48 wt.%. The method of this invention is also capable of converting at least 5 wt.% of the aromatic compound to a mixture of xylenes, preferably greater than 15 wt.%.
The following examples will serve to illustrate processes and some merits of the present invention. It is to be understood that these examples are merely illustrative in nature and that the present process is not necessarily limited thereto.
COMPARATIVE EXAMPLE I
This example illustrates the lack of para-selectivity from an untreated ZSM-5 for toluene methylation with methanol. The ZSM-5 zeolite had a Si02/AI203 ratio of 38. It was tested at the conditions of 450°C, 1 atmospheric pressure (1.01 x 105 Pa), 7 WHSV (weight hourly space velocity), and a toluene to methanol molar ratio of 1. Test results indicated that one hour after cutting in the toluene/methanol feed, toluene conversion was at 46% and the PX concentration in the xylene-fraction product was at the equilibrium value of 24%, indicating the lack of selectivity toward PX.
COMPARATIVE EXAMPLE II
This example illustrates the loss of zeolite activity or conversion from conventional selectivation techniques that use compounds which are small enough to enter the zeolite channels. An aqueous solution of magnesium nitrate was prepared by mixing magnesium nitrate hexahydrate and water on the basis of 0.71 gram per gram of water. The solution was used to impregnate a ZSM-5 (Si02/A1203 = 38) zeolite powder at a ratio of 1.35 cc solution to 1.50 g of zeolite. The mixture was heated at 75°C to evaporate the water. It was then dried at 120°C for 6 hours, at 250°C for 1/2 hour, and at 300°C for 1/2 hour, and then calcined at 500°C for 3 hours. Analysis of the zeolite sample indicated that 0.06 gram of magnesium oxide per gram of zeolite was deposited on the zeolite.
A portion of the treated zeolite was tested for toluene methylation with methanol. The test was carried out at the same conditions as in Example I. Test results indicated that one hour after cutting in the feed, toluene conversion was 29% and PX concentration in the xylene-fraction product was 58%.
The selectivation treatment was repeated on the remaining of the treated zeolite. This second treatment raised the Mg0 on zeolite from 0.06 g/g to 0.12 g/g. Toluene methylation results on this double-treated zeolite showed a toluene conversion of 18% and a PX concentration in the xylene-fraction product of 90%. Comparing Example II to Example I, it is apparent that an increase of PX selectivity from 24% to 90% lowered the conversion from 46% to 18%.
INVENTIVE EXAMPLE III
This example illustrates the use of bulky organometallic salts for zeolite selectivation. An aqueous solution of lanthanum nitrate was prepared by dissolving 18.0 gram of La(N03)3~6H20 in 80.0 cc of water. 60 cc of 25% ammonia solution was added to the lanthanum solution with stirring. The addition was completed in a period of 10 minutes. The precipitate of La(OH)3 was filtered and suspended into 300 cc of water.
13.7 gram of ethylenediaminetetraacetic acid (EDTA) was added to the suspension with stirring to obtain a solution, which was boiled and concentrated to obtain a La-EDTA solution with a concentration of 0.02 gram La per cc of solution.
11.4 cc of the La solution was used to impregnate 2.0 gram of ZSM-5 zeolite (Si02/AI203 = 38). The mixture was heated at 75°C to evaporate the water. It was then dried at 120°C overnight, and calcined at 500°C for 6 hours. Analysis of the zeolite sample indicated that 0.14 gram of La203 per gram of zeolite was deposited on the zeolite.
The La-treated zeolite was tested for toluene methylation with methanol at the same conditions as that in Examples I and II. Test results indicated a toluene conversion of 38% and a PX selectivity of 81 %.
Apparently, selectivation using a bulky organometallic salt such as La-EDTA was able to increase para-selectivity significantly with only small loss in zeolite activity.
INVENTIVE EXAMPLE IV
This example illustrates the use of another bulky organometallic salt for zeolite selectivation. An aqueous solution of Mg(N03)2 was prepared by mixing 128.35 g of Mg(N03)2~6H20 in 300 cc water. 60 cc of 25%
ammonia solution was added to the Mg(N03)2 solution with stirring in a 10 minutes period. The Mg(OH)2 precipitate was filtered and suspended in 500 cc water. 66.36 g phthalic acid was deeded to the suspension with stirring and heating to obtain a clear solution, which was boiled and concentrated to 300 cc. It was cooled to room temperature and filtered to obtain a Mg-phthalate filtrate having a concentration of 0.017g Mg per cc of filtrate.
2.05 cc of the Mg-phthalate solution was used to impregnate 2.01 g ZSM-5 zeolite (Si02/AI203 = 38). The mixture was heated at 75°C to evaporate the water. It was then dried at 120°C for 6 hours and calcined at 500°C for 8 hours. This procedure was repeated twice to obtain a 3-time selectivated zeolite sample containing 0.075 g Mg0 per gram of zeolite.
Results of toluene methylation test showed a toluene conversion of 39%
and a PX selectivity of 84%, indicating again the effectiveness of bulky organometallic salts for zeolite selectivation.
COMPARATIVE EXAMPLE V
This example illustrates one of the methods in preparing a catalyst.
The catalyst comprises (1 ) Cr and Zn mixed metal oxides; and (2) H-ZSM-5 5 zeolite with a Si02/AI203 molar ratio of 30 (obtained from PQ
Corporation, Valley Forge, PA). The Cr and Zn mixed metal oxides were prepared by co-precipitation of Cr(N03)3 and Zn(N03)2 with NH40H. 7.22 grams of Cr(N03)3 and 13.41 grams of Zn(N03)2 were dissolved in 100 ml distilled water separately. The two solutions were then mixed together.
10 NH40H was slowly added into the mixed solution with stirring until the pH
value of the solution reached about 8. The precipitate was filtered and recovered. This precipitate was dried at a temperature of 120°C for 12 hours, and then calcined in air at 500°C for 6 hours. These Cr/Zn mixed metal oxides were ground into powders.
15 The catalytic reaction system was prepared by physically mixing powders of a composition of 50% (w/w) Cr/Zn mixed metal oxides and 50% (w/w) H-ZSM-5 zeolite. Powders of 2.0 grams of Cr/Zn mixed metal oxides and 2.0 grams of H-ZSM-5 zeolite were mixed thoroughly in a grinding mortar. The mixed catalytic reaction system powders were 20 pelletized and screened to 8-12 mesh (0.89-0.73 cm) particles.
COMPARATIVE EXAMPLE VI
This example shows that the synthesis of xylenes with syngas alkylation of toluene can be achieved in a catalytic process as disclosed in a prior process. However, this example indicates that this process cannot achieve high para-xylene selectivity when the aluminosilicate component in the catalytic reaction system is not modified for shape selectivity. The catalytic reaction system was prepared as in Example V. The catalyst was reduced at 350°C under 5% H2 (balanced with 95% N2) for 16 hours at 1 atm prior to reaction.
The following examples will serve to illustrate processes and some merits of the present invention. It is to be understood that these examples are merely illustrative in nature and that the present process is not necessarily limited thereto.
COMPARATIVE EXAMPLE I
This example illustrates the lack of para-selectivity from an untreated ZSM-5 for toluene methylation with methanol. The ZSM-5 zeolite had a Si02/AI203 ratio of 38. It was tested at the conditions of 450°C, 1 atmospheric pressure (1.01 x 105 Pa), 7 WHSV (weight hourly space velocity), and a toluene to methanol molar ratio of 1. Test results indicated that one hour after cutting in the toluene/methanol feed, toluene conversion was at 46% and the PX concentration in the xylene-fraction product was at the equilibrium value of 24%, indicating the lack of selectivity toward PX.
COMPARATIVE EXAMPLE II
This example illustrates the loss of zeolite activity or conversion from conventional selectivation techniques that use compounds which are small enough to enter the zeolite channels. An aqueous solution of magnesium nitrate was prepared by mixing magnesium nitrate hexahydrate and water on the basis of 0.71 gram per gram of water. The solution was used to impregnate a ZSM-5 (Si02/A1203 = 38) zeolite powder at a ratio of 1.35 cc solution to 1.50 g of zeolite. The mixture was heated at 75°C to evaporate the water. It was then dried at 120°C for 6 hours, at 250°C for 1/2 hour, and at 300°C for 1/2 hour, and then calcined at 500°C for 3 hours. Analysis of the zeolite sample indicated that 0.06 gram of magnesium oxide per gram of zeolite was deposited on the zeolite.
A portion of the treated zeolite was tested for toluene methylation with methanol. The test was carried out at the same conditions as in Example I. Test results indicated that one hour after cutting in the feed, toluene conversion was 29% and PX concentration in the xylene-fraction product was 58%.
The selectivation treatment was repeated on the remaining of the treated zeolite. This second treatment raised the Mg0 on zeolite from 0.06 g/g to 0.12 g/g. Toluene methylation results on this double-treated zeolite showed a toluene conversion of 18% and a PX concentration in the xylene-fraction product of 90%. Comparing Example II to Example I, it is apparent that an increase of PX selectivity from 24% to 90% lowered the conversion from 46% to 18%.
INVENTIVE EXAMPLE III
This example illustrates the use of bulky organometallic salts for zeolite selectivation. An aqueous solution of lanthanum nitrate was prepared by dissolving 18.0 gram of La(N03)3~6H20 in 80.0 cc of water. 60 cc of 25% ammonia solution was added to the lanthanum solution with stirring. The addition was completed in a period of 10 minutes. The precipitate of La(OH)3 was filtered and suspended into 300 cc of water.
13.7 gram of ethylenediaminetetraacetic acid (EDTA) was added to the suspension with stirring to obtain a solution, which was boiled and concentrated to obtain a La-EDTA solution with a concentration of 0.02 gram La per cc of solution.
11.4 cc of the La solution was used to impregnate 2.0 gram of ZSM-5 zeolite (Si02/AI203 = 38). The mixture was heated at 75°C to evaporate the water. It was then dried at 120°C overnight, and calcined at 500°C for 6 hours. Analysis of the zeolite sample indicated that 0.14 gram of La203 per gram of zeolite was deposited on the zeolite.
The La-treated zeolite was tested for toluene methylation with methanol at the same conditions as that in Examples I and II. Test results indicated a toluene conversion of 38% and a PX selectivity of 81 %.
Apparently, selectivation using a bulky organometallic salt such as La-EDTA was able to increase para-selectivity significantly with only small loss in zeolite activity.
INVENTIVE EXAMPLE IV
This example illustrates the use of another bulky organometallic salt for zeolite selectivation. An aqueous solution of Mg(N03)2 was prepared by mixing 128.35 g of Mg(N03)2~6H20 in 300 cc water. 60 cc of 25%
ammonia solution was added to the Mg(N03)2 solution with stirring in a 10 minutes period. The Mg(OH)2 precipitate was filtered and suspended in 500 cc water. 66.36 g phthalic acid was deeded to the suspension with stirring and heating to obtain a clear solution, which was boiled and concentrated to 300 cc. It was cooled to room temperature and filtered to obtain a Mg-phthalate filtrate having a concentration of 0.017g Mg per cc of filtrate.
2.05 cc of the Mg-phthalate solution was used to impregnate 2.01 g ZSM-5 zeolite (Si02/AI203 = 38). The mixture was heated at 75°C to evaporate the water. It was then dried at 120°C for 6 hours and calcined at 500°C for 8 hours. This procedure was repeated twice to obtain a 3-time selectivated zeolite sample containing 0.075 g Mg0 per gram of zeolite.
Results of toluene methylation test showed a toluene conversion of 39%
and a PX selectivity of 84%, indicating again the effectiveness of bulky organometallic salts for zeolite selectivation.
COMPARATIVE EXAMPLE V
This example illustrates one of the methods in preparing a catalyst.
The catalyst comprises (1 ) Cr and Zn mixed metal oxides; and (2) H-ZSM-5 5 zeolite with a Si02/AI203 molar ratio of 30 (obtained from PQ
Corporation, Valley Forge, PA). The Cr and Zn mixed metal oxides were prepared by co-precipitation of Cr(N03)3 and Zn(N03)2 with NH40H. 7.22 grams of Cr(N03)3 and 13.41 grams of Zn(N03)2 were dissolved in 100 ml distilled water separately. The two solutions were then mixed together.
10 NH40H was slowly added into the mixed solution with stirring until the pH
value of the solution reached about 8. The precipitate was filtered and recovered. This precipitate was dried at a temperature of 120°C for 12 hours, and then calcined in air at 500°C for 6 hours. These Cr/Zn mixed metal oxides were ground into powders.
15 The catalytic reaction system was prepared by physically mixing powders of a composition of 50% (w/w) Cr/Zn mixed metal oxides and 50% (w/w) H-ZSM-5 zeolite. Powders of 2.0 grams of Cr/Zn mixed metal oxides and 2.0 grams of H-ZSM-5 zeolite were mixed thoroughly in a grinding mortar. The mixed catalytic reaction system powders were 20 pelletized and screened to 8-12 mesh (0.89-0.73 cm) particles.
COMPARATIVE EXAMPLE VI
This example shows that the synthesis of xylenes with syngas alkylation of toluene can be achieved in a catalytic process as disclosed in a prior process. However, this example indicates that this process cannot achieve high para-xylene selectivity when the aluminosilicate component in the catalytic reaction system is not modified for shape selectivity. The catalytic reaction system was prepared as in Example V. The catalyst was reduced at 350°C under 5% H2 (balanced with 95% N2) for 16 hours at 1 atm prior to reaction.
The catalytic reaction system was evaluated with co-feed of syngas (CO and H2) and toluene with a composition of H2/CO/toluene of 2/1/0.5 (molar ratio), a temperature of about 450°C, and a pressure of about 18 atm (i.e., 250 psig, 2.53 x 10' Pa). The WHSV (Weight Hourly Space Velocity) was about 3 h~' for toluene with respect to the catalyst. Test results are given in Table 1. Similar to prior art reported, the selectivity of para-xylene in xylenes is about 25%, which is close to equilibrium, with toluene conversion of 28.6% and xylene selectivity of 71.1 %.
Synthesis of PX using Zeolite not Selectivated CO conv. % H2 conv. % Toluene conv. % Xylene select. PX select.
31.7 17.1 28.6 71.1 25.0 INVENTIVE EXAMPLE VII
This example illustrates the preparation of para-alkyl selectivated ZSM-5 zeolite with magnesium oxide as the selectivating agent. 11.68 grams of magnesium hydroxide was mixed with distilled water. To the solution was added 20.44 grams of ammonium nitrate and 33.54 grams of phthalic acid in sequence. The mixture was heated to obtain a clear solution, which was cooled to room temperature before use. 14.80 grams of the solution was mixed with 7.77 grams of a ZSM-5 zeolite (Si02/A102 of 50). The mixture was heated to evaporate the water solvent. The remaining solid was dried at 120°C for 12 hours and calcined at 500°C for 8 hours with air purge. The para-alkyl selectivated ZSM-5 zeolite contained approximately 9 wt.% of magnesium oxide.
Synthesis of PX using Zeolite not Selectivated CO conv. % H2 conv. % Toluene conv. % Xylene select. PX select.
31.7 17.1 28.6 71.1 25.0 INVENTIVE EXAMPLE VII
This example illustrates the preparation of para-alkyl selectivated ZSM-5 zeolite with magnesium oxide as the selectivating agent. 11.68 grams of magnesium hydroxide was mixed with distilled water. To the solution was added 20.44 grams of ammonium nitrate and 33.54 grams of phthalic acid in sequence. The mixture was heated to obtain a clear solution, which was cooled to room temperature before use. 14.80 grams of the solution was mixed with 7.77 grams of a ZSM-5 zeolite (Si02/A102 of 50). The mixture was heated to evaporate the water solvent. The remaining solid was dried at 120°C for 12 hours and calcined at 500°C for 8 hours with air purge. The para-alkyl selectivated ZSM-5 zeolite contained approximately 9 wt.% of magnesium oxide.
INVENTIVE EXAMPLE VIII
This example illustrates the preparation of another type of the catalytic reaction system. The catalytic reaction system comprises (1 ) Mn and Zn mixed metal oxides, and (2) Mg0 modified H-ZSM-5 zeolite with a Si02/A102 of 38. The same preparation procedures as that given in Example VII were used. The Mn and Zn mixed metal oxides were prepared by co-precipitation of Mn(N03)2 and Zn(N03)2 with NH40H. 4.14 grams of Mn(N03)2 and 13.44 grams of Zn(N03)2 were dissolved in 100 ml distilled water separately. The two solutions were then mixed together.
NH40H was slowly added into the mixed solution with stirring until the pH
value of the solution reached about 7.5. The precipitate was filtered and recovered. This precipitate was dried at a temperature of 120°C for 12 hours, and then calcined in air at 500°C for 6 hours. These Mn/Zn mixed metal oxides were ground into powders.
The catalytic reaction system was prepared by physically mixing powders of a composition of 50% (w/w) Mn/Zn mixed metal oxides and 50% (w/w) Mg0 modified H-ZSM-5 zeolite. Powders of 2.0 grams of Mn/Zn mixed metal oxides and 2.0 grams of Mg0 modified H-ZSM-5 zeolite were mixed thoroughly in a grinding mortar. The mixed catalytic reaction system powders were pelletized and screened to 8-12 mesh (0.89-0.73 cm) particles.
INVENTIVE EXAMPLE IX
This example illustrates that metal oxides other than Cr/Zn mixed metal oxides are also suitable as one of the components in the catalytic reaction system used in the xylenes synthesis with syngas alkylation of toluene. In addition, this example demonstrates that high para-xylene selectivity can be obtained when the aluminosilicate component in the catalytic reaction system is modified for shape selectivity. The catalytic reaction system was prepared as in Example VIII. The catalytic reaction system was reduced at 350°C under 5% H2 (balanced with 95% N2) for 16 hours at 1 atm prior to reaction.
The reaction was conducted under similar conditions to those in Example VI. Test results are given in Table 2. The para-xylene selectivity in xylenes is about 76.0% with toluene conversion of 10.9% and xylene selectivity of 85.4%. Compared to Example VI, the para-xylene selectivity is significantly enhanced when the aluminosilicate component is modified for shape selectivity.
Synthesis of PX using Zeolite Modified for Shape Selectivity CO cony. % H2 cony. % Toluene cony. % Xylene select. % PX select.
11.7 5.6 10.9 85.4 76.0 INVENTIVE EXAMPLE X
This example illustrates that the toluene conversion can be increased with a similar high para-xylene selectivity when the reaction operation conditions are optimized. The catalytic reaction system used in this example was comprised of a composition of (1 ) 50% (w/w) Cr, Zn, and Mg mixed metal oxides, and (2) 50% (w/w) Mg0 modified H-ZSM-5 zeolite with a Si02/A102 of 38. The Cr, Zn, and Mg mixed metal oxides were prepared in a similar method as described in Example V with co-precipitation of Cr(N03)3, Zn(N03)2, and Mg(N03)2 with NH40H. The magnesium oxide-modified ZSM zeolite was prepared as described in Example VIII. The catalytic reaction system was prepared by physical mixing as described in Example V. The catalytic reaction system was reduced at 350°C under 5% H2 (balanced with 95% N2) for 16 hours at 1 atm (1.01 x 105 Pa) prior to reaction.
The catalytic reaction system was evaluated with co-feed of syngas (CO and H2) and toluene with a varied composition of H2/CO/toluene, a temperature from 450-490°C, and a pressure in the range of 18-28 atm (i.e. 250-390 psig, 2.53 x 10'-3.95 x 10' Pa). The WHSV (Weight Hourly Space Velocity) varied from 1.5-6 h-' for toluene with respect to the catalytic reaction system. Some of the test results are shown in Table 3.
As shown in Table 3, a toluene conversion of 34% was achieved with a similar para-xylene selectivity when the reaction was operated at a temperature of ca. 460°C, a pressure of ca. 28 atm (390 psig.), and a WHSV of ca. 1.5 h-' for toluene with respect to catalytic reaction system.
Synthesis of PX using Zeolite e Selectivity Modified for Shap Reaction Temperature, C 460 460 460 475 Reaction Pressure, psig 250 390 250 250 Reaction Pressure, Pa 2.53 x 10' 3.95 2.53 x 10' 2.53 x 10' x 10' Feed Composition, mole ratio 2/1/0.25 2/1/0.252/1/0.5 2/1/0.5 WHSV, h-' (Tol./Catalyst) 1.5 1.5 3 3 CO cony. % 18.4 29.2 17.4 18.1 H2 cony. % 6.6 9.4 7.4 7.6 Toluene cony. % 26.0 34.7 13.6 15.5 Xylene select. % 84.2 80.1 82.4 86.3 PX select. % 74.5 75.2 88.0 85.1 COMPARATIVE EXAMPLE XI
This example illustrates the problems of low methanol selectivity and fast catalytic reaction system deactivation associated with a low aromatic/methanol ratio and one-time methanol injection. The catalytic reaction system was extrudates of SAPO-11 material obtained from UOP.
The extrudates were ground and screened to 8-12 mesh (0.89-0.73 cm) and calcined at 550°C under air for 16 hours prior to use. The catalytic reaction system was evaluated at 350°C, 25 atm (350 psig, 3.55 x 10' Pa), and 8 h-' WHSV. The feed was a mixture of toluene/methanol with a molar ratio of 3.6. Test results are given in Table 4. It is seen that the methanol selectivity decreased from 70.0% to 55.0 % over a test period of 24 hours. Furthermore, the system was experiencing a severe catalytic reaction system deactivation as indicated by the decreasing toluene 5 conversion from 18.5% to 15.1 %.
Synthesis of PX with Low Methanol Selectivity and Catalyst Deactivation Toluene/Methanol (mole) 3.6 Hours on Stream 2 24 Toluene Total Conversion 18.5 % 15.1 Toluene Conversion due to Disproportionation 0 % 0 Toluene Conversion due to Methylation 18.5 % 15.1 Methanol Total Conversion 100 % 97.0 Methanol consumed by mono- and multiple 70.0 % 55.0 methylation of toluene Methanol consumed by other Reactions 30.0 % 42.0 COMPARATIVE EXAMPLE XII
This example demonstrates the problems of fast catalytic reaction system deactivation for Mg0 para-alkyl selectivated H-ZSM-5 in toluene methylation with low toluene/methanol ratio and one-time methanol injection. The catalytic reaction system was Mg0-para-alkyl selectivated H-ZSM-5 with a Si02/AIOZ ratio of 38. The same preparation procedure as that given in Example VIII was used. The catalytic reaction system was pelletized and screened to 40-60 mesh. The catalytic reaction system was tested at 460°C, 1 atm, and 14 h-' WHSV. The feed was a mixture of toluene/methanol with a molar ratio of 1Ø The results presented in Table 5 indicate that although Mg0 para-alkyl selectivation of H-ZSM-5 improves the para-xylene selectivity, this catalytic reaction system still exhibits serious catalytic reaction system deactivation as indicated by the decreasing toluene conversion from 20.5% to 8.5%.
Synthesis of PX Showinct Catalytic Reaction System Deactivation Toluene/Methanol (molar ratio) 1/1 Hours on Stream 0.5 2 2 2.5 Toluene Conversion, % 19.3 19.8 20.5 8.5 Methanol Conversion, % 100 100 100 99.6 Xylene Selectivity, % 76.7 76.4 84.1 86.1 Para-Xylene Selectivity, % 83.3 83.3 86.5 76.3 EXAMPLE XIII
This example demonstrates that the catalytic reaction system would suffer from deactivation for syngas methylation of toluene if the aluminosilicate component in the catalytic reaction system is not properly para-alkyl selectivated. The test was conducted in the same manner as Example VI. The reaction was monitored as time-on-stream, and the results are shown in Table 6. The catalytic reaction system displays some deactivation over a period of 18 hours as indicated by the decreasing toluene conversion from 35.3% to 28.6%.
08-06-2001 '1 ~'i : '«H uLM-Marian Mossman& sr~ ram 915 392 8805 US 00001300 seen that the catalytic reaction system had a stable activity for toluene conversion with stable PX selectivity.
Hiq,.her Activity Mainten ance for -xvlene sis P~ra Synthe H2ICO/Toluene (molar ratio) 21110.5 Hours on Stream, h 5.5 24 81.5 120 Toluene Conversion, % 17.0 18.0 17.4 17.1 CO Conversion, l0 20.5 20.7 17.9 17.8 H2 Conversion, % 8.5 9.3 9.1 9.1 Xylene Selectivity, % 76.5 80.2 80.6 80.5 Para-Xylene Selectivity, 63.4 67,0 71.4 75.2 %
In the foregoing specification, the invention has been described with reference to speck embodiments thereof, and has been demonstrated as effective in providing methods for modifying catalyst reaction systems, and the catalyst reaction systems per se, which may be used for directly and selectively producing PX from benzene andlor toluene and hydrogen together with CO andlor C02 andlor methanol, and for other reactions.
However, it will be evident that various modifications and changes can be made thereto without departing from the invention as set forth in the appended claims. Accordingly, the specification is to be regarded in an illustrative rather than a restrictive sense. For example, specific combinations of catalyst components, such as organometallic compounds, other than those specifically tried, in other proportions or ratios or mixed in different ways, falling within the claimed parameters, but.not specifically identified or tried in a. particular example, are anticipated to be within the scope of this invention. Further, various combinations of reactants, catalytic reaction systems, and control techniques not explicitly described but nonetheless falling within the appended claims are understood to be included.
':,i3~3~1;'t11~'(.= ;7I~E.::' ::n<:J~.i: ~3~
AMENDED SHEET
Emvfangsteit 8.Juni 15:48 Synthesis of PX Showina Catalytic Reaction System Deactivation CO/Toluene (molar ratio) 2/1/0.5 Hours on Stream 2 9.5 18.2 Toluene Conversion, 35.3 31.1 28.6 %
CO Conversion, % 33.6 31.4 31.7 H2 Conversion, % 17.8 16.4 17.1 Xylene Selectivity, 67.4 69.8 71.1 %
Para-Xylene Selectivity,24.8 24.9 25.0 %
INVENTIVE EXAMPLE XIV
This example illustrates that the process disclosed in this invention has a much higher activity maintenance for PX synthesis than the conventional methanol-toluene methylation process.
The catalytic reaction system used in this example comprised (1 ) Cr and Zn mixed metal oxides, and (2) Mg0 modified H-ZSM-5 zeolite with a Si02/A102 of 38. The Cr and Zn mixed metal oxides were prepared as described in Example I. The magnesium oxide-modified ZSM zeolite was prepared as described in Example V. The Cr/Zn mixed metal oxides were ground into powders. The catalytic reaction system was prepared by physically mixing powders of a composition of (1 ) 34% (w/w) Cr and Zn mixed metal oxides, and (2) 66% Mg0 modified H-ZSM-5 zeolite. The mixed catalytic reaction system powders were pelletized and screened to 8-12 mesh (0.89-0.73 cm) particles. The catalytic reaction system was reduced at 350°C under 5% H2 (balanced with 95% N2) for 16 hours at 1 atm (1.01 x 105 Pa) prior to reaction. The organometallic modifier was magnesium phthalate.
The catalytic reaction system was evaluated with similar operation conditions as those in Example II. Test results are given in Table 7. It is seen that the catalytic reaction system had a stable activity for toluene conversion with stable PX selectivity.
Higher Activity Maintenance for Para-xylene Synthesis H2/CO/Toluene (molar ratio) 2/1/0.5 Hours on Stream, h 5.5 24 91.5 120 Toluene Conversion, % 17.0 18.0 17.4 17.1 CO Conversion, % 20.5 20.7 17.9 17.8 H2 Conversion, % 8.5 9.3 9.1 9.1 Xylene Selectivity, % 76.5 80.2 80.6 80.5 Para-Xylene Selectivity, % 63.4 67.0 71.4 75.2 In the foregoing specification, the invention has been described with reference to specific embodiments thereof, and has been demonstrated as effective in providing methods for modifying catalyst reaction systems, and the catalyst reaction systems per se, which may be used for directly and selectively producing PX from benzene and/or toluene and hydrogen together with CO and/or C02 and/or methanol, and for other reactions. However, it will be evident that various modifications and changes can be made thereto without departing from the broader spirit or scope of the invention as set forth in the appended claims.
Accordingly, the specification is to be regarded in an illustrative rather than a restrictive sense. For example, specific combinations of catalyst components, such as organometallic compounds, other than those specifically tried, in other proportions or ratios or mixed in different ways, falling within the claimed parameters, but not specifically identified or tried in a particular example, are anticipated to be within the scope of this invention. Further, various combinations of reactants, catalytic reaction systems, and control techniques not explicitly described but nonetheless falling within the appended claims are understood to be included.
This example illustrates the preparation of another type of the catalytic reaction system. The catalytic reaction system comprises (1 ) Mn and Zn mixed metal oxides, and (2) Mg0 modified H-ZSM-5 zeolite with a Si02/A102 of 38. The same preparation procedures as that given in Example VII were used. The Mn and Zn mixed metal oxides were prepared by co-precipitation of Mn(N03)2 and Zn(N03)2 with NH40H. 4.14 grams of Mn(N03)2 and 13.44 grams of Zn(N03)2 were dissolved in 100 ml distilled water separately. The two solutions were then mixed together.
NH40H was slowly added into the mixed solution with stirring until the pH
value of the solution reached about 7.5. The precipitate was filtered and recovered. This precipitate was dried at a temperature of 120°C for 12 hours, and then calcined in air at 500°C for 6 hours. These Mn/Zn mixed metal oxides were ground into powders.
The catalytic reaction system was prepared by physically mixing powders of a composition of 50% (w/w) Mn/Zn mixed metal oxides and 50% (w/w) Mg0 modified H-ZSM-5 zeolite. Powders of 2.0 grams of Mn/Zn mixed metal oxides and 2.0 grams of Mg0 modified H-ZSM-5 zeolite were mixed thoroughly in a grinding mortar. The mixed catalytic reaction system powders were pelletized and screened to 8-12 mesh (0.89-0.73 cm) particles.
INVENTIVE EXAMPLE IX
This example illustrates that metal oxides other than Cr/Zn mixed metal oxides are also suitable as one of the components in the catalytic reaction system used in the xylenes synthesis with syngas alkylation of toluene. In addition, this example demonstrates that high para-xylene selectivity can be obtained when the aluminosilicate component in the catalytic reaction system is modified for shape selectivity. The catalytic reaction system was prepared as in Example VIII. The catalytic reaction system was reduced at 350°C under 5% H2 (balanced with 95% N2) for 16 hours at 1 atm prior to reaction.
The reaction was conducted under similar conditions to those in Example VI. Test results are given in Table 2. The para-xylene selectivity in xylenes is about 76.0% with toluene conversion of 10.9% and xylene selectivity of 85.4%. Compared to Example VI, the para-xylene selectivity is significantly enhanced when the aluminosilicate component is modified for shape selectivity.
Synthesis of PX using Zeolite Modified for Shape Selectivity CO cony. % H2 cony. % Toluene cony. % Xylene select. % PX select.
11.7 5.6 10.9 85.4 76.0 INVENTIVE EXAMPLE X
This example illustrates that the toluene conversion can be increased with a similar high para-xylene selectivity when the reaction operation conditions are optimized. The catalytic reaction system used in this example was comprised of a composition of (1 ) 50% (w/w) Cr, Zn, and Mg mixed metal oxides, and (2) 50% (w/w) Mg0 modified H-ZSM-5 zeolite with a Si02/A102 of 38. The Cr, Zn, and Mg mixed metal oxides were prepared in a similar method as described in Example V with co-precipitation of Cr(N03)3, Zn(N03)2, and Mg(N03)2 with NH40H. The magnesium oxide-modified ZSM zeolite was prepared as described in Example VIII. The catalytic reaction system was prepared by physical mixing as described in Example V. The catalytic reaction system was reduced at 350°C under 5% H2 (balanced with 95% N2) for 16 hours at 1 atm (1.01 x 105 Pa) prior to reaction.
The catalytic reaction system was evaluated with co-feed of syngas (CO and H2) and toluene with a varied composition of H2/CO/toluene, a temperature from 450-490°C, and a pressure in the range of 18-28 atm (i.e. 250-390 psig, 2.53 x 10'-3.95 x 10' Pa). The WHSV (Weight Hourly Space Velocity) varied from 1.5-6 h-' for toluene with respect to the catalytic reaction system. Some of the test results are shown in Table 3.
As shown in Table 3, a toluene conversion of 34% was achieved with a similar para-xylene selectivity when the reaction was operated at a temperature of ca. 460°C, a pressure of ca. 28 atm (390 psig.), and a WHSV of ca. 1.5 h-' for toluene with respect to catalytic reaction system.
Synthesis of PX using Zeolite e Selectivity Modified for Shap Reaction Temperature, C 460 460 460 475 Reaction Pressure, psig 250 390 250 250 Reaction Pressure, Pa 2.53 x 10' 3.95 2.53 x 10' 2.53 x 10' x 10' Feed Composition, mole ratio 2/1/0.25 2/1/0.252/1/0.5 2/1/0.5 WHSV, h-' (Tol./Catalyst) 1.5 1.5 3 3 CO cony. % 18.4 29.2 17.4 18.1 H2 cony. % 6.6 9.4 7.4 7.6 Toluene cony. % 26.0 34.7 13.6 15.5 Xylene select. % 84.2 80.1 82.4 86.3 PX select. % 74.5 75.2 88.0 85.1 COMPARATIVE EXAMPLE XI
This example illustrates the problems of low methanol selectivity and fast catalytic reaction system deactivation associated with a low aromatic/methanol ratio and one-time methanol injection. The catalytic reaction system was extrudates of SAPO-11 material obtained from UOP.
The extrudates were ground and screened to 8-12 mesh (0.89-0.73 cm) and calcined at 550°C under air for 16 hours prior to use. The catalytic reaction system was evaluated at 350°C, 25 atm (350 psig, 3.55 x 10' Pa), and 8 h-' WHSV. The feed was a mixture of toluene/methanol with a molar ratio of 3.6. Test results are given in Table 4. It is seen that the methanol selectivity decreased from 70.0% to 55.0 % over a test period of 24 hours. Furthermore, the system was experiencing a severe catalytic reaction system deactivation as indicated by the decreasing toluene 5 conversion from 18.5% to 15.1 %.
Synthesis of PX with Low Methanol Selectivity and Catalyst Deactivation Toluene/Methanol (mole) 3.6 Hours on Stream 2 24 Toluene Total Conversion 18.5 % 15.1 Toluene Conversion due to Disproportionation 0 % 0 Toluene Conversion due to Methylation 18.5 % 15.1 Methanol Total Conversion 100 % 97.0 Methanol consumed by mono- and multiple 70.0 % 55.0 methylation of toluene Methanol consumed by other Reactions 30.0 % 42.0 COMPARATIVE EXAMPLE XII
This example demonstrates the problems of fast catalytic reaction system deactivation for Mg0 para-alkyl selectivated H-ZSM-5 in toluene methylation with low toluene/methanol ratio and one-time methanol injection. The catalytic reaction system was Mg0-para-alkyl selectivated H-ZSM-5 with a Si02/AIOZ ratio of 38. The same preparation procedure as that given in Example VIII was used. The catalytic reaction system was pelletized and screened to 40-60 mesh. The catalytic reaction system was tested at 460°C, 1 atm, and 14 h-' WHSV. The feed was a mixture of toluene/methanol with a molar ratio of 1Ø The results presented in Table 5 indicate that although Mg0 para-alkyl selectivation of H-ZSM-5 improves the para-xylene selectivity, this catalytic reaction system still exhibits serious catalytic reaction system deactivation as indicated by the decreasing toluene conversion from 20.5% to 8.5%.
Synthesis of PX Showinct Catalytic Reaction System Deactivation Toluene/Methanol (molar ratio) 1/1 Hours on Stream 0.5 2 2 2.5 Toluene Conversion, % 19.3 19.8 20.5 8.5 Methanol Conversion, % 100 100 100 99.6 Xylene Selectivity, % 76.7 76.4 84.1 86.1 Para-Xylene Selectivity, % 83.3 83.3 86.5 76.3 EXAMPLE XIII
This example demonstrates that the catalytic reaction system would suffer from deactivation for syngas methylation of toluene if the aluminosilicate component in the catalytic reaction system is not properly para-alkyl selectivated. The test was conducted in the same manner as Example VI. The reaction was monitored as time-on-stream, and the results are shown in Table 6. The catalytic reaction system displays some deactivation over a period of 18 hours as indicated by the decreasing toluene conversion from 35.3% to 28.6%.
08-06-2001 '1 ~'i : '«H uLM-Marian Mossman& sr~ ram 915 392 8805 US 00001300 seen that the catalytic reaction system had a stable activity for toluene conversion with stable PX selectivity.
Hiq,.her Activity Mainten ance for -xvlene sis P~ra Synthe H2ICO/Toluene (molar ratio) 21110.5 Hours on Stream, h 5.5 24 81.5 120 Toluene Conversion, % 17.0 18.0 17.4 17.1 CO Conversion, l0 20.5 20.7 17.9 17.8 H2 Conversion, % 8.5 9.3 9.1 9.1 Xylene Selectivity, % 76.5 80.2 80.6 80.5 Para-Xylene Selectivity, 63.4 67,0 71.4 75.2 %
In the foregoing specification, the invention has been described with reference to speck embodiments thereof, and has been demonstrated as effective in providing methods for modifying catalyst reaction systems, and the catalyst reaction systems per se, which may be used for directly and selectively producing PX from benzene andlor toluene and hydrogen together with CO andlor C02 andlor methanol, and for other reactions.
However, it will be evident that various modifications and changes can be made thereto without departing from the invention as set forth in the appended claims. Accordingly, the specification is to be regarded in an illustrative rather than a restrictive sense. For example, specific combinations of catalyst components, such as organometallic compounds, other than those specifically tried, in other proportions or ratios or mixed in different ways, falling within the claimed parameters, but.not specifically identified or tried in a. particular example, are anticipated to be within the scope of this invention. Further, various combinations of reactants, catalytic reaction systems, and control techniques not explicitly described but nonetheless falling within the appended claims are understood to be included.
':,i3~3~1;'t11~'(.= ;7I~E.::' ::n<:J~.i: ~3~
AMENDED SHEET
Emvfangsteit 8.Juni 15:48 Synthesis of PX Showina Catalytic Reaction System Deactivation CO/Toluene (molar ratio) 2/1/0.5 Hours on Stream 2 9.5 18.2 Toluene Conversion, 35.3 31.1 28.6 %
CO Conversion, % 33.6 31.4 31.7 H2 Conversion, % 17.8 16.4 17.1 Xylene Selectivity, 67.4 69.8 71.1 %
Para-Xylene Selectivity,24.8 24.9 25.0 %
INVENTIVE EXAMPLE XIV
This example illustrates that the process disclosed in this invention has a much higher activity maintenance for PX synthesis than the conventional methanol-toluene methylation process.
The catalytic reaction system used in this example comprised (1 ) Cr and Zn mixed metal oxides, and (2) Mg0 modified H-ZSM-5 zeolite with a Si02/A102 of 38. The Cr and Zn mixed metal oxides were prepared as described in Example I. The magnesium oxide-modified ZSM zeolite was prepared as described in Example V. The Cr/Zn mixed metal oxides were ground into powders. The catalytic reaction system was prepared by physically mixing powders of a composition of (1 ) 34% (w/w) Cr and Zn mixed metal oxides, and (2) 66% Mg0 modified H-ZSM-5 zeolite. The mixed catalytic reaction system powders were pelletized and screened to 8-12 mesh (0.89-0.73 cm) particles. The catalytic reaction system was reduced at 350°C under 5% H2 (balanced with 95% N2) for 16 hours at 1 atm (1.01 x 105 Pa) prior to reaction. The organometallic modifier was magnesium phthalate.
The catalytic reaction system was evaluated with similar operation conditions as those in Example II. Test results are given in Table 7. It is seen that the catalytic reaction system had a stable activity for toluene conversion with stable PX selectivity.
Higher Activity Maintenance for Para-xylene Synthesis H2/CO/Toluene (molar ratio) 2/1/0.5 Hours on Stream, h 5.5 24 91.5 120 Toluene Conversion, % 17.0 18.0 17.4 17.1 CO Conversion, % 20.5 20.7 17.9 17.8 H2 Conversion, % 8.5 9.3 9.1 9.1 Xylene Selectivity, % 76.5 80.2 80.6 80.5 Para-Xylene Selectivity, % 63.4 67.0 71.4 75.2 In the foregoing specification, the invention has been described with reference to specific embodiments thereof, and has been demonstrated as effective in providing methods for modifying catalyst reaction systems, and the catalyst reaction systems per se, which may be used for directly and selectively producing PX from benzene and/or toluene and hydrogen together with CO and/or C02 and/or methanol, and for other reactions. However, it will be evident that various modifications and changes can be made thereto without departing from the broader spirit or scope of the invention as set forth in the appended claims.
Accordingly, the specification is to be regarded in an illustrative rather than a restrictive sense. For example, specific combinations of catalyst components, such as organometallic compounds, other than those specifically tried, in other proportions or ratios or mixed in different ways, falling within the claimed parameters, but not specifically identified or tried in a particular example, are anticipated to be within the scope of this invention. Further, various combinations of reactants, catalytic reaction systems, and control techniques not explicitly described but nonetheless falling within the appended claims are understood to be included.
Claims (9)
1. A method for modifying catalysts comprising contacting a first component selected from the group consisting of crystalline or amorphous aluminosilicates, substituted aluminosilicates, substituted silicates, crystalline or amorphous aluminophosphates, zeolite-bound zeolites, substituted aluminophosphates, and mixtures thereof with an agent that is an organometallic salt too bulky to enter channels in the first component, where the organometallic salt comprises:
an organic anion having functional groups selected from the group consisting of carboxylic groups, phenolic groups and mixtures thereof; and a metal ration selected from the group consisting of the element(s) of Groups 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, and 16 (new IUPAC notation).
an organic anion having functional groups selected from the group consisting of carboxylic groups, phenolic groups and mixtures thereof; and a metal ration selected from the group consisting of the element(s) of Groups 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, and 16 (new IUPAC notation).
2. The method of claim 1 where the contacting further comprises contacting a second component of one or more than one of the metals or oxides of the metals selected from Groups 1, 2, 3, 4, 5. 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, and 16.
3. The method of claim 2 where contacting the first component with the agent occurs prior to contacting the first component with the second component.
4. The method of claim 2 where contacting the first component with the second component occurs prior to contacting the first component with the agent.
5. The method of claim 1 further comprising:
making a solution of the agent with a solvent;
mixing the solution with the first component;
removing the solvent; and converting the agent into elemental forms or oxide forms.
making a solution of the agent with a solvent;
mixing the solution with the first component;
removing the solvent; and converting the agent into elemental forms or oxide forms.
6. The method of claim 1 or 2 further comprising:
mixing the agent with the first component in the absence of a solvent; and converting the agent into elemental forms or oxide forms.
mixing the agent with the first component in the absence of a solvent; and converting the agent into elemental forms or oxide forms.
7. The method of claim 6 where the converting is performed by heating the mixture at a temperature and for a time effective to convert the agent into metallic oxide.
8. The method of claim 1 where ratio of the wt.% of agent elements to wt.% of the first component ranges from 1/99 to 99/1.
9. A catalyst prepared according the method of any preceding claim.
Applications Claiming Priority (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/312,104 | 1999-05-14 | ||
US09/312,104 US6388156B1 (en) | 1999-05-14 | 1999-05-14 | Direct selective synthesis of para-xylene by reacting an aromatic compound with a methylating agent formed from CO, Co2 and H2 |
US09/327,241 US6613708B1 (en) | 1999-06-07 | 1999-06-07 | Catalyst selectivation |
US09/327,241 | 1999-06-07 | ||
PCT/US2000/013003 WO2000074847A1 (en) | 1999-05-14 | 2000-05-11 | Catalyst selectivation |
Publications (1)
Publication Number | Publication Date |
---|---|
CA2371225A1 true CA2371225A1 (en) | 2000-12-14 |
Family
ID=26978229
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CA002371225A Abandoned CA2371225A1 (en) | 1999-05-14 | 2000-05-11 | Catalyst selectivation |
Country Status (5)
Country | Link |
---|---|
EP (1) | EP1189697A1 (en) |
CN (1) | CN1505546A (en) |
CA (1) | CA2371225A1 (en) |
MX (1) | MXPA01012623A (en) |
WO (1) | WO2000074847A1 (en) |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20040097769A1 (en) * | 2002-11-14 | 2004-05-20 | Ou John D. Y. | Para-xylene production process employing in-situ catalyst selectivation |
KR100638444B1 (en) * | 2004-10-18 | 2006-10-24 | 주식회사 엘지화학 | Hydrocarbon Cracking Catalyst using Chemical Liquid Deposition and Method for Preparing the Same |
DE102006003954A1 (en) * | 2006-01-26 | 2007-08-02 | Sick Ag | light Curtain |
CN102464540B (en) * | 2010-11-17 | 2016-07-06 | 中国石油化工股份有限公司 | For the method producing para-alkylated arene |
US10099210B2 (en) | 2013-04-29 | 2018-10-16 | Saudi Basic Industries Corporation | Catalytic methods for converting naphtha into olefins |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4034053A (en) * | 1975-12-08 | 1977-07-05 | Mobil Oil Corporation | Selective production of para-xylene |
SU1301485A1 (en) * | 1985-04-02 | 1987-04-07 | Институт общей и неорганической химии АН БССР | Catalyst for isomerization of xylenes |
FR2643830B1 (en) * | 1989-03-03 | 1991-06-21 | Inst Francais Du Petrole | MORDENITE-BASED CATALYST CONTAINING AT LEAST ONE METAL FROM GROUPS IIA, IVB, IIB OR IVA AND ITS USE IN ISOMERIZATION OF AN AROMATIC C8 CUT |
RU2119470C1 (en) * | 1997-02-27 | 1998-09-27 | Конструкторско-технологический институт каталитических и адсорбционных процессов на цеолитах "Цеосит" СО РАН | Method of synthesis-gas alkylation of aromatic hydrocarbons |
US5990032A (en) * | 1997-09-30 | 1999-11-23 | Phillips Petroleum Company | Hydrocarbon conversion catalyst composition and processes therefor and therewith |
-
2000
- 2000-05-11 EP EP00935926A patent/EP1189697A1/en not_active Withdrawn
- 2000-05-11 CA CA002371225A patent/CA2371225A1/en not_active Abandoned
- 2000-05-11 MX MXPA01012623A patent/MXPA01012623A/en unknown
- 2000-05-11 WO PCT/US2000/013003 patent/WO2000074847A1/en not_active Application Discontinuation
- 2000-05-11 CN CNA008096724A patent/CN1505546A/en active Pending
Also Published As
Publication number | Publication date |
---|---|
WO2000074847A8 (en) | 2001-05-03 |
MXPA01012623A (en) | 2002-06-21 |
CN1505546A (en) | 2004-06-16 |
EP1189697A1 (en) | 2002-03-27 |
WO2000074847A1 (en) | 2000-12-14 |
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