EP2794522A1 - Method for isomerizing an aromatic c8 fraction in the presence of a catalyst containing an euo zeolite and a specific binder - Google Patents
Method for isomerizing an aromatic c8 fraction in the presence of a catalyst containing an euo zeolite and a specific binderInfo
- Publication number
- EP2794522A1 EP2794522A1 EP12813395.6A EP12813395A EP2794522A1 EP 2794522 A1 EP2794522 A1 EP 2794522A1 EP 12813395 A EP12813395 A EP 12813395A EP 2794522 A1 EP2794522 A1 EP 2794522A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- zeolite
- catalyst
- matrix
- metal
- group viii
- 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.)
- Withdrawn
Links
- 239000010457 zeolite Substances 0.000 title claims abstract description 135
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 title claims abstract description 116
- 229910021536 Zeolite Inorganic materials 0.000 title claims abstract description 114
- 239000003054 catalyst Substances 0.000 title claims abstract description 108
- 238000000034 method Methods 0.000 title claims abstract description 55
- 125000003118 aryl group Chemical group 0.000 title claims abstract description 14
- 239000011230 binding agent Substances 0.000 title description 4
- 229910052751 metal Inorganic materials 0.000 claims abstract description 74
- 239000002184 metal Substances 0.000 claims abstract description 74
- 239000011159 matrix material Substances 0.000 claims abstract description 46
- 239000000203 mixture Substances 0.000 claims abstract description 23
- 125000004432 carbon atom Chemical group C* 0.000 claims abstract description 12
- 230000000737 periodic effect Effects 0.000 claims abstract description 10
- 150000001491 aromatic compounds Chemical class 0.000 claims abstract description 9
- 238000007493 shaping process Methods 0.000 claims description 29
- 238000001354 calcination Methods 0.000 claims description 24
- 150000002739 metals Chemical class 0.000 claims description 15
- 238000005342 ion exchange Methods 0.000 claims description 14
- 238000006317 isomerization reaction Methods 0.000 claims description 14
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 13
- 230000015572 biosynthetic process Effects 0.000 claims description 10
- 230000008021 deposition Effects 0.000 claims description 10
- 238000001035 drying Methods 0.000 claims description 10
- 229910052739 hydrogen Inorganic materials 0.000 claims description 10
- 239000001257 hydrogen Substances 0.000 claims description 10
- 229910052680 mordenite Inorganic materials 0.000 claims description 10
- 238000003786 synthesis reaction Methods 0.000 claims description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 8
- 238000002360 preparation method Methods 0.000 claims description 8
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 4
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 claims description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 2
- ILRRQNADMUWWFW-UHFFFAOYSA-K aluminium phosphate Chemical class O1[Al]2OP1(=O)O2 ILRRQNADMUWWFW-UHFFFAOYSA-K 0.000 claims description 2
- 229910052810 boron oxide Inorganic materials 0.000 claims description 2
- JKWMSGQKBLHBQQ-UHFFFAOYSA-N diboron trioxide Chemical compound O=BOB=O JKWMSGQKBLHBQQ-UHFFFAOYSA-N 0.000 claims description 2
- 239000000395 magnesium oxide Substances 0.000 claims description 2
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 claims description 2
- JUWGUJSXVOBPHP-UHFFFAOYSA-B titanium(4+);tetraphosphate Chemical class [Ti+4].[Ti+4].[Ti+4].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O JUWGUJSXVOBPHP-UHFFFAOYSA-B 0.000 claims description 2
- LEHFSLREWWMLPU-UHFFFAOYSA-B zirconium(4+);tetraphosphate Chemical class [Zr+4].[Zr+4].[Zr+4].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O LEHFSLREWWMLPU-UHFFFAOYSA-B 0.000 claims description 2
- 239000003610 charcoal Substances 0.000 claims 1
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 31
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 26
- 239000008096 xylene Substances 0.000 description 17
- 150000003738 xylenes Chemical class 0.000 description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- 229910052697 platinum Inorganic materials 0.000 description 14
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 12
- 239000011148 porous material Substances 0.000 description 12
- 239000002253 acid Substances 0.000 description 11
- 238000000151 deposition Methods 0.000 description 11
- 238000001125 extrusion Methods 0.000 description 9
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 8
- 239000011734 sodium Substances 0.000 description 8
- 229910052717 sulfur Inorganic materials 0.000 description 8
- 239000011593 sulfur Substances 0.000 description 8
- 239000003795 chemical substances by application Substances 0.000 description 7
- 238000002156 mixing Methods 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 239000002243 precursor Substances 0.000 description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 6
- 229910052782 aluminium Inorganic materials 0.000 description 6
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 6
- 230000003197 catalytic effect Effects 0.000 description 6
- 229910052763 palladium Inorganic materials 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- -1 compound aromatic compound Chemical class 0.000 description 5
- 150000001875 compounds Chemical class 0.000 description 5
- 238000009826 distribution Methods 0.000 description 5
- 238000005470 impregnation Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 229910052718 tin Inorganic materials 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 229910052738 indium Inorganic materials 0.000 description 4
- APFVFJFRJDLVQX-UHFFFAOYSA-N indium atom Chemical compound [In] APFVFJFRJDLVQX-UHFFFAOYSA-N 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- ZZBAGJPKGRJIJH-UHFFFAOYSA-N 7h-purine-2-carbaldehyde Chemical compound O=CC1=NC=C2NC=NC2=N1 ZZBAGJPKGRJIJH-UHFFFAOYSA-N 0.000 description 3
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000006185 dispersion Substances 0.000 description 3
- 238000011066 ex-situ storage Methods 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
- 229910052742 iron Inorganic materials 0.000 description 3
- 238000004898 kneading Methods 0.000 description 3
- 229910000510 noble metal Inorganic materials 0.000 description 3
- 229910052702 rhenium Inorganic materials 0.000 description 3
- WUAPFZMCVAUBPE-UHFFFAOYSA-N rhenium atom Chemical compound [Re] WUAPFZMCVAUBPE-UHFFFAOYSA-N 0.000 description 3
- 229910052710 silicon Inorganic materials 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- 238000005987 sulfurization reaction Methods 0.000 description 3
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 2
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 2
- GYHNNYVSQQEPJS-UHFFFAOYSA-N Gallium Chemical compound [Ga] GYHNNYVSQQEPJS-UHFFFAOYSA-N 0.000 description 2
- 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 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 2
- CUJRVFIICFDLGR-UHFFFAOYSA-N acetylacetonate Chemical compound CC(=O)[CH-]C(C)=O CUJRVFIICFDLGR-UHFFFAOYSA-N 0.000 description 2
- YRKCREAYFQTBPV-UHFFFAOYSA-N acetylacetone Chemical compound CC(=O)CC(C)=O YRKCREAYFQTBPV-UHFFFAOYSA-N 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 238000005349 anion exchange Methods 0.000 description 2
- 239000011324 bead Substances 0.000 description 2
- 229910052796 boron Inorganic materials 0.000 description 2
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 2
- 229910052794 bromium Inorganic materials 0.000 description 2
- 150000001768 cations Chemical class 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 229910052733 gallium Inorganic materials 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 229910052741 iridium Inorganic materials 0.000 description 2
- GKOZUEZYRPOHIO-UHFFFAOYSA-N iridium atom Chemical compound [Ir] GKOZUEZYRPOHIO-UHFFFAOYSA-N 0.000 description 2
- UAEPNZWRGJTJPN-UHFFFAOYSA-N methylcyclohexane Chemical compound CC1CCCCC1 UAEPNZWRGJTJPN-UHFFFAOYSA-N 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 150000002894 organic compounds Chemical class 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- 238000005453 pelletization Methods 0.000 description 2
- NDBYXKQCPYUOMI-UHFFFAOYSA-N platinum(4+) Chemical class [Pt+4] NDBYXKQCPYUOMI-UHFFFAOYSA-N 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000011541 reaction mixture Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- JHJLBTNAGRQEKS-UHFFFAOYSA-M sodium bromide Chemical compound [Na+].[Br-] JHJLBTNAGRQEKS-UHFFFAOYSA-M 0.000 description 2
- QSHYGLAZPRJAEZ-UHFFFAOYSA-N 4-(chloromethyl)-2-(2-methylphenyl)-1,3-thiazole Chemical compound CC1=CC=CC=C1C1=NC(CCl)=CS1 QSHYGLAZPRJAEZ-UHFFFAOYSA-N 0.000 description 1
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- USFZMSVCRYTOJT-UHFFFAOYSA-N Ammonium acetate Chemical compound N.CC(O)=O USFZMSVCRYTOJT-UHFFFAOYSA-N 0.000 description 1
- 239000005695 Ammonium acetate Substances 0.000 description 1
- 229920002134 Carboxymethyl cellulose Polymers 0.000 description 1
- 229910052684 Cerium Inorganic materials 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 1
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 239000004372 Polyvinyl alcohol Substances 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 235000021355 Stearic acid Nutrition 0.000 description 1
- 125000005595 acetylacetonate group Chemical group 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 125000002877 alkyl aryl group Chemical group 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 229940043376 ammonium acetate Drugs 0.000 description 1
- 235000019257 ammonium acetate Nutrition 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 125000000129 anionic group Chemical group 0.000 description 1
- 239000012736 aqueous medium Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 125000003710 aryl alkyl group Chemical group 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 229920001222 biopolymer Polymers 0.000 description 1
- 150000001649 bromium compounds Chemical class 0.000 description 1
- 239000006229 carbon black Substances 0.000 description 1
- 235000019241 carbon black Nutrition 0.000 description 1
- 239000001768 carboxy methyl cellulose Substances 0.000 description 1
- 235000010948 carboxy methyl cellulose Nutrition 0.000 description 1
- 229920003064 carboxyethyl cellulose Polymers 0.000 description 1
- 239000008112 carboxymethyl-cellulose Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000005341 cation exchange Methods 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- ZMIGMASIKSOYAM-UHFFFAOYSA-N cerium Chemical compound [Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce] ZMIGMASIKSOYAM-UHFFFAOYSA-N 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 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 compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 229940125904 compound 1 Drugs 0.000 description 1
- 125000000753 cycloalkyl group Chemical group 0.000 description 1
- 239000007857 degradation product Substances 0.000 description 1
- LNIYNESXCOYFPW-UHFFFAOYSA-N dibenzyl(dimethyl)azanium Chemical class C=1C=CC=CC=1C[N+](C)(C)CC1=CC=CC=C1 LNIYNESXCOYFPW-UHFFFAOYSA-N 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- FAHBNUUHRFUEAI-UHFFFAOYSA-M hydroxidooxidoaluminium Chemical compound O[Al]=O FAHBNUUHRFUEAI-UHFFFAOYSA-M 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- PNDPGZBMCMUPRI-UHFFFAOYSA-N iodine Chemical compound II PNDPGZBMCMUPRI-UHFFFAOYSA-N 0.000 description 1
- 150000002736 metal compounds Chemical class 0.000 description 1
- GYNNXHKOJHMOHS-UHFFFAOYSA-N methyl-cycloheptane Natural products CC1CCCCCC1 GYNNXHKOJHMOHS-UHFFFAOYSA-N 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 150000002823 nitrates Chemical class 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 238000000696 nitrogen adsorption--desorption isotherm Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- QIQXTHQIDYTFRH-UHFFFAOYSA-N octadecanoic acid Chemical compound CCCCCCCCCCCCCCCCCC(O)=O QIQXTHQIDYTFRH-UHFFFAOYSA-N 0.000 description 1
- OQCDKBAXFALNLD-UHFFFAOYSA-N octadecanoic acid Natural products CCCCCCCC(C)CCCCCCCCC(O)=O OQCDKBAXFALNLD-UHFFFAOYSA-N 0.000 description 1
- 150000002896 organic halogen compounds Chemical class 0.000 description 1
- 150000002902 organometallic compounds Chemical class 0.000 description 1
- 229910052762 osmium Inorganic materials 0.000 description 1
- SYQBFIAQOQZEGI-UHFFFAOYSA-N osmium atom Chemical compound [Os] SYQBFIAQOQZEGI-UHFFFAOYSA-N 0.000 description 1
- GPNDARIEYHPYAY-UHFFFAOYSA-N palladium(ii) nitrate Chemical compound [Pd+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O GPNDARIEYHPYAY-UHFFFAOYSA-N 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- HRGDZIGMBDGFTC-UHFFFAOYSA-N platinum(2+) Chemical class [Pt+2] HRGDZIGMBDGFTC-UHFFFAOYSA-N 0.000 description 1
- BYFKUSIUMUEWCM-UHFFFAOYSA-N platinum;hexahydrate Chemical compound O.O.O.O.O.O.[Pt] BYFKUSIUMUEWCM-UHFFFAOYSA-N 0.000 description 1
- 229920002401 polyacrylamide Polymers 0.000 description 1
- 229920001223 polyethylene glycol Polymers 0.000 description 1
- 229920001470 polyketone Polymers 0.000 description 1
- 229920002451 polyvinyl alcohol Polymers 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 239000010948 rhodium Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229910001388 sodium aluminate Inorganic materials 0.000 description 1
- 239000011877 solvent mixture Substances 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008117 stearic acid Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 125000004434 sulfur atom Chemical group 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 239000003784 tall oil Substances 0.000 description 1
- AFCAKJKUYFLYFK-UHFFFAOYSA-N tetrabutyltin Chemical compound CCCC[Sn](CCCC)(CCCC)CCCC AFCAKJKUYFLYFK-UHFFFAOYSA-N 0.000 description 1
- HPGGPRDJHPYFRM-UHFFFAOYSA-J tin(iv) chloride Chemical class Cl[Sn](Cl)(Cl)Cl HPGGPRDJHPYFRM-UHFFFAOYSA-J 0.000 description 1
- 238000012876 topography Methods 0.000 description 1
- 238000011282 treatment Methods 0.000 description 1
- GSYXIGDIZRBXJH-UHFFFAOYSA-N triphenylindigane Chemical compound C1=CC=CC=C1[In](C=1C=CC=CC=1)C1=CC=CC=C1 GSYXIGDIZRBXJH-UHFFFAOYSA-N 0.000 description 1
- 229920001285 xanthan gum Polymers 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
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
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Definitions
- the present invention relates to the isomerization of an aromatic cut containing at least one aromatic compound with eight carbon atoms per molecule for the production of xylenes and in particular para-xylene.
- the present invention relates more particularly to a method of isomerization of an aromatic filler comprising at least one aromatic compound with eight carbon atoms per molecule to maximize the production of para-xylene, said isomerization process using a catalyst comprising at least one Group VIII metal supported on a particular zeolite support.
- the present invention also relates to the process for preparing said catalyst.
- the catalytic isomerization formulations of xylenes known to those skilled in the art are generally based on a zeolite and a Group VIII metal shaped with a binder, often aluminum.
- zeolites used in isomerization of aromatic C8 cuts, there is ZSM-5, used alone or mixed with other zeolites, such as mordenite.
- ZSM-5 used alone or mixed with other zeolites, such as mordenite.
- Other catalysts mainly based on mordenite have been described, for example, in US Pat. A-4,723,051, US-A-4,665,258 and FR-A-2,477,903.
- the present invention relates to a method for isomerizing an aromatic section containing at least one aromatic compound having eight carbon atoms per molecule comprising contacting said section with at least one catalyst comprising at least one metal of group VIII of the periodic classification of the elements, at least one zeolite support comprising a zeolite chosen from zeolites of structure type EUO and MOR, taken alone or as a mixture and at least one matrix, such that the specific surface area of the matrix in the zeolitic support of said catalyst is between 5 and 200 m 2 / g.
- a catalyst in the form of extrudates, balls, or trilobates comprising at least one metal of group VIII of the periodic table of elements, at least one zeolite support comprising a zeolite chosen among the zeolites of structure type EUO and MOR, taken alone or as a mixture and at least one matrix, such as the specific surface of the matrix in the zeolitic support of said catalyst is between 5 and 200 m z / g leads to improved catalytic performances in terms of activity when used in a process for isomerizing an aromatic cut comprising at least one compound aromatic compound with eight carbon atoms per molecule.
- such a catalyst is more active towards the desired products, namely xylenes and in particular paraxylene, than a catalyst of the state of the art.
- the present invention relates to a method for isomerizing an aromatic section containing at least one aromatic compound having eight carbon atoms per molecule comprising contacting said section with at least one catalyst comprising at least one metal of group VIII of the periodic classification of the elements, at least one zeolite support comprising a zeolite chosen from zeolites of structural type EUO and MOR, taken alone or as a mixture and at least one matrix, such that the specific surface of the matrix in the zeolitic support of said catalyst is between 5 and 200 m 2 / g.
- the specific surface of the matrix in the zeolitic support of said catalyst is between 20 and 160 m 2 / g, more preferably between 50 and 160 m 2 / g.
- the catalyst according to the invention advantageously comprises 1 to 90% by weight of zeolite of structure type EUO and / or MOR relative to the total weight of the catalyst.
- the zeolite of structural type EUO is chosen from zeolites EU-, TPZ-3, ZSM-50 or their mixture, preferably the zeolite of structural type EUO is zeolite EU-1.
- the structural type zeolite MOR is Mordenite.
- the zeolite used in the zeolitic support of the catalyst is a mixture of zeolite EU-1 and Mordenite.
- the catalyst according to the invention advantageously comprises a metal content (aux) group VIII between 0.01 and 4% by weight relative to the total weight of the catalyst.
- said catalyst additionally comprises at least one metal chosen from metals of groups IIIA, IVA and VIIB, said metal (s) in a content of less than or equal to 2% by weight relative to the total weight of the catalyst.
- the present invention also relates to a process for preparing the catalyst according to the invention comprising at least the following steps:
- a zeolitic support by shaping said zeolite with at least one matrix iii) the deposition of at least one metal of group VIII of the periodic table of elements on the zeolitic support resulting from stage ii) of shaping
- step i) of synthesis of the zeolite is advantageously followed by at least one calcination step and at least one ion exchange step carried out before the step ii) of implementation. form.
- the shaping step ii) is followed by a drying step carried out at a temperature of between 100 and 150 ° C. for a period of between 5 and 20 hours in an oven and then a calcination step carried out at a temperature between 250 ° C and 750 ° C for a period of between 1 and 8 hours.
- the isomerization process of the feedstock according to the invention in particular an aromatic cut containing at least one aromatic compound having eight carbon atoms per molecule, is advantageously used with the catalyst according to the invention at a temperature of 300.degree. 500 ° C, a hydrogen partial pressure of 0.3 to 1.5 MPa, a total pressure of 0.45 to 1.9 MPa and a feed space velocity, expressed in kilograms of feed introduced per kilogram of catalyst and per hour from 0.25 to 30 hr -1 .
- the present invention relates to a method for isomerizing an aromatic section containing at least one aromatic compound having eight carbon atoms per molecule comprising contacting said section with at least one catalyst comprising at least one metal of group VIII of the classification periodic element, at least one zeolite support comprising a zeolite selected from zeolites of structural type EUO and MOR, taken alone or in mixture and at least one matrix, such that the specific surface of the matrix in the zeolite support of said catalyst is included between 5 and 200 m 2 / g.
- the specific surface area of the matrix in said zeolitic catalyst support is between 5 and 200 m 2 / g, preferably between 20 and 160 m 2 / g, more preferably between 50 and 200 m 2 / g. and 160 m 2 / g, still more preferably between 50 and 150 m 2 / g.
- the zeolite used in the zeolite support of the catalyst used in the process according to the invention is chosen from zeolites of structural type EUO and MOR, taken alone or as a mixture.
- the zeolite of structural type EUO is chosen from zeolites EU-, TPZ-3 and ZSM-50, taken alone or as a mixture and more preferably, the EUO-structural zeolite is EU-1 zeolite.
- the structural type zeolite MOR is Mordenite.
- the zeolite used in the zeolitic support of the catalyst is a mixture of zeolite EU-1 and mordenite.
- the catalyst according to the invention comprises 1 to 90% by weight of zeolite with structure type EUO and / or MOR, preferably 3 to 80% and even more preferably 4 to 60% by weight of zeolite with structure type EUO and / or or MOR with respect to the total weight of the catalyst.
- the catalyst according to the invention advantageously comprises a content of Group VIII metal (s) of between 0.01 and 4% by weight, preferably 0.05 to 2.0% by weight relative to the total weight of the catalyst.
- the total pore volume of the catalyst measured by nitrogen adsorption is between 0.5 cm 3 / g and 1.5 cm 3 / g.
- the catalyst according to the invention has a macroporous volume of less than 0.1 cm 3 / g, preferably less than 0.05 cm 3 / g, the pore volume being defined as being the pore volume having a size greater than 50 nm.
- the mean diameter of the mesopores of the catalyst measured according to the BJH method is greater than 8 nm, preferably greater than 10 nm, preferably greater than 12 nm, the mesopores being understood as being the pores of size between 2 and 50 nm.
- the average diameter of the macropores of the catalyst measured according to the BJH method is greater than 60, preferably between 70 and 200 nm, more preferably between 70 and 150 nm.
- the present invention also relates to the process for preparing the catalyst according to the invention.
- the catalyst according to the invention is prepared according to a process comprising at least the following stages:
- the zeolites used according to the invention are crystalline solids which comprise silicon and at least one element T selected from the group formed by aluminum, iron, gallium and boron, preferably from the group formed by aluminum and boron, and more preferably aluminum; with an overall Si / T atomic ratio greater than 5.
- the zeolites used according to the invention are preferably in acid form, such that the Na / T ratio is less than 15%, preferably less than 10%, more preferably less than 5%.
- EUO-type zeolites have a one-dimensional (10MR) mean pore network with 12-tetrahedral (12MR) side pockets
- the MOR zeolites have a large-pore (2MR) one-dimensional lattice.
- the mode of preparation of the various zeolites is also well known to those skilled in the art.
- the methods for preparing such zeolites comprise the mixing in an aqueous medium of a silicon source, a source of a T element such as aluminum, a source of an alkali metal and a nitrogenous organic compound acting as a structurant.
- the zeolite EU-1 described in the European patent application EP-A-0 042 226, is prepared using, as structuring agent, either the alkylated derivative of a polymethylene ⁇ - ⁇ diammonium or a degradation product of said derivative. or else precursors of said derivative.
- the zeolite TPZ-3 described in European Patent Application EP-A-0 051 318, is prepared using the same family of structurant as that used to synthesize zeoiite EU-1. It is in particular described the use of the compound 1, 6- ⁇ , ⁇ , ⁇ , ⁇ ', ⁇ ', ⁇ '-hexamethylhexamethylenediammonium.
- Zeolite ZSM-50 described in EP 0 159 845 and US-A-4,640,829, is prepared by using as structurant the dibenzyldimethylammonium derivative (DBDMA).
- step i) for preparing the zeolite of the EUO structural type for preparing the zeolites of the EUO structural type according to the invention, one skilled in the art will usefully refer to one or the other of the references cited above describing the preparing such zeolites.
- Mordenite The synthesis of Mordenite is described by Meier et al (Kristallogr 115 (1961)). Kim et al (Zeolites 11 (1991) 745) which describe the synthesis of zeoiite Mordenite in the absence of a nitrogenous organic structurant, using a mixture of sodium hydroxide, sodium aluminate and silica.
- the specific surface of the zeolite resulting from stage i) is advantageously greater than 250 m 2 / g, preferably greater than 350 m 2 / g.
- the zeolite from step i) according to the invention is entirely microporous.
- step i) of synthesis of the zeolite is followed by at least one calcination step and at least one ion exchange step carried out before the shaping step ii).
- Calcination step of the zeolite resulting from step i) Said step of calcining under air flow of the zeolite resulting from said step i) is intended to eliminate the organic structuring agent present in the microporosity of said zeolite, by for example, the cation R 1 R 2 3 -N + - (CH 2 ) n - N + - R 4 R 5 R 6, preferably 1, 6 ⁇ , ⁇ , ⁇ , ⁇ ', ⁇ ', ⁇ '-hexamethylhexamethylene diammonium when the zeolite synthesized during said step i) is zeolite EU-1.
- the zeolite calcination step resulting from said step i) is advantageously carried out at a temperature of between 150 and 600 ° C, preferably between 200 and 600 ° C, more preferably between 250 and 550 ° C for a period of between 1 and 48 hours, preferably for a period of between 1 and 30 hours.
- the zeolite can also undergo after calcination of the zeolite from step i) at least one ion exchange step.
- the ion exchange (s) subsequent to said calcination In dry air stream it is possible to remove at least partly, preferably almost completely, the alkaline cation, in particular sodium, optionally present in the cationic position in the zeolite in its crude synthetic form.
- each ion exchange step is carried out at a temperature preferably between 20 and 150 ° C for a duration advantageously between 2 hours and 10 hours.
- Said ion exchange step is according to the invention carried out by at least one NH 4 NO 3 solution or ammonium acetate solution.
- the method for preparing the catalyst according to the invention is continued by carrying out the step ii) of shaping the zeolite with at least one matrix.
- the step ii) of shaping the zeolite is carried out on the zeolite synthesized according to step i) which has or has not undergone calcination and / or one or more ion exchanges. These last two operations can be performed after step ii) of shaping the zeolite.
- step ii) of shaping of said zeolite of structural type EUO and / or MOR according to the invention is carried out using a matrix chosen from clays, magnesia, aluminas, silicas titanium oxide, boron oxide, zirconia, aluminum phosphates, titanium phosphates, zirconium phosphates, silica-aluminas and coal or a mixture of at least two of these compositions.
- the matrix is an alumina.
- the shaping according to said step ii) consists more particularly in kneading the zeolite chosen from the structural types EUO and / or MOR, in a wet matrix gel, preferably alumina.
- Said wet matrix gel is generally obtained by mixing at least one acid and a matrix powder for a period of time necessary to obtain a good homogeneity of the dough and then forming an object that can be used in a catalytic reactor.
- a matrix powder is a predominantly solid compound and preferably an oxide or hydrate.
- a hydrate and, more preferably, an aluminum hydrate are preferably used. The loss on ignition of this hydrate will be greater than 15%.
- the alumina powders chosen according to the invention include commercial aluminas, such as TH, TM, Pural or Disperal grades from Sasol.
- the shaping can be performed using shaping techniques known to those skilled in the art, such as for example: extrusion, coating, spray drying or pelletizing. For example, by passing said dough thus obtained through a die to form extrudates of diameter advantageously between 0.4 and 4 mm.
- the shaping can also be carried out in the presence of the various constituents of the catalyst and extrusion of the obtained mineral paste, by pelletizing, shaped into beads at the rotating bezel or drum, drop coagulation, oil-drop, oil- up, or any other known method of agglomeration of a powder containing alumina and optionally other ingredients selected from those mentioned above.
- the catalysts used according to the invention are in the form of spheres or extrusions. However, it is advantageous that the catalyst is in the form of extrudates with a length of between 4 and 9 mm and more particularly between 2 and 5 mm.
- the shapes are cylindrical (which can be hollow or not), cylindrical twisted, multilobed (2, 3, 4 or 5 lobes for example), rings.
- the cylindrical shape is preferably used, but any other shape may be used.
- these supports used according to the present invention may have been treated as is well known to those skilled in the art by additives to facilitate the shaping and / or to improve the final mechanical properties of the supports.
- additives there may be mentioned in particular cellulose, carboxymethylcellulose, carboxyethyl cellulose, tall oil, xanthan gums, surfactants, flocculating agents such as polyacrylamides, carbon black, starches, stearic acid, polyacrylic alcohol, polyvinyl alcohol, biopolymers, glucose, polyethylene glycols, etc.
- Extrusion can be performed by any conventional tool, commercially available.
- the paste resulting from the mixing is extruded through a die, for example using a piston or a single screw or twin extrusion screw.
- This extrusion step can be performed by any method known to those skilled in the art.
- the adjustment of the characteristic porosity of the zeolite supports according to the invention, and in particular the specific surface area, is partially carried out during this step of shaping the support particles and any type of matrix known to man is suitable for invention.
- influential shaping parameters are the water content, the acid level, the mixing time. Water can be added or removed to adjust the viscosity of the extrusion paste. This step can be performed at any stage of the kneading step.
- the acid content added to the kneading before shaping is less than 30%, preferably between 0.5 and 30%, more preferably between 0.5 and 20% by weight of the mass.
- Nitric acid is preferred.
- a base to neutralize the paste during the shaping after mixing in the presence of acid, for example ammonia, at a content of between 1 and 50% by weight.
- acid for example ammonia
- the mixing time is advantageously between 5 minutes and 120 minutes, preferably between 5 minutes and 90 minutes, even more preferably between 5 and 60 minutes.
- Zeolite can be added at any time during mixing.
- Traces of impurities may be present in the matrix used according to the invention, for example Na, Fe, Si or sulfur. Their content is preferably limited. According to the invention, the traces of sulfur are less than 0.2% by weight, the traces of Na 2 0 are less than 0.01% by weight, and the traces of Si0 2 and Fe 2 0 3 are less than 0.02% by weight relative to the mass. total of the matrix.
- the zeolite associated with the matrix also called zeolite support in the context of the present invention, is in the form of beads, extrudates or trilobés, advantageously in the form of extrudates or trilobés, more preferably under trilobed form.
- the catalyst according to the invention comprises 1 to 90% by weight of zeolite of structural type EUO and / or MOR, preferably 3 to 80% and even more preferably 4 to 60% by weight of zeolite of structural type EUO and / or MOR, the matrix constituting the 100% complement.
- the specific surface of the zeolite support of the catalyst depends on the amount of zeolite present in the zeolite support. It is equal to the sum of the specific surfaces of the 2 constituents matrix and zeolite, weighted by their mass within the zeolitic support.
- the choice of the matrix used in the invention is such that, after the shaping step ii), the specific surface area of the matrix in the zeolite support is between 5 and 200 m 2 / g, preferably between 20 and 160 m 2 / g, more preferably between 50 and 160 m 2 / g, more preferably between 50 and 150 m 2 / g.
- the BET specific surface area of the matrix is obtained by subtracting the specific surface area of the EUO and / or MOR zeolite (included in the weighted zeolite support of the introduced mass) from the total specific surface area of the zeolitic support of the catalyst.
- the specific surface of the zeolite support is measured at the end of the zeolite support drying and calcination step subsequent to the shaping step ii).
- the shaping step ii) is advantageously followed by a drying step and then a calcination step.
- the drying step is advantageously carried out at a temperature of between 100 and 150 ° C. for a period of between 5 and 20 hours in an oven and the calcination step is advantageously carried out at a temperature of between 250 ° C. and 750 ° C for a period of between 1 and 8 hours. It may be advantageous to carry out this calcination step in the presence of water vapor.
- Step iii) depositing at least one Group VIII metal on the zeolite support
- step iii) which consists in introducing at least one metal of group VIII of the periodic table of elements onto the zeolitic support prepared in step ii).
- said group VIII metal is selected from iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium and platinum, preferably from noble metals platinum, palladium , nickel, iridium and very preferably among palladium and platinum, taken alone or as a mixture. Even more preferably, said group VIII metal is platinum.
- the catalyst according to the invention comprises a content of Group VIII metal (s) of between 0.01 and 4% by weight, preferably 0.05 to 2.0% by weight relative to the total weight of the catalyst.
- step iii) the deposition of said Group VIII metal (s) on the zeolitic support can be carried out by the dry impregnation technique, the technique of impregnation by excess or by ion exchange, preferably, step iii) is carried out by the technique of dry impregnation or ion exchange and more preferably by ion exchange.
- step iii) is carried out by the technique of dry impregnation or ion exchange and more preferably by ion exchange.
- All group VIII metal precursors are suitable for the deposition of one or more Group VIII metals (ux) on the zeolitic support.
- any noble metal of group VIII it is possible to use ammonia compounds or compounds such as, for example, ammonium chloroplatinate, platinum dicarboxylic dichloride, hexahydroxyplatinic acid, palladium or palladium nitrate. Platinum is advantageously introduced in the form of hexachloroplatinic acid.
- the introduction of the Group VIII noble metal is preferably carried out by impregnation with an aqueous or organic solution of one of the metal compounds mentioned above.
- paraffinic, naphthenic or aromatic hydrocarbons containing, for example, from 6 to 12 carbon atoms per molecule
- halogenated organic compounds containing, for example, from 1 to 12 carbon atoms per molecule.
- Solvent mixtures can also be used.
- step iii) of deposition of the Group VIII metal on the zeolite support resulting from the shaping step ii) the control of certain parameters implemented, in particular the nature of the precursor of the metal (s) (ux) of the group VIII used (s) and / or the impregnation technique, can guide the deposit of (es) said (s) metal (ux) mainly on the matrix or on the zeolite or statistically on the zeolite-matrix set namely the entire zeolitic support.
- the group VIII metal (s), preferably platinum and / or palladium, predominantly on the matrix it is possible to carry out anionic exchange with hexachloroplatinic acid and / or hexachloropalladic acid, in the presence of a competing agent, for example hydrochloric acid.
- a competing agent for example hydrochloric acid.
- This deposit is preferably followed by calcination, for example at a temperature between 350 and 550 ° C and for a period of between 1 and 4 hours.
- the group VIII metal (s) is (are) predominantly deposited on the matrix and the said metal (s) exhibit good dispersion and stability. good macroscopic distribution through the catalyst grain.
- the precursor may for example be chosen from:
- ammonia compounds such as tetrammine platinum (II) salts of formula
- X being a halogen selected from the group consisting of chlorine, fluorine, bromine and iodine, X being preferably chlorine, and "acac" representing the acetylacetonate group (of formula C5H7O2), derived from acetylacetone .
- the group VIII metal (s) is (are) deposited predominantly on the zeolite and the said metal (s) present (s) a good dispersion and a good macroscopic distribution through the catalyst grain.
- step iii) of depositing the Group VIII metal on the zeolitic support is preferably carried out by ion exchange with hexachloroplatinic acid.
- step iii) comprises the further deposition of at least one additional metal selected from the metals of groups NIA, IVA and VIIB.
- Said metal chosen from the metals of groups IIIA, IVA and VIIB is advantageously chosen from gallium, indium, tin and rhenium, preferably from indium, tin and rhenium.
- the catalyst according to the invention advantageously comprises the said metal (s) in a content less than or equal to 2% by weight relative to the total weight of the catalyst.
- this content is between 0.01 and 2%, preferably between 0.05 and 1.0% by weight relative to the total weight of the catalyst.
- the catalyst used in the isomerization process of the invention also contains at least one additional metal selected from the metals of groups IIIA, IVA and VIIB
- all the techniques of deposition of such a metal known from the skilled in the art and all the precursors of such metals may be suitable.
- Group VIII metal (s) and Group IIIA, IVA and VIIB metal (s) may be added either separately or simultaneously in at least one unit step. When at least one Group IIIA, IVA and VIIB metal is added separately, it is preferred that it be added after the Group VIII metal.
- the additional metal selected from the metals of groups NIA, IVA and VIIB may be introduced via compounds such as, for example, the chlorides, bromides and nitrates of metals of groups IIIA, IVA and VIIB.
- compounds such as, for example, the chlorides, bromides and nitrates of metals of groups IIIA, IVA and VIIB.
- indium nitrate or chloride is advantageously used, and in the case of rhenium, perrhenic acid is advantageously used.
- tin chlorides SnCl 2 and SnCl 4 are preferred.
- the additional metal chosen from the metals of groups IIIA, IVA and VIIB may also be introduced in the form of at least one organic compound chosen from the group consisting of the complexes of said metal, in particular the metal polyketone complexes and the hydrocarbylmetals such as alkyls, cycloalkyls, aryls, alkylaryls and arylalkyls.
- the introduction of the metal is advantageously carried out using a solution of the organometallic compound of said metal in an organic solvent.
- Compounds can also be used organohalogenated metal.
- organic compounds of metals there may be mentioned in particular tetrabutyltin, in the case of tin, and triphenylindium, in the case of indium.
- intermediate treatments such as, for example, calcination and / or reduction may be applied between the successive deposits of the different metals.
- the preparation of the catalyst according to the invention is advantageously terminated by calcination, preferably at a temperature of between 250 ° C. and 600 ° C., for a duration of between 0.5 and 10 hours.
- the calcination is preferably preceded by drying, for example in an oven, at a temperature of between 25 ° C. and 250 ° C., preferably between 40 ° C. and 200 ° C. Said drying step is preferably conducted during the rise in temperature necessary to effect said calcination. It is possible to carry out a preliminary reduction of the ex situ catalyst, under a stream of hydrogen, for example at a temperature of 450 ° C. to 600 ° C., for a period of 0.5 to 4 hours.
- the deposition of said Group VIII metal (s) is advantageously carried out in such a way that the dispersion of said metal (s), determined by chemisorption, is from 50% to 100% preferably from 60% to 100% and even more preferably from 70% to 100%.
- the deposition of said Group VIII metal (s) is also advantageously carried out so as to obtain a good distribution of said metal (s) in the shaped catalyst. This distribution is characterized by its profile obtained by microprobe of Castaing.
- the ratio of the concentrations of each element of group VIII to the heart of the grain with respect to the edge of this same grain, defined as the distribution coefficient, is advantageously from 0.6: 1 to 1, 34: 1, preferably from 0 to , 7: 1 to 1, 3: 1.
- the sulfur is introduced on the shaped catalyst, calcined, containing the metal or metals mentioned above, either in situ before the catalytic reaction, or ex situ. Possible sulphurisation occurs after the reduction.
- in situ sulfurization the reduction, if the catalyst has not been reduced beforehand, occurs before the sulfurization.
- ex situ sulphurization reduction is carried out and then sulphurization.
- the Sulfurization is carried out in the presence of hydrogen using any sulphurizing agent well known to those skilled in the art, such as, for example, dimethyl sulphide or hydrogen sulphide.
- the catalyst is treated with a dimethyl sulfide-containing filler in the presence of hydrogen, with a concentration such that the sulfur / metal atomic ratio is 1.5.
- the catalyst is then maintained for about 3 hours at about 400 ° C under hydrogen flow prior to feed injection.
- the sulfur content in the catalyst is such that the ratio of the number of sulfur atoms to the number of metal atoms of the group VIII deposited is up to 2: 1, preferably from 0.5: 1 to 2: 1.
- the isomerization process according to the invention comprises contacting an aromatic section containing at least one aromatic compound having eight carbon atoms per molecule with at least said catalyst described above in the present description.
- said aromatic cut comprises in particular either only a mixture of xylenes, or only ethylbenzene, or a mixture of xylene (s) and ethylbenzene.
- Said isomerization process according to the invention is generally carried out according to the following operating conditions:
- a feed space velocity expressed in kilograms of feed introduced per kilogram of catalyst per hour, from 0.25 to 30 h -1 , preferably from 1 to 10 h -1 and more preferably from 2 to 6 h "1 .
- the raw material used is a synthetic crude zeolite EU-1, comprising the organic structuring agent namely 1, 6 ⁇ , ⁇ , ⁇ , ⁇ ', ⁇ ', ⁇ '-hexamethylhexamethylene diammonium and which has an Si / Si atomic ratio.
- a global AI equal to 15.3 and a weight content of sodium corresponding to an atomic ratio Na / Al (in%) equal to 30.8.
- This zeolite was synthesized according to teaching of EP-B1 -0.042.226.
- the reaction mixture has the following molar composition: 60 SiO 2 : 10.6 Na 2 O: 5.27 NaBr: 1.5 Al 2 O 3 : 19.5 Hexa-Br 2 : 2777 H 2 O. Hexa-Br 2 being 1, 6 ⁇ , ⁇ , ⁇ , ⁇ ', ⁇ ', ⁇ '-hexamethylhexamethylene diammonium, bromine being the counter-ion.
- the reaction mixture is placed in an autoclave with stirring (300 rpm) for 5 days at 180 ° C.
- This EU-1 zeolite is first subjected to so-called dry calcination at 550 ° C. under a flow of dry air for 24 hours so as to eliminate the organic structurant.
- the solid obtained is then subjected to four ion exchanges in a solution of 10N NH 4 NO 3 at about 100 ° C. for 4 hours for each exchange.
- the zeolite EU-1 thus prepared has a BET surface area of 410 m 2 / g.
- Example 2 Preparation of catalyst A comprising an EU-1 zeolite
- the EU-1 zeolite (1) obtained in Example 1 is then shaped by extrusion with a commercial alumina gel (Pural SB3 from Sasol) so as to obtain, after drying at a temperature of 100 ° C. for 1 night and calcination in dry air carried out at a temperature of 450 ° C. for 4 hours, the support S1 which contains, by weight, 8% of zeolite EU-1 and 92% alumina.
- a commercial alumina gel Pural SB3 from Sasol
- the support S1 has a specific surface area of 266 m 2 / g.
- This support S1 is subjected to anion exchange with hexachloroplatinic acid in the presence of hydrochloric acid as a competing agent, so as to deposit 0.3% by weight of platinum based on the weight of the catalyst.
- the wet solid is then dried at 120 ° C for 12 hours and calcined under a dry air flow rate at 500 ° C for one hour.
- Catalyst A thus obtained contains, by weight, 8% of EU-1 zeolite, 91.7% of alumina and 0.3% of platinum.
- Example 3 (in conformity): Preparation of catalyst B comprising an EU-1 zeolite
- the EU-1 zeolite (1) obtained in Example 1 is then shaped by extrusion with a commercial alumina gel (Pural TH100 from Sasol) so as to obtain, after drying at a temperature equal to 100 ° C. for 1 night and calcination under dry air at a temperature equal to 450 ° C. for 4 hours, the support S 2 which contains, by weight, 8% of EU-1 zeolite and 92% of alumina.
- a commercial alumina gel Physical TH100 from Sasol
- the support S2 has a specific surface of 180 m 2 / g
- This support S2 is subjected to anion exchange with hexachloroplatinic acid in the presence of hydrochloric acid as a competing agent, so as to deposit 0.3% by weight of platinum based on the weight of the catalyst.
- the wet solid is then dried at 120 ° C for 12 hours and calcined under a dry air flow rate at 500 ° C for one hour.
- the catalyst B thus obtained contains, by weight, 8% of EU-1 zeolite, 91.7% of alumina and 0.3% of platinum.
- the catalysts were evaluated in terms of ethylbenzene conversion and selectivity to xylenes.
- the selectivity to xylenes is calculated using the yield of xylenes produced.
- the yield of xylenes is determined from the mass percentage of the xylenes produced, obtained by analysis of each effluent.
- the conversion of ethylbenzene is the percentage of ethylbenzene consumed.
- Table 1 Conversion of ethylbenzene and selectivity to xylenes on catalysts A, B
- the results presented in Table 1 show that the catalyst B leads to a much better catalytic performance in terms of ethylbenzene conversion than that obtained using the catalyst A. Moreover, the catalyst B according to the invention leads to a selectivity in xylenes improved compared to that obtained with the catalyst A, consequently the catalyst B according to the invention leads to a yield of xylenes much higher than the yield of xylenes obtained with the comparative catalyst A, the yield of xylenes being the product of the conversion of ethylbenzene by selectivity to xylenes.
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Abstract
The invention relates to a method for isomerizing an aromatic fraction comprising at least one aromatic compound having eight carbon atoms per molecule, which comprises contacting said fraction with at least one catalyst including at least one metal of Group VIII of the periodic table of the elements, at least one zeolite support including a zeolite selected from among the zeolites having an EUO and MOR structure type, taken alone or in a mixture, and at least one matrix, such that the specific surface area of the matrix in the zeolite support of said catalyst is between 5 and 200 m2/g.
Description
PROCEDE D'ISOMERISATION D'UNE COUPE C8 AROMATIQUE EN PRESENCE D'UN CATALYSEUR A BASE D'UNE ZEOLITHE EUO ET D'UN LIANT PARTICULIER PROCESS FOR ISOMERIZING AN AROMATIC C8 CUT IN THE PRESENCE OF A CATALYST BASED ON A EUO ZEOLITE AND A PARTICULAR BINDER
Domaine de l'invention Field of the invention
La présente invention se rapporte à l'isomérisation d'une coupe aromatique contenant au moins un composé aromatique à huit atomes de carbone par molécule en vue de la production de xylènes et en particulier, de para-xylène. La présente invention concerne plus particulièrement un procédé d'isomérisation d'une charge aromatique comprenant au moins un composé aromatique à huit atomes de carbone par molécule visant à maximiser la production de para-xylène, ledit procédé d'isomérisation mettant en oeuvre une catalyseur comprenant au moins un métal du groupe VIII supporté sur un support zéolithique particulier. La présente invention se rapporte également au procédé de préparation dudit catalyseur. The present invention relates to the isomerization of an aromatic cut containing at least one aromatic compound with eight carbon atoms per molecule for the production of xylenes and in particular para-xylene. The present invention relates more particularly to a method of isomerization of an aromatic filler comprising at least one aromatic compound with eight carbon atoms per molecule to maximize the production of para-xylene, said isomerization process using a catalyst comprising at least one Group VIII metal supported on a particular zeolite support. The present invention also relates to the process for preparing said catalyst.
État de la technique antérieure State of the art
Les formulations catalytiques d'isomérisation des xylènes connues de l'homme de l'art sont généralement à base d'une zéoiithe et d'un métal du groupe VIII mis en forme avec un liant, souvent aluminique. Parmi les zéolithes utilisées en isomérisation des coupes C8 aromatiques, on trouve la ZSM-5, utilisée seule ou en mélange avec d'autres zéolithes, comme par exemple la mordénite. Ces catalyseurs sont notamment décrits dans les brevets US-A-4 467 129, US-A-4 482 773 et EP-B- 13 617. D'autres catalyseurs principalement à base de mordénite ont été décrits par exemple dans les brevets US-A-4 723 051 , US-A-4 665 258 et FR-A-2 477 903. Plus récemment, il a été proposé un catalyseur à base d'une zéoiithe de type structural EUO (EP-A1-923 987). La demande de brevet WO- A-2005/065 380 décrit l'utilisation d'une zéoiithe de type structural MTW en isomérisation des xylènes et de l'éthylbenzène. La demande WO2010/000652 décrit l'utilisation d'un catalyseur constitué de zéoiithe ZSM-12 et d'un liant aluminique, ayant un volume poreux supérieur à 0,6 m3/g et une surface spécifique supérieure à 250 m2/g. The catalytic isomerization formulations of xylenes known to those skilled in the art are generally based on a zeolite and a Group VIII metal shaped with a binder, often aluminum. Among the zeolites used in isomerization of aromatic C8 cuts, there is ZSM-5, used alone or mixed with other zeolites, such as mordenite. These catalysts are described in particular in US Pat. No. 4,467,129, US Pat. No. 4,482,773 and EP-B-13,617. Other catalysts mainly based on mordenite have been described, for example, in US Pat. A-4,723,051, US-A-4,665,258 and FR-A-2,477,903. More recently, it has been proposed a catalyst based on a zeolite of structural type EUO (EP-A1-923 987). The patent application WO-A-2005/065 380 describes the use of a zeolite of MTW structural type in isomerization of xylenes and ethylbenzene. Application WO2010 / 000652 describes the use of a catalyst consisting of zeolite ZSM-12 and an aluminum binder, having a pore volume greater than 0.6 m 3 / g and a specific surface area greater than 250 m 2 / g .
Objet et intérêt de l'invention Object and interest of the invention
La présente invention concerne un procédé d'isomérisation d'une coupe aromatique contenant au moins un composé aromatique ayant huit atomes de carbone par molécule comprenant la mise en contact de ladite coupe avec au moins un catalyseur comprenant au moins un métal du groupe VIII de la classification périodique des éléments, au moins un support zéolithique comprenant une zéoiithe choisie parmi les zéolithes de type structural EUO et MOR, prises seules ou en mélange et au moins une matrice, tel que la surface spécifique de la matrice dans le support zéolithique dudit catalyseur est comprise entre 5 et 200 m2/g. The present invention relates to a method for isomerizing an aromatic section containing at least one aromatic compound having eight carbon atoms per molecule comprising contacting said section with at least one catalyst comprising at least one metal of group VIII of the periodic classification of the elements, at least one zeolite support comprising a zeolite chosen from zeolites of structure type EUO and MOR, taken alone or as a mixture and at least one matrix, such that the specific surface area of the matrix in the zeolitic support of said catalyst is between 5 and 200 m 2 / g.
Il a été découvert, de façon surprenante, qu'un catalyseur, sous forme d'extrudés, tJe billes, ou de trilobés comprenant au moins un métal du groupe VIII de la classification périodique des éléments, au moins un support zéolithique comprenant une zéoiithe choisie parmi les zéolithes de type structural EUO et MOR, prises seule ou en mélange et au moins une matrice, tel que la surface spécifique de la
matrice dans le support zéolithique dudit catalyseur est comprise entre 5 et 200 mz/g, conduit à des performances catalytiques améliorées en terme d'activité lorsqu'il est utilisé dans un procédé d'isomérisation d'une coupe aromatique comprenant au moins un composé aromatique à huit atomes de carbone par molécule. En particulier, un tel catalyseur est plus actif envers les produits recherchés, à savoir les xylènes et en particulier le paraxyléne, qu'un catalyseur de l'état de la technique. It has surprisingly been found that a catalyst, in the form of extrudates, balls, or trilobates comprising at least one metal of group VIII of the periodic table of elements, at least one zeolite support comprising a zeolite chosen among the zeolites of structure type EUO and MOR, taken alone or as a mixture and at least one matrix, such as the specific surface of the matrix in the zeolitic support of said catalyst is between 5 and 200 m z / g leads to improved catalytic performances in terms of activity when used in a process for isomerizing an aromatic cut comprising at least one compound aromatic compound with eight carbon atoms per molecule. In particular, such a catalyst is more active towards the desired products, namely xylenes and in particular paraxylene, than a catalyst of the state of the art.
Description de l'invention Description of the invention
Résumé de l'invention Summary of the invention
La présente invention concerne un procédé d'isomérisation d'une coupe aromatique contenant au moins un composé aromatique ayant huit atomes de carbone par molécule comprenant la mise en contact de ladite coupe avec au moins un catalyseur comprenant au moins un métal du groupe VIII de la classification périodique des éléments, au moins un support zéolithique comprenant une zéolithe choisie parmi les zéolithes de type structural EUO et MOR, prises seule ou en mélange et au moins une matrice, tel que la surface spécifique de la matrice dans le support zéolithique dudit catalyseur est comprise entre 5 et 200 m2/g. The present invention relates to a method for isomerizing an aromatic section containing at least one aromatic compound having eight carbon atoms per molecule comprising contacting said section with at least one catalyst comprising at least one metal of group VIII of the periodic classification of the elements, at least one zeolite support comprising a zeolite chosen from zeolites of structural type EUO and MOR, taken alone or as a mixture and at least one matrix, such that the specific surface of the matrix in the zeolitic support of said catalyst is between 5 and 200 m 2 / g.
De manière préférée selon l'invention, la surface spécifique de la matrice dans le support zéolithique dudit catalyseur est comprise entre 20 et 160 m2/g, de manière plus préférée entre 50 et 160 m2/g.In a preferred manner according to the invention, the specific surface of the matrix in the zeolitic support of said catalyst is between 20 and 160 m 2 / g, more preferably between 50 and 160 m 2 / g.
Le catalyseur selon l'invention comprend avantageusement 1 à 90 % poids de zéolithe de type structural EUO et/ou MOR par rapport au poids total du catalyseur. Selon l'invention, la zéolithe de type structural EUO est choisie parmi les zéolithes EU- , TPZ-3, ZSM-50 ou leur mélange, de manière préférée la zéolithe de type structural EUO est la zéolithe EU-1. Selon l'invention, la zéolithe de type structural MOR est la Mordénite. De manière avantageuse, la zéolithe utilisée dans le support zéolithique du catalyseur est un mélange de la zéolithe EU-1 et de la Mordénite The catalyst according to the invention advantageously comprises 1 to 90% by weight of zeolite of structure type EUO and / or MOR relative to the total weight of the catalyst. According to the invention, the zeolite of structural type EUO is chosen from zeolites EU-, TPZ-3, ZSM-50 or their mixture, preferably the zeolite of structural type EUO is zeolite EU-1. According to the invention, the structural type zeolite MOR is Mordenite. Advantageously, the zeolite used in the zeolitic support of the catalyst is a mixture of zeolite EU-1 and Mordenite.
Le catalyseur selon l'invention comprend avantageusement une teneur en métal(aux) du groupe VIII comprise entre 0,01 et 4 % en poids par rapport au poids total du catalyseur. The catalyst according to the invention advantageously comprises a metal content (aux) group VIII between 0.01 and 4% by weight relative to the total weight of the catalyst.
Dans une variante selon l'invention, ledit catalyseur comprend en outre au moins un métal choisi parmi les métaux des groupes IIIA, IVA et VIIB, le(s)dit(s) métal (aux) dans une teneur inférieure ou égale à 2 % en poids par rapport au poids total du catalyseur. La présente invention concerne également un procédé de préparation du catalyseur selon l'invention comprenant au moins les étapes suivantes : In a variant according to the invention, said catalyst additionally comprises at least one metal chosen from metals of groups IIIA, IVA and VIIB, said metal (s) in a content of less than or equal to 2% by weight relative to the total weight of the catalyst. The present invention also relates to a process for preparing the catalyst according to the invention comprising at least the following steps:
i) la synthèse d'au moins une zéolithe de type structural EUO et/ou MOR, i) the synthesis of at least one zeolite of structure type EUO and / or MOR,
ii) la préparation d'un support zéolithique par la mise en forme de ladite zéolithe avec au moins une matrice
iii) le dépôt d'au moins un métal du groupe VIII de la classification périodique des éléments sur le support zéolithique issu de l'étape ii) de mise en forme ii) preparing a zeolitic support by shaping said zeolite with at least one matrix iii) the deposition of at least one metal of group VIII of the periodic table of elements on the zeolitic support resulting from stage ii) of shaping
Selon le procédé de l'invention, l'étape i) de synthèse de la zéolithe est avantageusement suivie d'au moins une étape de calcination et d'au moins une étape d'échange ionique réalisées avant l'étape ii) de mise en forme. According to the process of the invention, step i) of synthesis of the zeolite is advantageously followed by at least one calcination step and at least one ion exchange step carried out before the step ii) of implementation. form.
Selon le procédé de l'invention, l'étape ii) de mise en forme est suivie d'une étape de séchage réalisée à une température comprise entre 100 et 150°C pendant une durée comprise entre 5 et 20 heures en étuve puis d'une étape de calcination réalisée à une température comprise entre 250°C et 750°C pendant une durée comprise entre 1 et 8 heures. According to the process of the invention, the shaping step ii) is followed by a drying step carried out at a temperature of between 100 and 150 ° C. for a period of between 5 and 20 hours in an oven and then a calcination step carried out at a temperature between 250 ° C and 750 ° C for a period of between 1 and 8 hours.
Le procédé d'isomérisation de la charge selon l'invention, notamment une coupe aromatique contenant au moins un composé aromatique ayant huit atomes de carbone par molécule est avantageusement mis en oeuvre avec le catalyseur selon l'invention à une température de 300°C à 500°C, une pression partielle d'hydrogène de 0,3 à 1 ,5 MPa, une pression totale de 0,45 à 1 ,9 MPa et une vitesse spatiale d'alimentation, exprimée en kilogramme de charge introduite par kilogramme de catalyseur et par heure de 0,25 à 30 h"1. The isomerization process of the feedstock according to the invention, in particular an aromatic cut containing at least one aromatic compound having eight carbon atoms per molecule, is advantageously used with the catalyst according to the invention at a temperature of 300.degree. 500 ° C, a hydrogen partial pressure of 0.3 to 1.5 MPa, a total pressure of 0.45 to 1.9 MPa and a feed space velocity, expressed in kilograms of feed introduced per kilogram of catalyst and per hour from 0.25 to 30 hr -1 .
Description détaillée de l'invention Detailed description of the invention
La présente invention concerne un procédé d'isomérisation d'une coupe aromatique contenant au moins un composé aromatique ayant huit atomes de carbone par molécule comprenant la mise en contact de ladite coupe avec au moins un catalyseur comprenant moins un métal du groupe VIII de la classification périodique des éléments, au moins un support zéolithique comprenant une zéolithe choisie parmi les zéolithes de type structural EUO et MOR, prises seule ou en mélange et au moins une matrice, tel que la surface spécifique de la matrice dans le support zéolithique dudit catalyseur est comprise entre 5 et 200 m2/g. The present invention relates to a method for isomerizing an aromatic section containing at least one aromatic compound having eight carbon atoms per molecule comprising contacting said section with at least one catalyst comprising at least one metal of group VIII of the classification periodic element, at least one zeolite support comprising a zeolite selected from zeolites of structural type EUO and MOR, taken alone or in mixture and at least one matrix, such that the specific surface of the matrix in the zeolite support of said catalyst is included between 5 and 200 m 2 / g.
Dans une variante du procédé selon l'invention, la surface spécifique de la matrice dans ledit support zéolithique du catalyseur est comprise entre 5 et 200 m2/g, de préférence entre 20 et 160 m2/g, de manière plus préférée entre 50 et 160 m2/g, de manière encore pus préférée entre 50 et 150 m2/g. Selon l'invention, la zéolithe utilisée dans le support zéolithique du catalyseur mis en œuvre dans le procédé selon l'invention est choisie parmi les zéolithes de type structural EUO et MOR, prises seules ou en mélange. De préférence, la zéolithe de type structural EUO est choisie parmi les zéolithes EU- ,
TPZ-3 et ZSM-50, prises seules ou en mélange et de manière plus préférée, la zéolithe de type structural EUO est la zéolithe EU-1. Selon l'invention, la zéolithe de type structural MOR est la Mordénite. Dans une variante selon l'invention, la zéolithe utilisée dans le support zéolithique du catalyseur est un mélange de la zéolithe EU-1 et de la mordénite. In a variant of the process according to the invention, the specific surface area of the matrix in said zeolitic catalyst support is between 5 and 200 m 2 / g, preferably between 20 and 160 m 2 / g, more preferably between 50 and 200 m 2 / g. and 160 m 2 / g, still more preferably between 50 and 150 m 2 / g. According to the invention, the zeolite used in the zeolite support of the catalyst used in the process according to the invention is chosen from zeolites of structural type EUO and MOR, taken alone or as a mixture. Preferably, the zeolite of structural type EUO is chosen from zeolites EU-, TPZ-3 and ZSM-50, taken alone or as a mixture and more preferably, the EUO-structural zeolite is EU-1 zeolite. According to the invention, the structural type zeolite MOR is Mordenite. In a variant according to the invention, the zeolite used in the zeolitic support of the catalyst is a mixture of zeolite EU-1 and mordenite.
Avantageusement, le catalyseur selon l'invention comprend 1 à 90 % poids de zéolithe de type structural EUO et/ou MOR, de préférence 3 à 80 % et de manière encore plus préférée 4 à 60 % poids de zéolithe de type structural EUO et/ou MOR par rapport au poids total du catalyseur. Le catalyseur selon l'invention comprend avantageusement une teneur en métal(aux) du groupe VIII comprise entre 0,01 et 4 % en poids, de préférence de 0,05 à 2,0 % poids par rapport au poids total du catalyseur. Advantageously, the catalyst according to the invention comprises 1 to 90% by weight of zeolite with structure type EUO and / or MOR, preferably 3 to 80% and even more preferably 4 to 60% by weight of zeolite with structure type EUO and / or or MOR with respect to the total weight of the catalyst. The catalyst according to the invention advantageously comprises a content of Group VIII metal (s) of between 0.01 and 4% by weight, preferably 0.05 to 2.0% by weight relative to the total weight of the catalyst.
Selon l'invention, le volume poreux total du catalyseur mesuré par adsorption d'azote est compris entre 0.5 cm3/g et 1.5 cm3/g. According to the invention, the total pore volume of the catalyst measured by nitrogen adsorption is between 0.5 cm 3 / g and 1.5 cm 3 / g.
De préférence, le catalyseur selon l'invention présente un volume macroporeux inférieur à 0.1 cm3/g, de préférence inférieur à 0.05 cm3/g, le volume poreux étant défini comment étant le volume des pores ayant une taille supérieure à 50 nm. Preferably, the catalyst according to the invention has a macroporous volume of less than 0.1 cm 3 / g, preferably less than 0.05 cm 3 / g, the pore volume being defined as being the pore volume having a size greater than 50 nm.
Selon l'invention, le diamètre moyen des mésopores du catalyseur mesuré selon la méthode BJH (d Vmeso/2) est supérieur à 8 nm, de préférence supérieur à 10 nm, de préférence supérieur à 12 nm, les mésopores étant entendu comme étant les pores de taille comprise entre 2 et 50 nm. Le diamètre moyen des macropores du catalyseur mesuré selon la méthode BJH (d Vmacro/2) est supérieur à 60, de préférence comprise entre 70 et 200 nm, de manière plus préférée comprise entre 70 et 150 nm. According to the invention, the mean diameter of the mesopores of the catalyst measured according to the BJH method (d Vmeso / 2) is greater than 8 nm, preferably greater than 10 nm, preferably greater than 12 nm, the mesopores being understood as being the pores of size between 2 and 50 nm. The average diameter of the macropores of the catalyst measured according to the BJH method (d Vmacro / 2) is greater than 60, preferably between 70 and 200 nm, more preferably between 70 and 150 nm.
Techniques de caractérisation Characterization techniques
On définit la surface spécifique par la surface spécifique B. ET. déterminée par adsorption d'azote conformément à la norme ASTM D 3663-78 établie à partir de la méthode BRUNAUER-EMMETT- TELLER décrite dans le périodique « The Journal of American Society", 60, 309, (1938). La distribution poreuse mesurée par adsorption d'azote a été déterminée par le modèle Barrett- Joyner-Halenda (BJH). L'isotherme d'adsorption - désorption d'azote selon le modèle BJH est décrit dans le périodique "The Journal of American Society", 73, 373, (1951) écrit par E.P.Barrett, L.G.Joyner
et P.P.Halenda. On entend par volume adsorption azote, le volume mesuré pour P/P0= 0.99, pression pour laquelle il est admis que l'azote a rempli tous les pores. On définit le diamètre moyen désorption azote comme étant un diamètre tel que tous les pores inférieurs à ce diamètre constituent 50% du volume poreux (Vp) mesuré sur la branche de désorption de l'isotherme azote. The specific surface is defined by the specific surface area B. ET. determined by nitrogen adsorption in accordance with ASTM D 3663-78 established from the BRUNAUER-EMMETT-TELLER method described in the Journal of the American Society, 60, 309, (1938). Nitrogen adsorption was determined by the Barrett-Joyner-Halenda model (BJH) The nitrogen adsorption-desorption isotherm according to the BJH model is described in the journal "The Journal of American Society", 73, 373, (1951) written by EPBarrett, LGJoyner and PPHalenda. Nitrogen adsorption volume means the volume measured for P / P 0 = 0.99, pressure for which it is assumed that nitrogen has filled all the pores. The average nitrogen desorption diameter is defined as a diameter such that all the pores smaller than this diameter constitute 50% of the pore volume (Vp) measured on the desorption branch of the nitrogen isotherm.
La présente invention concerne également le procédé de préparation du catalyseur selon l'invention. Le catalyseur selon l'invention est préparé selon un procédé comprenant au moins les étapes suivantes : The present invention also relates to the process for preparing the catalyst according to the invention. The catalyst according to the invention is prepared according to a process comprising at least the following stages:
i) la synthèse d'au moins une zéolithe de type structural EUO et/ou MOR, i) the synthesis of at least one zeolite of structure type EUO and / or MOR,
ii) la préparation d'un support zéolithique par la mise en forme de ladite zéolithe avec au moins une matrice ii) preparing a zeolitic support by shaping said zeolite with at least one matrix
iii) le dépôt d'au moins un métal du groupe VIII de la classification périodique des éléments sur le support zéolithique issu de l'étape ii) de mise en forme iii) the deposition of at least one metal of group VIII of the periodic table of elements on the zeolitic support resulting from stage ii) of shaping
Étape i) de synthèse de la zéolithe Step i) synthesis of the zeolite
Les zéolithes utilisées selon l'invention sont des solides cristallisés qui comprennent du silicium et au moins un élément T choisi dans le groupe formé par l'aluminium, le fer, le gallium et le bore, de préférence dans le groupe formé l'aluminium et le bore, et de manière plus préférée l'aluminium; avec un rapport Si/T atomique global supérieur à 5. Les zéolithes utilisées selon l'invention sont de préférence sous forme acide, tel que le rapport Na/T soit inférieur à 15%, de préférence inférieur à 10%, de manière plus préférée inférieure à 5%. The zeolites used according to the invention are crystalline solids which comprise silicon and at least one element T selected from the group formed by aluminum, iron, gallium and boron, preferably from the group formed by aluminum and boron, and more preferably aluminum; with an overall Si / T atomic ratio greater than 5. The zeolites used according to the invention are preferably in acid form, such that the Na / T ratio is less than 15%, preferably less than 10%, more preferably less than 5%.
Les zéolithes de type structural EUO et/ou MOR décrites sont bien connues de l'art antérieur et leur structure poreuse et topographie est définie dans P'Atlas of Zeolite Framework Types", Ch. Baerlocher, W.M. Meier, D.H. Oison, 7ème édition, 2007). Les zéolithes de type EUO présentent un réseau de pores moyens (10MR) monodimensionnel avec des poches latérale à 12 atomes tétraédriques (12MR). Les , zéolithes de type MOR présentent un réseau monodimensionnel à large pores ( 2MR). Zeolites with structure type EUO and / or MOR described are well known in the prior art and their porous structure and topography is defined in P'Atlas of Zeolite Framework Types ", Ch. Baerlocher, WM Meier, DH Olson, 7th edition , 2007) EUO-type zeolites have a one-dimensional (10MR) mean pore network with 12-tetrahedral (12MR) side pockets The MOR zeolites have a large-pore (2MR) one-dimensional lattice.
Le mode de préparation des différentes zéolithes est également bien connu de l'homme du métier. De manière générale, les méthodes de préparation de telles zéolithes comprennent le mélange en milieu aqueux d'une source de silicium, d'une source d'un élément T tel que l'aluminium, d'une source d'un métal alcalin et d'un composé organique azoté jouant le rôle de structurant. La zéolithe EU-1 , décrite dans la demande de brevet européenne EP-A-0 042 226, est préparée en utilisant comme structurant soit le dérivé alkylé d'une polyméthylène α-ω diammonium, soit un produit de dégradation dudit dérivé
soit encore des précurseurs dudit dérivé. La zéoiithe TPZ-3, décrite dans la demande de brevet européenne EP-A-0 051 318, est préparée en utilisant la même famille de structurant que celle employée pour synthétiser la zéoiithe EU-1. Il est notamment décrit l'utilisation du composé 1 ,6- Ν,Ν,Ν,Ν',Ν',Ν'-hexaméthylhexaméthylènediammonium. La zéoiithe ZSM-50, décrite dans les documents EP 0 159 845 et US-A-4,640,829, est préparée en utilisant comme structurant le dérivé dibenzyldiméthylammonium (DBDMA). The mode of preparation of the various zeolites is also well known to those skilled in the art. In general, the methods for preparing such zeolites comprise the mixing in an aqueous medium of a silicon source, a source of a T element such as aluminum, a source of an alkali metal and a nitrogenous organic compound acting as a structurant. The zeolite EU-1, described in the European patent application EP-A-0 042 226, is prepared using, as structuring agent, either the alkylated derivative of a polymethylene α-ω diammonium or a degradation product of said derivative. or else precursors of said derivative. The zeolite TPZ-3, described in European Patent Application EP-A-0 051 318, is prepared using the same family of structurant as that used to synthesize zeoiite EU-1. It is in particular described the use of the compound 1, 6- Ν, Ν, Ν, Ν ', Ν', Ν'-hexamethylhexamethylenediammonium. Zeolite ZSM-50, described in EP 0 159 845 and US-A-4,640,829, is prepared by using as structurant the dibenzyldimethylammonium derivative (DBDMA).
Aussi, pour la mise en oeuvre de ladite étape i) de préparation de la zéoiithe de type structural EUO selon l'invention, l'homme du métier se référera utilement à l'une ou l'autre des références citées ci- dessus décrivant la préparation de telles zéolithes. Also, for the implementation of said step i) for preparing the zeolite of the EUO structural type according to the invention, one skilled in the art will usefully refer to one or the other of the references cited above describing the preparing such zeolites.
La synthèse de la Mordénite est décrite par Meier et al (Kristallogr 115 (1961)). Kim et al (Zeolites 11 (1991) 745) qui décrivent la synthèse de la zéoiithe Mordénite en l'absence d'un structurant organique azoté, en mettant en œuvre un mélange de soude, aluminate de sodium et silice. The synthesis of Mordenite is described by Meier et al (Kristallogr 115 (1961)). Kim et al (Zeolites 11 (1991) 745) which describe the synthesis of zeoiite Mordenite in the absence of a nitrogenous organic structurant, using a mixture of sodium hydroxide, sodium aluminate and silica.
Selon l'invention, la surface spécifique de la zéoiithe issue de l'étape i) est avantageusement supérieure à 250 m2/g, de préférence supérieure à 350 m2/g. De préférence, la zéoiithe issue de l'étape i) selon l'invention est entièrement microporeuse. De préférence, l'étape i) de synthèse de la zéoiithe est suivie d'au moins une étape de calcination et d'au moins une étape d'échange ionique réalisées avant l'étape ii) de mise en forme. According to the invention, the specific surface of the zeolite resulting from stage i) is advantageously greater than 250 m 2 / g, preferably greater than 350 m 2 / g. Preferably, the zeolite from step i) according to the invention is entirely microporous. Preferably, step i) of synthesis of the zeolite is followed by at least one calcination step and at least one ion exchange step carried out before the shaping step ii).
-Étape de calcination de la zéoiithe issue de l'étape i) Ladite étape de calcination sous flux d'air de la zéoiithe issue de ladite étape i) a pour but d'éliminer le structurant organique présent dans la microporosité de ladite zéoiithe, par exemple le cation R1R2 3 - N+ - (CH2)n - N+ - R4R5R6, de préférence le 1 ,6 Ν,Ν,Ν,Ν',Ν',Ν'-hexaméthylhexaméthylène diammonium lorsque la zéoiithe synthétisée au cours de ladite étape i) est la zéoiithe EU-1. Selon l'invention, l'étape de calcination la zéoiithe issue de ladite étape i) est avantageusement mise en ouvre à une température comprise entre 150 et 600°C , de préférence entre 200 et 600 °C , de manière plus préférée entre 250 et 550°C pendant une durée comprise entre 1 et 48 heures, de préférence pendant une durée comprise entre 1 et 30 heures. Calcination step of the zeolite resulting from step i) Said step of calcining under air flow of the zeolite resulting from said step i) is intended to eliminate the organic structuring agent present in the microporosity of said zeolite, by for example, the cation R 1 R 2 3 -N + - (CH 2 ) n - N + - R 4 R 5 R 6, preferably 1, 6 Ν, Ν, Ν, Ν ', Ν', Ν'-hexamethylhexamethylene diammonium when the zeolite synthesized during said step i) is zeolite EU-1. According to the invention, the zeolite calcination step resulting from said step i) is advantageously carried out at a temperature of between 150 and 600 ° C, preferably between 200 and 600 ° C, more preferably between 250 and 550 ° C for a period of between 1 and 48 hours, preferably for a period of between 1 and 30 hours.
-Étape d'échange ionique sur la zéoiithe issue de l'étape i) calcinée Ion exchange step on the zeoiite from step i) calcined
Selon l'invention, la zéoiithe peut en outre subir après la calcination de la zéoiithe issue de l'étape i) au moins une étape d'échange ionique. Le ou les échange(s) ionique(s) subséquent(s) à ladite calcination
sous flux d'air sec permet(tent) d'éliminer au moins en partie, de préférence pratiquement totalement, le cation alcalin, en particulier le sodium, éventuellement présent en position cationique dans la zéolithe sous sa forme brute de synthèse. Selon l'invention, chaque étape d'échange ionique est réalisée à une température préférentiellement comprise entre 20 et 150°C pendant une durée avantageusement comprise entre 2 heures et 10 heures. Ladite étape d'échange ionique est selon l'invention réalisée par au moins une solution NH4NO3 ou acétate d'ammonium. According to the invention, the zeolite can also undergo after calcination of the zeolite from step i) at least one ion exchange step. The ion exchange (s) subsequent to said calcination In dry air stream it is possible to remove at least partly, preferably almost completely, the alkaline cation, in particular sodium, optionally present in the cationic position in the zeolite in its crude synthetic form. According to the invention, each ion exchange step is carried out at a temperature preferably between 20 and 150 ° C for a duration advantageously between 2 hours and 10 hours. Said ion exchange step is according to the invention carried out by at least one NH 4 NO 3 solution or ammonium acetate solution.
Étape ii) de préparation d'un support zéolithique par la mise en forme de la zéolithe synthétisée avec au moins une matrice. Step ii) of preparing a zeolite support by shaping the zeolite synthesized with at least one matrix.
Le procédé de préparation du catalyseur selon l'invention se poursuit par la mise en oeuvre de l'étape ii) de mise en forme de la zéolithe avec au moins une matrice. Selon l'invention, l'étape ii) de mise en forme de la zéolithe est réalisée sur la zéolithe synthétisée selon l'étape i) ayant subi ou non une calcination et/ou un ou plusieurs échanges ioniques. Ces deux dernières opérations pouvant être réalisées après l'étape ii) de mise en forme de la zéolithe. The method for preparing the catalyst according to the invention is continued by carrying out the step ii) of shaping the zeolite with at least one matrix. According to the invention, the step ii) of shaping the zeolite is carried out on the zeolite synthesized according to step i) which has or has not undergone calcination and / or one or more ion exchanges. These last two operations can be performed after step ii) of shaping the zeolite.
La mise en oeuvre de ladite étape ii) de mise en forme de ladite zéolithe de type structural EUO et/ou MOR selon l'invention, est réalisée en utilisant une matrice choisie parmi les argiles, la magnésie, les alumines, les silices, l'oxyde de titane, l'oxyde de bore, la zircone, les phosphates d'aluminium, les phosphates de titane, les phosphates de zirconium, les silices-alumines et le charbon ou un mélange d'au moins deux de ces compositions. De préférence, la matrice est une alumine. La mise en forme conformément à ladite étape ii) consiste plus particulièrement à malaxer la zéolithe choisie parmi les types structuraux EUO et/ou MOR, dans un gel humide de matrice, préférentiellement d'alumine. Ledit gel humide de matrice est généralement obtenu par mélange d'au moins un acide et d'une poudre de matrice, pendant une durée nécessaire à l'obtention d'une bonne homogénéité de la pâte puis une mise en forme en objet utilisable dans un réacteur catalytique. The implementation of said step ii) of shaping of said zeolite of structural type EUO and / or MOR according to the invention is carried out using a matrix chosen from clays, magnesia, aluminas, silicas titanium oxide, boron oxide, zirconia, aluminum phosphates, titanium phosphates, zirconium phosphates, silica-aluminas and coal or a mixture of at least two of these compositions. Preferably, the matrix is an alumina. The shaping according to said step ii) consists more particularly in kneading the zeolite chosen from the structural types EUO and / or MOR, in a wet matrix gel, preferably alumina. Said wet matrix gel is generally obtained by mixing at least one acid and a matrix powder for a period of time necessary to obtain a good homogeneity of the dough and then forming an object that can be used in a catalytic reactor.
Une poudre de matrice est un composé majoritairement solide et de préférence un oxyde ou un hydrate. On utilisera de manière préférée un hydrate et de manière encore plus préférée un hydrate d'aluminium. La perte au feu de cet hydrate sera supérieure à 15%. Les poudres d'alumines choisies selon l'invention incluent les alumines commerciales, comme par exemple les grades TH, TM, pural ou Disperal de chez Sasol.
La mise en forme peut être réalisée en utilisant les techniques de mise en forme connues de l'homme du métier, telles que par exemple: extrusion, dragéification, séchage par atomisation ou encore pastillage. Par exemple, par passage de ladite pâte ainsi obtenue à travers une filière pour former des extrudés de diamètre avantageusement compris entre 0,4 et 4 mm. La mise en forme peut également être réalisée en présence des différents constituants du catalyseur et extrusion de la pâte minérale obtenue, par pastillage, mise en forme sous forme de billes au drageoir tournant ou au tambour, coagulation en goutte, oil-drop, oil-up, ou tout autre procédé connu d'agglomération d'une poudre contenant de l'alumine et éventuellement d'autres ingrédients choisis parmi ceux mentionnés ci- dessus. A matrix powder is a predominantly solid compound and preferably an oxide or hydrate. A hydrate and, more preferably, an aluminum hydrate are preferably used. The loss on ignition of this hydrate will be greater than 15%. The alumina powders chosen according to the invention include commercial aluminas, such as TH, TM, Pural or Disperal grades from Sasol. The shaping can be performed using shaping techniques known to those skilled in the art, such as for example: extrusion, coating, spray drying or pelletizing. For example, by passing said dough thus obtained through a die to form extrudates of diameter advantageously between 0.4 and 4 mm. The shaping can also be carried out in the presence of the various constituents of the catalyst and extrusion of the obtained mineral paste, by pelletizing, shaped into beads at the rotating bezel or drum, drop coagulation, oil-drop, oil- up, or any other known method of agglomeration of a powder containing alumina and optionally other ingredients selected from those mentioned above.
Les catalyseurs utilisés selon l'invention ont la forme de sphères ou d'extrudés. Il est toutefois avantageux que le catalyseur se présente sous forme d'extrudés d'une longueur comprise entre 4 et 9 mm et plus particulièrement entre 2 et 5 mm. Les formes sont cylindriques (qui peuvent être creuses ou non), cylindriques torsadées, multilobées (2, 3, 4 ou 5 lobes par exemple), anneaux. La forme cylindrique est utilisée de manière préférée, mais toute autre forme peut être utilisée. The catalysts used according to the invention are in the form of spheres or extrusions. However, it is advantageous that the catalyst is in the form of extrudates with a length of between 4 and 9 mm and more particularly between 2 and 5 mm. The shapes are cylindrical (which can be hollow or not), cylindrical twisted, multilobed (2, 3, 4 or 5 lobes for example), rings. The cylindrical shape is preferably used, but any other shape may be used.
Par ailleurs, ces supports mis en oeuvre selon la présente invention peuvent avoir été traités ainsi qu'il est bien connu de l'homme de l'art par des additifs pour faciliter la mise en forme et/ou améliorer les propriétés mécaniques finales des supports. A titre d'exemple d'additifs, on peut citer notamment la cellulose, la carboxyméthyl-cellulose, la carboxy-ethyl-cellulose, du tall-oil, les gommes xanthaniques, des agents tensio-actifs, des agents flocculants comme les polyacrylamides, le noir de carbone, les amidons, l'acide stéarique, l'alcool polyacrylique, l'alcool polyvinylique, des biopolymères, le glucose, les polyéthylènes glycols, etc. Furthermore, these supports used according to the present invention may have been treated as is well known to those skilled in the art by additives to facilitate the shaping and / or to improve the final mechanical properties of the supports. . By way of example of additives, there may be mentioned in particular cellulose, carboxymethylcellulose, carboxyethyl cellulose, tall oil, xanthan gums, surfactants, flocculating agents such as polyacrylamides, carbon black, starches, stearic acid, polyacrylic alcohol, polyvinyl alcohol, biopolymers, glucose, polyethylene glycols, etc.
L'extrusion peut être réalisée par n'importe quel outil conventionnel, disponible commercialement. La pâte issue du malaxage est extrudée à travers une filière, par exemple à l'aide d'un piston ou d'une mono-vis ou double vis d'extrusion. Cette étape d'extrusion peut être réalisée par toute méthode connue de l'homme du métier. Extrusion can be performed by any conventional tool, commercially available. The paste resulting from the mixing is extruded through a die, for example using a piston or a single screw or twin extrusion screw. This extrusion step can be performed by any method known to those skilled in the art.
Le réglage de la porosité caractéristique des supports zéolithiques selon l'invention, et en particulier la surface spécifique, est opéré partiellement lors de cette étape de mise en forme des particules de supports et tout type de matrice connue de l'homme convient à l'invention. Sans être exhaustif, les paramètres de mise en forme influents sont la teneur en eau, le taux d'acide, la durée de malaxage. On peut ajouter ou retirer de l'eau pour ajuster la viscosité de la pâte à extruder. Cette étape peut être réalisée à tout stade de l'étape de malaxage. The adjustment of the characteristic porosity of the zeolite supports according to the invention, and in particular the specific surface area, is partially carried out during this step of shaping the support particles and any type of matrix known to man is suitable for invention. Without being exhaustive, influential shaping parameters are the water content, the acid level, the mixing time. Water can be added or removed to adjust the viscosity of the extrusion paste. This step can be performed at any stage of the kneading step.
La teneur en acide ajouté au malaxage avant la mise en forme est inférieure à 30%, de préférence comprise entre 0,5 et 30%, de manière plus préférée comprise entre 0,5 et 20% poids de la masse
anhydre en zéoiithe et de matrice, de préférence l'alumine engagée dans la synthèse. L'acide nitrique est préféré. The acid content added to the kneading before shaping is less than 30%, preferably between 0.5 and 30%, more preferably between 0.5 and 20% by weight of the mass. anhydrous zeolite and matrix, preferably alumina engaged in the synthesis. Nitric acid is preferred.
De manière optionnelle, on peut également ajouter une base pour neutraliser la pâte lors de la mise en forme à l'issue du malaxage en présence d'acide, par exemple de l'ammoniaque, à une teneur comprise entre 1 et 50% de masse anhydre en zéoiithe et matrice, de préférence l'alumine engagée. Optionally, it is also possible to add a base to neutralize the paste during the shaping after mixing in the presence of acid, for example ammonia, at a content of between 1 and 50% by weight. anhydrous zeolite and matrix, preferably alumina engaged.
La durée de malaxage est avantageusement comprise entre 5 minutes et 120 minutes, de préférence entre 5 minutes et 90 minutes, de manière encore plus préférée entre 5 et 60 minutes. La zéoiithe peut être ajoutée à n'importe quel moment du malaxage. The mixing time is advantageously between 5 minutes and 120 minutes, preferably between 5 minutes and 90 minutes, even more preferably between 5 and 60 minutes. Zeolite can be added at any time during mixing.
Des traces d'impuretés peuvent être présentes dans la matrice utilisée selon l'invention comme par exemple Na, Fe, Si, soufre. Leur teneur est de préférence limitée. Selon l'invention, les traces de soufre sont inférieures à 0.2% poids, les traces de Na20 inférieures à 0.01 % poids, et les traces de Si02 et de Fe203 inférieures à 0.02% poids par rapport à la masse totale de la matrice. Traces of impurities may be present in the matrix used according to the invention, for example Na, Fe, Si or sulfur. Their content is preferably limited. According to the invention, the traces of sulfur are less than 0.2% by weight, the traces of Na 2 0 are less than 0.01% by weight, and the traces of Si0 2 and Fe 2 0 3 are less than 0.02% by weight relative to the mass. total of the matrix.
Avantageusement, la zéoiithe associée à la matrice, nommée également support zéolithique dans le cadre de la présente invention, est mise sous forme de billes, d'extrudés ou de trilobés, avantageusement sous forme d'extrudés ou de trilobés, de manière plus préférée sous forme de trilobés. Advantageously, the zeolite associated with the matrix, also called zeolite support in the context of the present invention, is in the form of beads, extrudates or trilobés, advantageously in the form of extrudates or trilobés, more preferably under trilobed form.
Dans une variante du procédé selon l'invention, un élément tel que l'étain, le cérium ou le phosphore peut être avantageusement introduit lors de l'étape ii) de mise en forme, par exemple par comalaxage Avantageusement, le catalyseur selon l'invention comprend 1 à 90 % poids de zéoiithe de type structural EUO et/ou MOR, de préférence 3 à 80 % et de manière encore plus préférée 4 à 60 % poids de zéoiithe de type structural EUO et/ou MOR, la matrice constituant le complément à 100%. In a variant of the process according to the invention, an element such as tin, cerium or phosphorus can be advantageously introduced during the shaping step ii), for example by comalaxing Advantageously, the catalyst according to the invention The invention comprises 1 to 90% by weight of zeolite of structural type EUO and / or MOR, preferably 3 to 80% and even more preferably 4 to 60% by weight of zeolite of structural type EUO and / or MOR, the matrix constituting the 100% complement.
La surface spécifique du support zéolithique du catalyseur dépend de la quantité de zéoiithe présente dans le support zéolithique. Elle est égale à la somme des surfaces spécifiques des 2 constituants matrice et zéolithique, pondérée de leur masse au sein du support zéolithique. Le choix de la matrice utilisée dans l'invention est tel que à l'issue de l'étape ii) de mise en forme, la surface spécifique de la matrice dans le support zéolithique est comprise entre 5 et 200 m2/g, de préférence entre 20 et 160 m2/g, de manière plus préférée entre 50 et 160 m2/g, de manière encore pus préférée entre 50 et 150 m2/g. La surface spécifique B.E.T de la matrice est obtenue par soustraction de la surface spécifique de la zéoiithe de type EUO et/ou MOR (comprise dans le support zéolithique et pondéré de la masse introduite) à la surface spécifique totale du support zéolithique du catalyseur.
La surface spécifique du support zéolithique est mesurée à i'issue de l'étape de séchage et de calcination du support zéolithique subséquentes à l'étape ii) de mise en forme. The specific surface of the zeolite support of the catalyst depends on the amount of zeolite present in the zeolite support. It is equal to the sum of the specific surfaces of the 2 constituents matrix and zeolite, weighted by their mass within the zeolitic support. The choice of the matrix used in the invention is such that, after the shaping step ii), the specific surface area of the matrix in the zeolite support is between 5 and 200 m 2 / g, preferably between 20 and 160 m 2 / g, more preferably between 50 and 160 m 2 / g, more preferably between 50 and 150 m 2 / g. The BET specific surface area of the matrix is obtained by subtracting the specific surface area of the EUO and / or MOR zeolite (included in the weighted zeolite support of the introduced mass) from the total specific surface area of the zeolitic support of the catalyst. The specific surface of the zeolite support is measured at the end of the zeolite support drying and calcination step subsequent to the shaping step ii).
-Séchage et calcination après étape ii) de mise en forme. Selon le procédé de l'invention, l'étape ii) de mise en forme est avantageusement suivie d'une étape de séchage puis d'une étape de calcination. Dans ce cas, l'étape de séchage est avantageusement réalisée à une température comprise entre 100 et 150°C pendant une durée comprise entre 5 et 20 heures en étuve et l'étape de calcination est avantageusement réalisée à une température comprise entre 250°C et 750°C pendant une durée comprise entre 1 et 8 heures. Il peut être avantageux de réaliser cette étape de calcination en présence de vapeur d'eau. Drying and calcination after step ii) shaping. According to the process of the invention, the shaping step ii) is advantageously followed by a drying step and then a calcination step. In this case, the drying step is advantageously carried out at a temperature of between 100 and 150 ° C. for a period of between 5 and 20 hours in an oven and the calcination step is advantageously carried out at a temperature of between 250 ° C. and 750 ° C for a period of between 1 and 8 hours. It may be advantageous to carry out this calcination step in the presence of water vapor.
Étape iii) de dépôt d'au moins un métal du groupe VIII sur le support zéolithique Step iii) depositing at least one Group VIII metal on the zeolite support
Selon l'invention, le procédé de préparation du catalyseur se poursuit par la mise en oeuvre de l'étape iii) qui consiste à introduire au moins un métal du groupe VIII de la classification périodique des éléments sur le support zéolithique préparé dans l'étape ii). According to the invention, the process for the preparation of the catalyst is continued by the implementation of step iii) which consists in introducing at least one metal of group VIII of the periodic table of elements onto the zeolitic support prepared in step ii).
Avantageusement, ledit métal du groupe VIII est choisi parmi le fer, le cobalt, le nickel, le ruthénium, le rhodium, le palladium, l'osmium, l'iridium et le platine, de préférence parmi les métaux nobles le platine, le palladium, le nickel, l'iridium et très préférentiellement parmi le palladium et le platine, pris seul ou en mélange. De manière encore plus préférée, ledit métal du groupe VIII est le platine. Advantageously, said group VIII metal is selected from iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium and platinum, preferably from noble metals platinum, palladium , nickel, iridium and very preferably among palladium and platinum, taken alone or as a mixture. Even more preferably, said group VIII metal is platinum.
Avantageusement le catalyseur selon l'invention comprend une teneur en métal(aux) du groupe VIII comprise entre 0,01 et 4 % en poids, de préférence de 0,05 à 2,0 % poids par rapport au poids total du catalyseur. Advantageously, the catalyst according to the invention comprises a content of Group VIII metal (s) of between 0.01 and 4% by weight, preferably 0.05 to 2.0% by weight relative to the total weight of the catalyst.
Conformément à l'étape iii), le dépôt du(s)dit(s) métal(aux) du groupe VIII sur le support zéolithique peut être effectué par la technique d'imprégnation à sec, la technique d'imprégnation par excès ou par échange ionique, de préférence, l'étape iii) est réalisée par la technique d'imprégnation à sec ou par échange ionique et de manière plus préférée par échange ionique. Lorsque plusieurs métaux sont introduits, ceux-ci peuvent être introduits soit tous de la même façon soit par des techniques différentes. According to step iii), the deposition of said Group VIII metal (s) on the zeolitic support can be carried out by the dry impregnation technique, the technique of impregnation by excess or by ion exchange, preferably, step iii) is carried out by the technique of dry impregnation or ion exchange and more preferably by ion exchange. When several metals are introduced, they can be introduced either all in the same way or by different techniques.
Tous les précurseurs de métaux du groupe VIII conviennent pour le dépôt d'un ou de plusieurs métal(ux) du groupe VIII sur le support zéolithique. En particulier, pour tout métal noble du groupe VIII, on peut utiliser des composés ammoniaqués ou des composés tels que par exemple le chloroplatinate d'ammonium, le dichlorure de platine dicarbonyle, l'acide hexahydroxyplatinique, le chlorure de
palladium ou le nitrate de palladium. Le platine est avantageusement introduit sous forme d'acide hexachloroplatinique. L'introduction du métal noble du groupe VIII est de préférence effectuée par imprégnation à l'aide d'une solution aqueuse ou organique de l'un des composés métalliques cités ci- dessus. Parmi les solvants organiques utilisables, on peut citer les hydrocarbures paraffiniques, naphténiques ou aromatiques contenant par exemple de 6 à 12 atomes de carbone par molécule, et les composés organiques halogénés contenant par exemple de 1 à 12 atomes de carbone par molécule. On peut citer par exemple le n-heptane, le méthylcyclohexane, le toluène et le chloroforme. On peut aussi utiliser les mélanges de solvants. Lors de l'étape iii) de dépôt du métal du groupe VIII sur le support zéolithique issu de l'étape ii) de mise en forme, le contrôle de certains paramètres mis en œuvre, en particulier la nature du précurseur du (des) métal(ux) du groupe VIII utilisé(s) et/ou la technique d'imprégnation, permet d'orienter le dépôt du(es)dit(s) métal(ux) majoritairement sur la matrice ou sur la zéolithe ou encore statistiquement sur l'ensemble zéolithe-matrice à savoir l'ensemble du support zéolithique. All group VIII metal precursors are suitable for the deposition of one or more Group VIII metals (ux) on the zeolitic support. In particular, for any noble metal of group VIII, it is possible to use ammonia compounds or compounds such as, for example, ammonium chloroplatinate, platinum dicarboxylic dichloride, hexahydroxyplatinic acid, palladium or palladium nitrate. Platinum is advantageously introduced in the form of hexachloroplatinic acid. The introduction of the Group VIII noble metal is preferably carried out by impregnation with an aqueous or organic solution of one of the metal compounds mentioned above. Among the organic solvents that can be used, mention may be made of paraffinic, naphthenic or aromatic hydrocarbons containing, for example, from 6 to 12 carbon atoms per molecule, and halogenated organic compounds containing, for example, from 1 to 12 carbon atoms per molecule. For example, n-heptane, methylcyclohexane, toluene and chloroform may be mentioned. Solvent mixtures can also be used. During step iii) of deposition of the Group VIII metal on the zeolite support resulting from the shaping step ii), the control of certain parameters implemented, in particular the nature of the precursor of the metal (s) (ux) of the group VIII used (s) and / or the impregnation technique, can guide the deposit of (es) said (s) metal (ux) mainly on the matrix or on the zeolite or statistically on the zeolite-matrix set namely the entire zeolitic support.
Ainsi, pour introduire le(s) métal(ux) du groupe VIII, préférentiellement le platine et/ou le palladium, majoritairement sur la matrice, on peut mettre en œuvre un échange anionique avec de l'acide hexachloroplatinique et/ou de l'acide hexachloropalladique, en présence d'un agent compétiteur, par exemple de l'acide chlorhydrique. Ce dépôt est de préférence suivi d'une calcination, par exemple à une température comprise entre 350 et 550°C et pendant une durée comprise entre 1 et 4 heures. Avec de tels précurseurs, le(s) métal(ux) du groupe VIII est(sont) déposé(s) majoritairement sur la matrice et le(s)dit(s) métal(ux) présente(nt) une bonne dispersion et une bonne répartition macroscopique à travers le grain de catalyseur. Thus, to introduce the group VIII metal (s), preferably platinum and / or palladium, predominantly on the matrix, it is possible to carry out anionic exchange with hexachloroplatinic acid and / or hexachloropalladic acid, in the presence of a competing agent, for example hydrochloric acid. This deposit is preferably followed by calcination, for example at a temperature between 350 and 550 ° C and for a period of between 1 and 4 hours. With such precursors, the group VIII metal (s) is (are) predominantly deposited on the matrix and the said metal (s) exhibit good dispersion and stability. good macroscopic distribution through the catalyst grain.
On peut aussi envisager de déposer le(s) métal(ux) du groupe VIII, préférentiellement le platine et/ou le palladium, par échange cationique de manière à ce que le(s)dit(s) métal(ux) soi(en)t déposé(s) majoritairement sur la zéolithe. Ainsi, dans le cas du platine, le précurseur peut être par exemple choisi parmi : It is also conceivable to deposit the group VIII metal (s), preferably platinum and / or palladium, by cation exchange so that said metal (s) is (in particular) ) t mainly deposited on the zeolite. Thus, in the case of platinum, the precursor may for example be chosen from:
- les composés ammoniaqués tels que les sels de platine (II) tétrammines de formule ammonia compounds such as tetrammine platinum (II) salts of formula
Pt(NH3) X2, les sels de platine (IV) hexammines de formule Pt(NH3)6X ; les sels de platine (IV) halogénopentammines de formule ( tX(NH3)s)X3 ; les sels de platine N- tétrahalogénodiammines de formule PtX4(NH3)2 ; et Pt (NH 3 ) X 2, hexammine platinum (IV) salts of formula Pt (NH 3) 6X; platinum (IV) halogenopentammine salts of formula (tX (NH 3) s) X 3 ; platinum N-tetrahalogenodiamine salts of formula PtX4 (NH3) 2; and
les composés halogénés de formule H(Pt(acac)2X) ; halogenated compounds of formula H (Pt (acac) 2X);
X étant un halogène choisi dans le groupe formé par le chlore, le fluor, le brome et l'iode, X étant de préférence le chlore, et "acac" représentant le groupe acétylacétonate (de formule brute C5H7O2), dérivé de l'acétylacétone. Avec de tels précurseurs, le(s) métal(ux) du groupe VIII est(sont) déposé(s)
majoritairement sur la zéolithe et le(s)dit(s) métal(ux) présente(nt) une bonne dispersion et une bonne répartition macroscopique à travers le grain de catalyseur. Selon l'invention, l'étape iii) de dépôt du métal du groupe VIII sur le support zéolithique est préférentiellement réalisée par la mise en oeuvre par échange ionique avec de l'acide hexachloroplatinique. X being a halogen selected from the group consisting of chlorine, fluorine, bromine and iodine, X being preferably chlorine, and "acac" representing the acetylacetonate group (of formula C5H7O2), derived from acetylacetone . With such precursors, the group VIII metal (s) is (are) deposited predominantly on the zeolite and the said metal (s) present (s) a good dispersion and a good macroscopic distribution through the catalyst grain. According to the invention, step iii) of depositing the Group VIII metal on the zeolitic support is preferably carried out by ion exchange with hexachloroplatinic acid.
Dans une autre variante du procédé selon l'invention, l'étape iii) comprend le dépôt en outre d'au moins un métal additionnel choisi parmi les métaux des groupes NIA, IVA et VIIB. Ledit métal choisi parmi les métaux des groupes IIIA, IVA et VIIB est avantageusement choisi parmi le gallium, l'indium, l'étain et le rhénium, de préférence parmi l'indium, l'étain et le rhénium. In another variant of the process according to the invention, step iii) comprises the further deposition of at least one additional metal selected from the metals of groups NIA, IVA and VIIB. Said metal chosen from the metals of groups IIIA, IVA and VIIB is advantageously chosen from gallium, indium, tin and rhenium, preferably from indium, tin and rhenium.
Dan un tel cas, le catalyseur selon l'invention comprend avantageusement le(s)dit(s) métal (aux) dans une teneur inférieure ou égale à 2 % en poids par rapport au poids total du catalyseur. De préférence, cette teneur est comprise entre 0,01 et 2 %, de préférence entre 0,05 et 1 ,0 % en poids par rapport au poids total du catalyseur. In such a case, the catalyst according to the invention advantageously comprises the said metal (s) in a content less than or equal to 2% by weight relative to the total weight of the catalyst. Preferably, this content is between 0.01 and 2%, preferably between 0.05 and 1.0% by weight relative to the total weight of the catalyst.
Dans le cas où le catalyseur utilisé dans le procédé d'isomérisation de l'invention contient également au moins un métal additionnel choisi parmi les métaux des groupes IIIA, IVA et VIIB, toutes les techniques de dépôt d'un tel métal connues de l'homme du métier et tous les précurseurs de tels métaux peuvent convenir. On peut ajouter le(s) métal(ux) du groupe VIII et celui(ceux) des groupes IIIA, IVA et VIIB, soit séparément soit simultanément dans au moins une étape unitaire. Lorsqu'au moins un métal des groupes IIIA, IVA et VIIB est ajouté séparément, il est préférable qu'il soit ajouté après le métal du groupe VIII. In the case where the catalyst used in the isomerization process of the invention also contains at least one additional metal selected from the metals of groups IIIA, IVA and VIIB, all the techniques of deposition of such a metal known from the skilled in the art and all the precursors of such metals may be suitable. Group VIII metal (s) and Group IIIA, IVA and VIIB metal (s) may be added either separately or simultaneously in at least one unit step. When at least one Group IIIA, IVA and VIIB metal is added separately, it is preferred that it be added after the Group VIII metal.
Le métal additionnel choisi parmi les métaux des groupes NIA, IVA et VIIB peut être introduit par l'intermédiaire de composés tels que par exemple les chlorures, les bromures et les nitrates des métaux des groupes IIIA, IVA et VIIB. Par exemple dans le cas de l'indium, on utilise avantageusement le nitrate ou le chlorure et dans le cas du rhénium, on utilise avantageusement l'acide perrhénique. Dans le cas de l'étain, les chlorures d'étain SnCI2 et SnCI4 sont préférés. Le métal additionnel choisi parmi les métaux des groupes IIIA, IVA et VIIB peut également être introduit sous la forme d'au moins un composé organique choisi dans le groupe constitué par les complexes dudit métal, en particulier les complexes polycétoniques du métal et les hydrocarbylmétaux tels que les alkyles, les cycloalkyles, les aryles, les alkylaryles et les arylalkyles métaux. Dans ce dernier cas, l'introduction du métal est avantageusement effectuée à l'aide d'une solution du composé organométallique dudit métal dans un solvant organique. On peut également employer des composés
organohalogénés du métal. Comme composés organiques de métaux, on peut citer en particulier le tétrabutylétain, dans le cas de l'étain, et le triphénylindium, dans le cas de l'indium. The additional metal selected from the metals of groups NIA, IVA and VIIB may be introduced via compounds such as, for example, the chlorides, bromides and nitrates of metals of groups IIIA, IVA and VIIB. For example, in the case of indium, nitrate or chloride is advantageously used, and in the case of rhenium, perrhenic acid is advantageously used. In the case of tin, tin chlorides SnCl 2 and SnCl 4 are preferred. The additional metal chosen from the metals of groups IIIA, IVA and VIIB may also be introduced in the form of at least one organic compound chosen from the group consisting of the complexes of said metal, in particular the metal polyketone complexes and the hydrocarbylmetals such as alkyls, cycloalkyls, aryls, alkylaryls and arylalkyls. In the latter case, the introduction of the metal is advantageously carried out using a solution of the organometallic compound of said metal in an organic solvent. Compounds can also be used organohalogenated metal. As organic compounds of metals, there may be mentioned in particular tetrabutyltin, in the case of tin, and triphenylindium, in the case of indium.
De plus, des traitements intermédiaires tels que par exemple une calcination et/ou une réduction peuvent être appliqués entre les dépôts successifs des différents métaux. In addition, intermediate treatments such as, for example, calcination and / or reduction may be applied between the successive deposits of the different metals.
La préparation du catalyseur selon l'invention se termine avantageusement par une calcination, préférentiellement à une température comprise entre 250°C et 600°C, pour une durée comprise entre 0,5 et 10 heures. De préférence la calcination est précédée d'un séchage, par exemple à l'étuve, à une température comprise entre 25°C et 250°C, de préférence entre 40°C et 200°C. Ladite étape de séchage est de préférence menée pendant la montée en température nécessaire pour effectuer ladite calcination. On peut mettre en œuvre une réduction préalable du catalyseur ex situ, sous courant d'hydrogène, par exemple à une température de 450°C à 600°C, pendant une durée de 0,5 à 4 heures. The preparation of the catalyst according to the invention is advantageously terminated by calcination, preferably at a temperature of between 250 ° C. and 600 ° C., for a duration of between 0.5 and 10 hours. The calcination is preferably preceded by drying, for example in an oven, at a temperature of between 25 ° C. and 250 ° C., preferably between 40 ° C. and 200 ° C. Said drying step is preferably conducted during the rise in temperature necessary to effect said calcination. It is possible to carry out a preliminary reduction of the ex situ catalyst, under a stream of hydrogen, for example at a temperature of 450 ° C. to 600 ° C., for a period of 0.5 to 4 hours.
Il peut être avantageux selon l'invention de recalciner le catalyseur après réduction, en présence d'air et éventuellement en présence de vapeur d'eau selon les enseignements des demandes de brevet FR0702941 et FR0702943. Le dépôt du(es)dit(s) métal(ux) du groupe VIII est avantageusement opéré de façon telle que la dispersion du(des)dit(s) métal(ux), déterminée par chimisorption, soit de 50 % à 100 %, de préférence de 60 % à 100 % et, de manière encore plus préférée, de 70 % à 100 %. Le dépôt du(es)dit(s) métal(ux) du groupe VIII est également avantageusement opéré de manière à obtenir une bonne répartition du(des)dit(s) métal(ux) dans le catalyseur mis en forme. Cette répartition est caractérisée par son profil obtenu par microsonde de Castaing. Le rapport des concentrations de chaque élément du groupe VIII au cœur du grain par rapport au bord de ce même grain, défini comme étant le coefficient de répartition, est avantageusement de 0,6:1 à 1 ,34:1 , de préférence de 0,7:1 à 1 ,3:1. It may be advantageous according to the invention to recalcine the catalyst after reduction, in the presence of air and optionally in the presence of water vapor according to the teachings of patent applications FR0702941 and FR0702943. The deposition of said Group VIII metal (s) is advantageously carried out in such a way that the dispersion of said metal (s), determined by chemisorption, is from 50% to 100% preferably from 60% to 100% and even more preferably from 70% to 100%. The deposition of said Group VIII metal (s) is also advantageously carried out so as to obtain a good distribution of said metal (s) in the shaped catalyst. This distribution is characterized by its profile obtained by microprobe of Castaing. The ratio of the concentrations of each element of group VIII to the heart of the grain with respect to the edge of this same grain, defined as the distribution coefficient, is advantageously from 0.6: 1 to 1, 34: 1, preferably from 0 to , 7: 1 to 1, 3: 1.
Dans le cas où le catalyseur ne contient pas de soufre, une réduction du métal sous hydrogène est avantageusement réalisée in situ avant injection de la charge. In the case where the catalyst does not contain sulfur, a reduction of the metal in hydrogen is advantageously carried out in situ before injection of the feedstock.
Dans le cas où le catalyseur utilisé dans l'invention contient du soufre, le soufre est introduit sur le catalyseur mis en forme, calciné, contenant le ou les métaux cités précédemment, soit in situ avant la réaction catalytique, soit ex situ. La sulfuration éventuelle intervient après la réduction. Dans le cas d'une sulfuration in situ, la réduction, si le catalyseur n'a pas été préalablement réduit, intervient avant la sulfuration. Dans le cas d'une sulfuration ex situ, on effectue la réduction puis la sulfuration. La
sulfuration s'effectue en présence d'hydrogène en utilisant tout agent sulfurant bien connu de l'homme de métier, tel que par exemple le sulfure de diméthyle ou le sulfure d'hydrogène. Par exemple, le catalyseur est traité avec une charge contenant du sulfure de diméthyle en présence d'hydrogène, avec une concentration telle que le rapport atomique soufre/métal soit de 1 ,5. Le catalyseur est ensuite maintenu pendant environ 3 heures à environ 400°C sous débit d'hydrogène avant l'injection de la charge. Dans le cas où le catalyseur utilisé dans l'invention contient du soufre, la teneur en soufre dans le catalyseur est telle que le rapport du nombre d'atomes de soufre sur le nombre d'atomes de métal du groupe VIII déposés aille jusqu'à 2:1 , avantageusement de 0,5:1 à 2:1. Utilisation du catalyseur selon l'invention In the case where the catalyst used in the invention contains sulfur, the sulfur is introduced on the shaped catalyst, calcined, containing the metal or metals mentioned above, either in situ before the catalytic reaction, or ex situ. Possible sulphurisation occurs after the reduction. In the case of in situ sulfurization, the reduction, if the catalyst has not been reduced beforehand, occurs before the sulfurization. In the case of an ex situ sulphurization, reduction is carried out and then sulphurization. The Sulfurization is carried out in the presence of hydrogen using any sulphurizing agent well known to those skilled in the art, such as, for example, dimethyl sulphide or hydrogen sulphide. For example, the catalyst is treated with a dimethyl sulfide-containing filler in the presence of hydrogen, with a concentration such that the sulfur / metal atomic ratio is 1.5. The catalyst is then maintained for about 3 hours at about 400 ° C under hydrogen flow prior to feed injection. In the case where the catalyst used in the invention contains sulfur, the sulfur content in the catalyst is such that the ratio of the number of sulfur atoms to the number of metal atoms of the group VIII deposited is up to 2: 1, preferably from 0.5: 1 to 2: 1. Use of the catalyst according to the invention
Le procédé d'isomérisation selon l'invention consiste à mettre en contact une coupe aromatique contenant au moins un composé aromatique ayant huit atomes de carbone par molécule avec au moins ledit catalyseur décrit plus haut dans la présente description. The isomerization process according to the invention comprises contacting an aromatic section containing at least one aromatic compound having eight carbon atoms per molecule with at least said catalyst described above in the present description.
Selon le procédé de l'invention, ladite coupe aromatique comprend en particulier soit uniquement un mélange de xylènes, soit uniquement de l'éthylbenzène, soit un mélange de xylène(s) et d'éthylbenzène. Ledit procédé d'isomérisation selon l'invention est mis en oeuvre généralement selon les conditions opératoires suivantes : According to the process of the invention, said aromatic cut comprises in particular either only a mixture of xylenes, or only ethylbenzene, or a mixture of xylene (s) and ethylbenzene. Said isomerization process according to the invention is generally carried out according to the following operating conditions:
- une température de 300°C à 500°C, de préférence de 320°C à 450°C et de manière encore plus préférée de 340°C à 430°C ; a temperature of 300 ° C to 500 ° C, preferably 320 ° C to 450 ° C and even more preferably 340 ° C to 430 ° C;
- une pression partielle d'hydrogène de 0,3 à 1 ,5 MPa, de préférence de 0,4 et 1 ,2 MPa et de manière encore préférée de 0,7 à 1,2 MPa ; a hydrogen partial pressure of 0.3 to 1.5 MPa, preferably 0.4 and 1.2 MPa and more preferably 0.7 to 1.2 MPa;
- une pression totale de 0,45 à 1 ,9 MPa, de préférence de 0,6 à 1 ,5 MPa ; et a total pressure of 0.45 to 1.9 MPa, preferably 0.6 to 1.5 MPa; and
- une vitesse spatiale d'alimentation, exprimée en kilogramme de charge introduite par kilogramme de catalyseur et par heure, de 0,25 à 30 h"1, de préférence de 1 à 10 h"1 et de manière encore préférée de 2 à 6 h"1. a feed space velocity, expressed in kilograms of feed introduced per kilogram of catalyst per hour, from 0.25 to 30 h -1 , preferably from 1 to 10 h -1 and more preferably from 2 to 6 h "1 .
Les exemples qui suivent illustrent l'invention sans pour autant en limiter la portée. The examples which follow illustrate the invention without limiting its scope.
Exemple 1 : Préparation d'une zéolithe EU-1 Example 1 Preparation of an EU-1 Zeolite
La matière première utilisée est une zéolithe EU-1 , brute de synthèse, comprenant le structurant organique à savoir le 1 ,6 Ν,Ν,Ν,Ν',Ν',Ν'-hexaméthylhexaméthylène diammonium et qui possède un rapport atomique Si/AI global égal à 15,3 et une teneur pondérale en sodium correspondant à un rapport atomique Na/AI (en %) égal à 30,8. Cette zéolithe a été synthétisée conformément à
l'enseignement du brevet EP-B1 -0.042.226. Pour la préparation d'une telle zéolithe, le mélange réactionnel présente la composition molaire suivante : 60 Si02 : 10,6 Na20 : 5,27 NaBr : 1 ,5 Al203 : 19,5 Hexa-Br2 : 2777 H20. Hexa-Br2 étant le 1 ,6 Ν,Ν,Ν,Ν',Ν',Ν'-hexaméthylhexaméthylène diammonium, le brome étant le contre-ion. Le mélange réactionnel est placé dans un autoclave sous agitation (300 tours/min) pendant 5 jours à 180°C. The raw material used is a synthetic crude zeolite EU-1, comprising the organic structuring agent namely 1, 6 Ν, Ν, Ν, Ν ', Ν', Ν'-hexamethylhexamethylene diammonium and which has an Si / Si atomic ratio. A global AI equal to 15.3 and a weight content of sodium corresponding to an atomic ratio Na / Al (in%) equal to 30.8. This zeolite was synthesized according to teaching of EP-B1 -0.042.226. For the preparation of such a zeolite, the reaction mixture has the following molar composition: 60 SiO 2 : 10.6 Na 2 O: 5.27 NaBr: 1.5 Al 2 O 3 : 19.5 Hexa-Br 2 : 2777 H 2 O. Hexa-Br 2 being 1, 6 Ν, Ν, Ν, Ν ', Ν', Ν'-hexamethylhexamethylene diammonium, bromine being the counter-ion. The reaction mixture is placed in an autoclave with stirring (300 rpm) for 5 days at 180 ° C.
Cette zéolithe EU-1 subit tout d'abord une calcination dite sèche à 550°C sous flux d'air sec durant 24 heures de manière à éliminer le structurant organique. Puis le solide obtenu est soumis à quatre échanges ioniques dans une solution de NH4NO3 10N, à environ 100°C pendant 4 heures pour chaque échange. Le solide ainsi obtenu est référencé EU-1(1 ) et possède un rapport atomique Si/AI global = 15,3 et un rapport atomique Na/AI=0,51 %. This EU-1 zeolite is first subjected to so-called dry calcination at 550 ° C. under a flow of dry air for 24 hours so as to eliminate the organic structurant. The solid obtained is then subjected to four ion exchanges in a solution of 10N NH 4 NO 3 at about 100 ° C. for 4 hours for each exchange. The solid thus obtained is referenced EU-1 (1) and has an overall Si / Al atomic ratio = 15.3 and an atomic ratio Na / Al = 0.51%.
La zéolithe EU-1 ainsi préparée présente une surface BET de 410 m2/g. The zeolite EU-1 thus prepared has a BET surface area of 410 m 2 / g.
Exemple 2 (non conforme) : Préparation du catalyseur A comprenant une zéolithe EU-1 La zéolithe EU-1 (1 ) obtenue à l'exemple 1 est ensuite mise en forme par extrusion avec un gel d'alumine commerciale (Pural SB3 de chez Sasol) de manière à obtenir, après séchage à une température égale à 100 °C pendant 1 nuit et une calcination sous air sec menée à une température égale à 450°C pendant 4 heures, le support S1 qui contient en poids 8 % de zéolithe EU-1 et 92 % d'alumine. Example 2 (non-compliant): Preparation of catalyst A comprising an EU-1 zeolite The EU-1 zeolite (1) obtained in Example 1 is then shaped by extrusion with a commercial alumina gel (Pural SB3 from Sasol) so as to obtain, after drying at a temperature of 100 ° C. for 1 night and calcination in dry air carried out at a temperature of 450 ° C. for 4 hours, the support S1 which contains, by weight, 8% of zeolite EU-1 and 92% alumina.
Le support S1 possède une surface spécifique de 266 m2/g. The support S1 has a specific surface area of 266 m 2 / g.
Les caractéristiques de porosité de la matrice sont: The porosity characteristics of the matrix are:
- Surface spécifique = 233 m2/g - Specific surface = 233 m 2 / g
- Volume poreux = 0,51 cm3/g - Pore volume = 0.51 cm 3 / g
- Diamètre moyen de mesopores = 8 nm - Average diameter of mesopores = 8 nm
Ce support S1 est soumis à un échange anionique avec de l'acide hexachloroplatinique en présence d'acide chlorhydrique en tant qu'agent compétiteur, de manière à déposer 0.3 % poids de platine par rapport au poids du catalyseur. Le solide humide est ensuite séché à 120°C pendant 12 heures et calciné sous un débit d'air sec à la température de 500°C pendant une heure. This support S1 is subjected to anion exchange with hexachloroplatinic acid in the presence of hydrochloric acid as a competing agent, so as to deposit 0.3% by weight of platinum based on the weight of the catalyst. The wet solid is then dried at 120 ° C for 12 hours and calcined under a dry air flow rate at 500 ° C for one hour.
Le catalyseur A ainsi obtenu contient, en poids, 8 % de zéolithe EU-1 , 91.7 % d'alumine et 0,3 % de platine. Catalyst A thus obtained contains, by weight, 8% of EU-1 zeolite, 91.7% of alumina and 0.3% of platinum.
Exemple 3 (conforme) : Préparation du catalyseur B comprenant une zéolithe EU-1 Example 3 (in conformity): Preparation of catalyst B comprising an EU-1 zeolite
La zéolithe EU-1 (1 ) obtenue à l'exemple 1 est ensuite mise en forme par extrusion avec un gel d'alumine commerciale (Pural TH100 de chez Sasol) de manière à obtenir, après séchage à une température égale à 100 °C pendant 1 nuit et une calcination sous air sec menée à une température
égale à 450°C pendant 4 heures, le support S2 qui contient en poids 8 % de zéolithe EU-1 et 92 % d'alumine. The EU-1 zeolite (1) obtained in Example 1 is then shaped by extrusion with a commercial alumina gel (Pural TH100 from Sasol) so as to obtain, after drying at a temperature equal to 100 ° C. for 1 night and calcination under dry air at a temperature equal to 450 ° C. for 4 hours, the support S 2 which contains, by weight, 8% of EU-1 zeolite and 92% of alumina.
Le support S2 possède une surface spécifique de 180 m2/g The support S2 has a specific surface of 180 m 2 / g
Les caractéristiques de porosité de la matrice sont: The porosity characteristics of the matrix are:
- Surface spécifique = 147 m2/g - Specific surface = 147 m 2 / g
- Volume poreux = 1 ,02 cm3/g - Pore volume = 1, 02 cm 3 / g
- Diamètre moyen des mésopores = 10 nm - Mean diameter of the mesopores = 10 nm
Ce support S2 est soumis à un échange anionique avec de l'acide hexachloroplatinique en présence ^ d'acide chlorhydrique en tant qu'agent compétiteur, de manière à déposer 0.3 % poids de platine par rapport au poids du catalyseur. Le solide humide est ensuite séché à 120°C pendant 12 heures et calciné sous un débit d'air sec à la température de 500°C pendant une heure. This support S2 is subjected to anion exchange with hexachloroplatinic acid in the presence of hydrochloric acid as a competing agent, so as to deposit 0.3% by weight of platinum based on the weight of the catalyst. The wet solid is then dried at 120 ° C for 12 hours and calcined under a dry air flow rate at 500 ° C for one hour.
Le catalyseur B ainsi obtenu contient, en poids, 8 % de zéolithe EU-1 , 91 ,7 % d'alumine et 0,3 % de platine. The catalyst B thus obtained contains, by weight, 8% of EU-1 zeolite, 91.7% of alumina and 0.3% of platinum.
Exemple 4 : Évaluation des propriétés catalytiques des catalyseurs A et B en isomérisation de l'éthylbenzène. La charge à isomériser, mise en contact respectivement avec le catalyseur A et le catalyseur B est constituée uniquement d'éthylbenzène. EXAMPLE 4 Evaluation of the Catalytic Properties of Catalysts A and B in Isomerization of Ethylbenzene The charge to be isomerized, placed in contact with catalyst A and catalyst B, respectively, consists solely of ethylbenzene.
Les conditions opératoires de l'isomérisation sont les suivantes : The operating conditions of the isomerization are as follows:
- température : 400°C ; temperature: 400 ° C .;
pression totale : 9 bar (1 bar = 0, 1 MPa) ; total pressure: 9 bar (1 bar = 0.1 MPa);
- pression partielle d'hydrogène : 7,5 bar. hydrogen partial pressure: 7.5 bar.
charge : ethylbenzène charge: ethylbenzene
vitesse spatiale d'alimentation, exprimée en kilogramme de charge introduite par kilogramme de catalyseur et par heure, égale à 8,7 h"1. . On évalue successivement les propriétés catalytiques des catalyseurs A et B pour l'isomérisation de l'éthylbenzène. Chacun des catalyseurs est réduit sous hydrogène pendant 4 heures à 480°C avant injection de la charge. feeding space velocity, expressed in kilograms of feed introduced per kilogram of catalyst per hour, equal to 8.7 h -1, The catalytic properties of catalysts A and B for the isomerization of ethylbenzene are successively evaluated. Each of the catalysts is reduced under hydrogen for 4 hours at 480 ° C. before injection of the charge.
Les catalyseurs ont été évalués en termes de conversion d'éthylbenzène et de sélectivité en xylènes. La sélectivité en xylènes est calculée au moyen du rendement en xylènes produits. Le rendement en xylènes est déterminé à partir du pourcentage massique des xylènes produits, obtenu par analyse de chaque effluent.
La conversion de l'éthylbenzène est le pourcentage d'éthylbenzène consommé. Tableau 1 :Conversion de l'éthylbenzène et sélectivité en xylènes sur les catalyseurs A, B The catalysts were evaluated in terms of ethylbenzene conversion and selectivity to xylenes. The selectivity to xylenes is calculated using the yield of xylenes produced. The yield of xylenes is determined from the mass percentage of the xylenes produced, obtained by analysis of each effluent. The conversion of ethylbenzene is the percentage of ethylbenzene consumed. Table 1: Conversion of ethylbenzene and selectivity to xylenes on catalysts A, B
Les résultats présentés dans le tableau 1 montrent que le catalyseur B conduit à de bien meilleures performances catalytiques en terme de conversion d'éthylbenzène que celle obtenue au moyen du catalyseur A. Par ailleurs, le catalyseur B selon l'invention conduit à une sélectivité en xylènes améliorée par rapport à celle obtenue avec le catalyseur A, en conséquence le catalyseur B selon l'invention conduit à un rendement en xylènes bien supérieur au rendement en xylènes obtenu avec le catalyseur comparatif A, le rendement en xylènes étant le produit de la conversion de l'éthylbenzène par la sélectivité en xylènes.
The results presented in Table 1 show that the catalyst B leads to a much better catalytic performance in terms of ethylbenzene conversion than that obtained using the catalyst A. Moreover, the catalyst B according to the invention leads to a selectivity in xylenes improved compared to that obtained with the catalyst A, consequently the catalyst B according to the invention leads to a yield of xylenes much higher than the yield of xylenes obtained with the comparative catalyst A, the yield of xylenes being the product of the conversion of ethylbenzene by selectivity to xylenes.
Claims
1. Procédé d'isomérisation d'une coupe aromatique contenant au moins un composé aromatique ayant huit atomes de carbone par molécule comprenant la mise en contact de ladite coupe avec au moins un catalyseur comprenant au moins un métal du groupe VIII de la classification périodique des éléments, au moins un support zéolithique comprenant une zéolithe choisie parmi les zéolithes de type structural EUO et MOR, prises seule ou en mélange et au moins une matrice, tel que la surface spécifique de la matrice dans le support zéolithique dudit catalyseur est comprise entre 5 et 200 m2/g. A process for isomerizing an aromatic section containing at least one aromatic compound having eight carbon atoms per molecule comprising contacting said section with at least one catalyst comprising at least one metal of group VIII of the periodic table. elements, at least one zeolite support comprising a zeolite chosen from zeolites of structure type EUO and MOR, taken alone or as a mixture and at least one matrix, such that the specific surface of the matrix in the zeolitic support of said catalyst is between and 200 m 2 / g.
2. Procédé selon la revendication 1 dans lequel la surface spécifique de la matrice dans le support zéolithique dudit catalyseur est comprise entre 20 et 160 m2/g. 2. The method of claim 1 wherein the specific surface of the matrix in the zeolitic support of said catalyst is between 20 and 160 m 2 / g.
3. Procédé selon la revendication 1 ou 2 dans lequel la surface spécifique de la matrice dans le support zéolithique dudit catalyseur est comprise entre 50 et 160 m2/g. 3. The method of claim 1 or 2 wherein the specific surface of the matrix in the zeolitic support of said catalyst is between 50 and 160 m 2 / g.
4. Procédé selon l'une des revendications précédentes dans lequel ledit catalyseur comprend 1 à 90 % poids de zéolithe de type structural EUO et/ou MOR par rapport au poids total du catalyseur. 4. Method according to one of the preceding claims wherein said catalyst comprises 1 to 90% by weight of zeolite structural type EUO and / or MOR with respect to the total weight of the catalyst.
5. Procédé selon l'une des revendications précédentes dans lequel la zéolithe de type structural EUO est choisie parmi les zéolithes EU-1 , TPZ-3, ZSM-50 ou leur mélange. 5. Method according to one of the preceding claims wherein the zeolite of structural type EUO is selected from zeolites EU-1, TPZ-3, ZSM-50 or their mixture.
6. Procédé selon la revendication 5 dans lequel la zéolithe de type structural EUO est la zéolithe EU-1. 6. Process according to claim 5, in which the zeolite of structure type EUO is zeolite EU-1.
7. Procédé selon l'une des revendications précédentes dans lequel la zéolithe de type structural MOR est la Mordénite. 7. Process according to one of the preceding claims, in which the zeolite of structural type MOR is Mordenite.
8. Procédé selon l'une des revendications précédentes dans lequel la zéolithe utilisée dans le support zéolithique du catalyseur est un mélange de la zéolithe EU-1 et de la Mordénite 8. Process according to one of the preceding claims, in which the zeolite used in the zeolitic support of the catalyst is a mixture of zeolite EU-1 and Mordenite.
9. Procédé selon l'une des revendications précédentes dans lequel ledit catalyseur comprend une teneur en métal(aux) du groupe VIII comprise entre 0,01 et 4 % en poids par rapport au poids total du catalyseur. 9. Method according to one of the preceding claims wherein said catalyst comprises a metal content (aux) Group VIII between 0.01 and 4% by weight relative to the total weight of the catalyst.
10. Procédé selon l'une des revendications précédentes dans lequel ladite matrice est choisie parmi les argiles, la magnésie, les alumines, les silices, l'oxyde de titane, l'oxyde de bore, la zircone, les phosphates d'aluminium, les phosphates de titane, les phosphates de zirconium, les silices-alumines et le charbon ou un mélange d'au moins deux de ces compositions. 10. Method according to one of the preceding claims wherein said matrix is selected from clays, magnesia, aluminas, silicas, titanium oxide, boron oxide, zirconia, aluminum phosphates, titanium phosphates, zirconium phosphates, silica-aluminas and charcoal or a mixture of at least two of these compositions.
11. Procédé selon la revendication 10 tel que la matrice est une alumine. 11. The method of claim 10 wherein the matrix is an alumina.
12. Procédé selon l'une des revendications précédentes dans lequel ledit catalyseur comprend en outre au moins un métal choisi parmi les métaux des groupes IIIA, IVA et VIIB, le(s)dit(s) métal (aux) dans une teneur inférieure ou égale à 2 % en poids par rapport au poids total du catalyseur. 12. Method according to one of the preceding claims wherein said catalyst further comprises at least one metal selected from the metals of groups IIIA, IVA and VIIB, said (s) metal (s) in a lower content or equal to 2% by weight relative to the total weight of the catalyst.
13. Procédé de préparation du catalyseur selon les revendications 1 à 12, comprenant au moins les étapes suivantes : Process for the preparation of the catalyst according to claims 1 to 12, comprising at least the following steps:
i) la synthèse d'au moins une zéolithe de type structural EUO et/ou O , i) the synthesis of at least one zeolite of structure type EUO and / or O,
ii) la préparation d'un support zéolithique par la mise en forme de ladite zéolithe avec au moins une matrice ii) preparing a zeolitic support by shaping said zeolite with at least one matrix
iii) le dépôt d'au moins un métal du groupe VIII de la classification périodique des éléments sur le support zéolithique issu de l'étape ii) de mise en forme iii) the deposition of at least one metal of group VIII of the periodic table of elements on the zeolitic support resulting from stage ii) of shaping
14. Procédé selon la revendication 13 dans lequel l'étape i) de synthèse de la zéolithe est suivie d'au moins une étape de calcination et d'au moins une étape d'échange ionique réalisées avant l'étape ii) de mise en forme. 14. The method of claim 13 wherein the step i) of synthesis of the zeolite is followed by at least one calcination step and at least one ion exchange step carried out before the step ii) of implementation. form.
15. Procédé sélon la revendication 13 ou 14 dans lequel l'étape ii) de mise en forme est suivie d'une étape de séchage réalisée à une température comprise entre 100 et 150°C pendant une durée comprise entre 5 et 20 heures en étuve puis d'une étape de calcination réalisée à une température comprise entre 250°C et 750°C pendant une durée comprise entre 1 et 8 heures. 15. The method of claim 13 or 14 wherein the shaping step ii) is followed by a drying step carried out at a temperature between 100 and 150 ° C for a period of between 5 and 20 hours in an oven then a calcination step carried out at a temperature between 250 ° C and 750 ° C for a period of between 1 and 8 hours.
16. Procédé selon l'une des revendications précédentes dans lequel le procédé d'isomérisation est mis en oeuvre à une température de 300°C à 500°C, une pression partielle d'hydrogène de 0,3 à 1 ,5 MPa, une pression totale de 0,45 à 1 ,9 MPa et une vitesse spatiale d'alimentation, exprimée en kilogramme de charge introduite par kilogramme de catalyseur et par heure de 0,25 à 30 h"1. 16. The process as claimed in one of the preceding claims, in which the isomerization process is carried out at a temperature of 300 ° C. to 500 ° C., a hydrogen partial pressure of 0.3 to 1.5 MPa, total pressure of 0.45 to 1, 9 MPa and a feed space velocity, expressed in kilogram of feed introduced per kilogram of catalyst and per hour of 0.25 to 30 h -1 .
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FR1103995A FR2984308B1 (en) | 2011-12-20 | 2011-12-20 | PROCESS FOR ISOMERIZING AN AROMATIC C8 CUT IN THE PRESENCE OF A CATALYST BASED ON A EUO ZEOLITE AND A PARTICULAR BINDER |
PCT/FR2012/000474 WO2013093222A1 (en) | 2011-12-20 | 2012-11-20 | Method for isomerizing an aromatic c8 fraction in the presence of a catalyst containing an euo zeolite and a specific binder |
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US4762957A (en) * | 1987-06-10 | 1988-08-09 | Uop Inc. | Process for isomerization of alkylaromatics |
US6057486A (en) * | 1997-12-22 | 2000-05-02 | Institut Francais Du Petrole | Catalyst containing a zeolite EUO and the use of the catalyst in a process for isomerizing aromatic compounds containing 8 carbon atoms per molecule |
FR2777275B1 (en) * | 1998-04-08 | 2000-05-19 | Inst Francais Du Petrole | PROCESS FOR ISOMERIZATION OF AROMATIC COMPOUNDS WITH EIGHT CARBON ATOMS USING A CATALYST CONTAINING A EUO STRUCTURAL TYPE ZEOLITE |
US6143941A (en) * | 1999-03-03 | 2000-11-07 | Uop Llc | Selective xylenes isomerization and ethylbenzene conversion |
KR100991482B1 (en) * | 2003-12-30 | 2010-11-04 | 유오피 엘엘씨 | Process and catalyst for c8 alkylaromatic isomerization |
FR2895282B1 (en) | 2005-12-22 | 2008-02-01 | Inst Francais Du Petrole | BIZEOLITHIC CATALYST COMPRISING A GROUP VIII METAL AND A GROUP IIIA METAL AND ITS USE IN ISOMERIZATION OF C8 AROMATIC COMPOUNDS |
FR2915112B1 (en) | 2007-04-23 | 2009-11-20 | Inst Francais Du Petrole | METHOD FOR ISOMERIZING AN AROMATIC C8 CUT IN THE PRESENCE OF A CATALYST BASED ON A DEALUMINATED EUO ZEOLITE. |
US7939701B2 (en) * | 2007-12-12 | 2011-05-10 | Uop Llc | Aromatic isomerization catalyst and a process of use thereof |
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