WO2014001412A2 - Katalysatorbeschichtung und verfahren für die umwandlung von oxygenaten zu olefinen - Google Patents
Katalysatorbeschichtung und verfahren für die umwandlung von oxygenaten zu olefinen Download PDFInfo
- Publication number
- WO2014001412A2 WO2014001412A2 PCT/EP2013/063436 EP2013063436W WO2014001412A2 WO 2014001412 A2 WO2014001412 A2 WO 2014001412A2 EP 2013063436 W EP2013063436 W EP 2013063436W WO 2014001412 A2 WO2014001412 A2 WO 2014001412A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- catalyst
- zeolites
- range
- present
- oxygenates
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 190
- 239000003054 catalyst Substances 0.000 title claims abstract description 184
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 92
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 79
- 239000011248 coating agent Substances 0.000 title claims description 23
- 238000000576 coating method Methods 0.000 title claims description 23
- 239000010457 zeolite Substances 0.000 claims abstract description 126
- 239000000758 substrate Substances 0.000 claims abstract description 104
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims abstract description 36
- 150000001342 alkaline earth metals Chemical class 0.000 claims abstract description 36
- 238000004519 manufacturing process Methods 0.000 claims abstract description 16
- 239000000203 mixture Substances 0.000 claims description 140
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 100
- 239000011230 binding agent Substances 0.000 claims description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- 229910001868 water Inorganic materials 0.000 claims description 33
- 238000002360 preparation method Methods 0.000 claims description 30
- 238000001035 drying Methods 0.000 claims description 28
- 238000001354 calcination Methods 0.000 claims description 27
- 150000001298 alcohols Chemical class 0.000 claims description 26
- 241000264877 Hippospongia communis Species 0.000 claims description 25
- 238000005470 impregnation Methods 0.000 claims description 21
- 238000011068 loading method Methods 0.000 claims description 21
- 239000002245 particle Substances 0.000 claims description 21
- 239000007787 solid Substances 0.000 claims description 21
- 239000002904 solvent Substances 0.000 claims description 18
- -1 aliphatic alcohols Chemical class 0.000 claims description 11
- 238000010924 continuous production Methods 0.000 claims description 9
- 239000000919 ceramic Substances 0.000 claims description 8
- 239000006260 foam Substances 0.000 claims description 8
- 238000000265 homogenisation Methods 0.000 claims description 7
- 229930195733 hydrocarbon Natural products 0.000 claims description 7
- 150000002430 hydrocarbons Chemical class 0.000 claims description 7
- 239000008188 pellet Substances 0.000 claims description 7
- 150000002170 ethers Chemical class 0.000 claims description 6
- 238000003756 stirring Methods 0.000 claims description 6
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 claims description 6
- 239000008187 granular material Substances 0.000 claims description 5
- 239000007921 spray Substances 0.000 claims description 5
- 229910052751 metal Inorganic materials 0.000 claims description 4
- 239000002184 metal Substances 0.000 claims description 4
- 239000007769 metal material Substances 0.000 claims description 4
- 239000004215 Carbon black (E152) Substances 0.000 claims description 3
- 150000001728 carbonyl compounds Chemical class 0.000 claims description 3
- 238000004898 kneading Methods 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 3
- 230000029936 alkylation Effects 0.000 claims description 2
- 238000005804 alkylation reaction Methods 0.000 claims description 2
- 238000004231 fluid catalytic cracking Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 45
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 31
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 30
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 27
- 229910021536 Zeolite Inorganic materials 0.000 description 25
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 17
- 239000000725 suspension Substances 0.000 description 15
- 239000011777 magnesium Substances 0.000 description 14
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 13
- 230000000052 comparative effect Effects 0.000 description 13
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 13
- 239000000126 substance Substances 0.000 description 13
- 230000003197 catalytic effect Effects 0.000 description 12
- 239000000463 material Substances 0.000 description 12
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 12
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 10
- 229910052749 magnesium Inorganic materials 0.000 description 10
- 229910052878 cordierite Inorganic materials 0.000 description 9
- JSKIRARMQDRGJZ-UHFFFAOYSA-N dimagnesium dioxido-bis[(1-oxido-3-oxo-2,4,6,8,9-pentaoxa-1,3-disila-5,7-dialuminabicyclo[3.3.1]nonan-7-yl)oxy]silane Chemical compound [Mg++].[Mg++].[O-][Si]([O-])(O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2)O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2 JSKIRARMQDRGJZ-UHFFFAOYSA-N 0.000 description 9
- 239000000843 powder Substances 0.000 description 9
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 8
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 8
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 8
- 238000006555 catalytic reaction Methods 0.000 description 8
- YIXJRHPUWRPCBB-UHFFFAOYSA-N magnesium nitrate Chemical compound [Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O YIXJRHPUWRPCBB-UHFFFAOYSA-N 0.000 description 8
- 239000000047 product Substances 0.000 description 8
- 229910052681 coesite Inorganic materials 0.000 description 7
- 229910052906 cristobalite Inorganic materials 0.000 description 7
- 229910052682 stishovite Inorganic materials 0.000 description 7
- 229910052905 tridymite Inorganic materials 0.000 description 7
- 238000003618 dip coating Methods 0.000 description 6
- 229910010271 silicon carbide Inorganic materials 0.000 description 6
- 239000000243 solution Substances 0.000 description 6
- XOBKSJJDNFUZPF-UHFFFAOYSA-N Methoxyethane Chemical compound CCOC XOBKSJJDNFUZPF-UHFFFAOYSA-N 0.000 description 5
- 229910052791 calcium Inorganic materials 0.000 description 5
- 239000011575 calcium Substances 0.000 description 5
- 150000001875 compounds Chemical class 0.000 description 5
- 239000012153 distilled water Substances 0.000 description 5
- 239000002243 precursor Substances 0.000 description 5
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 description 5
- 229910052712 strontium Inorganic materials 0.000 description 5
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 4
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical compound CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 4
- 238000004939 coking Methods 0.000 description 4
- 230000009849 deactivation Effects 0.000 description 4
- 239000000395 magnesium oxide Substances 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- 150000005215 alkyl ethers Chemical class 0.000 description 3
- 239000002734 clay mineral Substances 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- CIOAGBVUUVVLOB-UHFFFAOYSA-N strontium atom Chemical compound [Sr] CIOAGBVUUVVLOB-UHFFFAOYSA-N 0.000 description 3
- 238000002604 ultrasonography Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- ZAFNJMIOTHYJRJ-UHFFFAOYSA-N Diisopropyl ether Chemical compound CC(C)OC(C)C ZAFNJMIOTHYJRJ-UHFFFAOYSA-N 0.000 description 2
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 2
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- 150000001299 aldehydes Chemical class 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910000323 aluminium silicate Inorganic materials 0.000 description 2
- VXAUWWUXCIMFIM-UHFFFAOYSA-M aluminum;oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Al+3] VXAUWWUXCIMFIM-UHFFFAOYSA-M 0.000 description 2
- 239000007900 aqueous suspension Substances 0.000 description 2
- 229910052788 barium Inorganic materials 0.000 description 2
- 238000005815 base catalysis Methods 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 229910010293 ceramic material Inorganic materials 0.000 description 2
- 239000003426 co-catalyst Substances 0.000 description 2
- 239000000306 component Substances 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 229910052593 corundum Inorganic materials 0.000 description 2
- 150000001983 dialkylethers Chemical class 0.000 description 2
- KZHJGOXRZJKJNY-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Si]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O KZHJGOXRZJKJNY-UHFFFAOYSA-N 0.000 description 2
- 238000007598 dipping method Methods 0.000 description 2
- POLCUAVZOMRGSN-UHFFFAOYSA-N dipropyl ether Chemical compound CCCOCCC POLCUAVZOMRGSN-UHFFFAOYSA-N 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 238000000227 grinding Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000007654 immersion Methods 0.000 description 2
- 229910010272 inorganic material Inorganic materials 0.000 description 2
- 239000011147 inorganic material Substances 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 2
- 238000003801 milling Methods 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 229910052863 mullite Inorganic materials 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000011574 phosphorus Substances 0.000 description 2
- 150000004760 silicates Chemical class 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 229910052566 spinel group Inorganic materials 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 229910001845 yogo sapphire Inorganic materials 0.000 description 2
- 229910052845 zircon Inorganic materials 0.000 description 2
- GFQYVLUOOAAOGM-UHFFFAOYSA-N zirconium(iv) silicate Chemical compound [Zr+4].[O-][Si]([O-])([O-])[O-] GFQYVLUOOAAOGM-UHFFFAOYSA-N 0.000 description 2
- 125000006526 (C1-C2) alkyl group Chemical group 0.000 description 1
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- ZZBAGJPKGRJIJH-UHFFFAOYSA-N 7h-purine-2-carbaldehyde Chemical compound O=CC1=NC=C2NC=NC2=N1 ZZBAGJPKGRJIJH-UHFFFAOYSA-N 0.000 description 1
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- 239000005995 Aluminium silicate Substances 0.000 description 1
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 1
- 229910014585 C2-Ce Inorganic materials 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 229930194542 Keto Natural products 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- SMZOGRDCAXLAAR-UHFFFAOYSA-N aluminium isopropoxide Chemical compound [Al+3].CC(C)[O-].CC(C)[O-].CC(C)[O-] SMZOGRDCAXLAAR-UHFFFAOYSA-N 0.000 description 1
- 235000012211 aluminium silicate Nutrition 0.000 description 1
- HPTYUNKZVDYXLP-UHFFFAOYSA-N aluminum;trihydroxy(trihydroxysilyloxy)silane;hydrate Chemical compound O.[Al].[Al].O[Si](O)(O)O[Si](O)(O)O HPTYUNKZVDYXLP-UHFFFAOYSA-N 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- 229910001680 bayerite Inorganic materials 0.000 description 1
- 229910000278 bentonite Inorganic materials 0.000 description 1
- 239000000440 bentonite Substances 0.000 description 1
- SVPXDRXYRYOSEX-UHFFFAOYSA-N bentoquatam Chemical compound O.O=[Si]=O.O=[Al]O[Al]=O SVPXDRXYRYOSEX-UHFFFAOYSA-N 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 229910001593 boehmite Inorganic materials 0.000 description 1
- 229910052796 boron Inorganic materials 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- GUJOJGAPFQRJSV-UHFFFAOYSA-N dialuminum;dioxosilane;oxygen(2-);hydrate Chemical compound O.[O-2].[O-2].[O-2].[Al+3].[Al+3].O=[Si]=O.O=[Si]=O.O=[Si]=O.O=[Si]=O GUJOJGAPFQRJSV-UHFFFAOYSA-N 0.000 description 1
- 229910001649 dickite Inorganic materials 0.000 description 1
- 238000000921 elemental analysis Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 229910001679 gibbsite Inorganic materials 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000003365 glass fiber Substances 0.000 description 1
- 229910052621 halloysite Inorganic materials 0.000 description 1
- 239000008240 homogeneous mixture Substances 0.000 description 1
- FAHBNUUHRFUEAI-UHFFFAOYSA-M hydroxidooxidoaluminium Chemical compound O[Al]=O FAHBNUUHRFUEAI-UHFFFAOYSA-M 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 1
- 125000000468 ketone group Chemical group 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 229910052901 montmorillonite Inorganic materials 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910052756 noble gas Inorganic materials 0.000 description 1
- 150000002835 noble gases Chemical class 0.000 description 1
- 229910052755 nonmetal Inorganic materials 0.000 description 1
- 150000002843 nonmetals Chemical class 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000006104 solid solution Substances 0.000 description 1
- 239000011877 solvent mixture Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 1
- 239000003981 vehicle Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/7038—MWW-type, e.g. MCM-22, ERB-1, ITQ-1, PSH-3 or SSZ-25
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/80—Mixtures of different zeolites
-
- 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
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/19—Catalysts containing parts with different compositions
-
- 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
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/024—Multiple impregnation or coating
- B01J37/0246—Coatings comprising a zeolite
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/024—Multiple impregnation or coating
- B01J37/0248—Coatings comprising impregnated particles
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Definitions
- the present invention relates to a catalyst in the form of a coated carrier substrate for the conversion of oxygenates to olefins and a process for its preparation. Furthermore, the present invention relates to a process for the conversion of oxygenates to olefins, in particular using the coated carrier substrate according to the invention as catalyst and the use of a catalyst according to the present invention in specific catalytic processes.
- No. 4,692,423 relates to a process for the preparation of a supported zeolite-containing catalyst by applying a mixture of a zeolite in a polymerizable solvent such as tetrahydrofuran to a porous carrier substrate, the latter being made of organic or inorganic material.
- a polymerizable solvent such as tetrahydrofuran
- WO 98/29519 A1 describes non-zeolitic molecular sieves supported on inorganic materials and in particular SAPO and their use in methanol-to-olefin processes.
- WO 94/25151 A1 describes zeolites carried on monoliths and in particular ZSM-5 and their use as molecular sieves in separation processes.
- Hammon et al. in Applied Catalysis 1988, 37, pages 155-174 relates to processes for the preparation of Zeolithextrulves with little to no binder and their use in methanol-to-olefin process.
- the use of monoliths shaped extrudates described as catalysts because of rapid coking and thus associated short downtime as particularly disadvantageous.
- DD 238733 A1 relates to a zeolite doped with magnesium and its use in the conversion of methanol to lower olefins, especially of the C number range> 3.
- Mclntosh et al. in Applied Catalysis 1983, 6, p 307-314 specifically describes ZSM-5 catalysts and their use in methanol-to-olefin processes, as well as their doping with various metals and non-metals, such as magnesium or phosphorus, and their Influence on yields and product distribution in the catalytic conversion of methanol. No.
- 4,049,573 relates to a catalytic process for the conversion of lower alcohols and their ethers and, in particular, methanol and dimethyl ether selectively into a hydrocarbon mixture with a high proportion of C 2 -C 3 -olefins and mononuclear aromatics and, in particular, Para-xylene, wherein the catalysts used therein are doped with boron, magnesium and / or phosphorus.
- Ciambelli et al. "Acid-base catalysis in the conversion of methanol to olefins over Mg-modified ZSM-5 zeolite", Successful Design of Catalysts, Elsevier Science Publishers BV, Amsterdam, 1988, pp. 239-246 examines the influence of magnesium in the MTO process and in particular in cooperation with ZSM-5 zeolite as catalyst.
- the object of the present invention was to provide an improved catalyst, in particular for the conversion of oxygenates to olefins, which enables a longer service life of the catalyst at comparable space velocity and conversion to oxygenates.
- the object of the present invention in particular, was to bring about improvements in the coking of the catalyst, which, for example, in methanol-to-olefin process, the service life of a catalyst, to which the regeneration of the catalyst is required, to the desired selectivity and / or to achieve a sufficient space-time yield.
- a catalyst for the conversion of oxygenates to olefins which comprises a carrier substrate and a layer applied to the substrate, wherein the catalytically active layer comprises one or more zeolites of the MFI, MEL and / or MWW structure type, each containing one or more alkaline earth metals, includes, not only possesses a considerably improved tool life, but also a surprisingly high selectivity of C3 and C4 olefins having.
- the particular combination of doping one or more MFI, MEL and / or MWW structural type zeolites with one or more alkaline earth metals in conjunction with one embodiment of the catalyst as coated with the one or more zeolites Carrier substrate has both an unexpected improvement in the resistance of the catalyst to deactivation during its use in a catalytic process as well as a surprisingly high olefin selectivity when using the catalyst for the conversion of oxygenates result.
- the present invention relates to a catalyst for the conversion of oxygenates to olefins comprising a carrier substrate and
- the layer containing one or more MFI, MEL and / or MWW-type zeolites and wherein the one or more zeolites contain one or more alkaline-earth metals.
- the carrier substrate used in the catalyst according to the invention there is in principle no restriction as to its shape.
- any conceivable possible form for the carrier substrate can be chosen, provided that it is suitable for being at least partially coated with a layer of the one or more MFI, MEL and / or MWW structure type zeolites.
- the shape of the supporting substrate is selected from the group consisting of granules, pellets, nets, rings, spheres, cylinders, hollow cylinders, monoliths and mixtures and / or combinations of two or more thereof.
- these preferably relate to those forms of the carrier substrate which are commonly used for the production of beds, in particular the preferred forms of the carrier substrate selected from the group of granules, pellets, nets, rings, balls, cylinders and hollow cylinders ,
- the beds preferably carrier substrates selected from the group consisting of granules, pellets, nets, rings, spheres, cylinders, hollow cylinders and mixtures of contain two or more of them.
- such combinations of beds and monoliths relate to preferred forms of the catalyst which include a series of one or more monoliths and one or more beds in which the bed (s) and monolith (s) form individual zones of the catalyst.
- embodiments of the catalyst according to the invention are preferred, which contain combinations of monoliths as a form of the carrier substrate, in particular combinations of monoliths according to the particular ren or preferred embodiments as described in the present application.
- the carrier substrate consists of one or more monoliths, wherein when using a plurality of monoliths preferably a sequence and / or a juxtaposition of single or more monoliths at least in pairs adjacent monoliths is contained in the catalyst.
- embodiments of the catalyst for the conversion of oxygenates to olefins are preferred in which the shape of the carrier substrate is selected from the group consisting of granules, pellets, nets, rings, spheres, cylinders, hollow cylinders, monoliths and mixtures and / or combinations of two or more thereof, wherein the carrier substrate is preferably one or more monoliths.
- the one or more monoliths which are preferably present as carrier substrate in the catalyst according to the invention, in principle there is no restriction as to the shape which the one or more monoliths can assume.
- monoliths are preferred which are selected from the group consisting of honeycombs, braids, foams, and combinations of two or more thereof, more preferably, the one or more monoliths containing one or more honeycombs and / or braids.
- the one or more monoliths which are preferably used as the carrier substrate have honeycomb shape.
- embodiments of the catalyst for the conversion of oxygenates to olefins in which the one or more monoliths are selected as the preferred carrier substrate are selected from the group consisting of honeycombs, braids, foams, and combinations of two or more thereof wherein the one or more monoliths are preferably honeycomb.
- the preferred embodiments which contain one or more honeycomb monoliths, there are no particular restrictions on the honeycomb shape, provided that it is suitable, at least in part, for the one or more zeolites of the MFI, MEL and / or MWW zeolites. Structure type to be coated.
- the honeycomb consists of a plurality of parallel running channels which are separated by the walls of the monolith, preferably the shape of the channels and / or preferably the thickness of the walls of the monolith separating the channels from each other to a certain tolerance both with regard to the shape of the channels and with regard to the wall thickness, which is usually given by the substance used for the production of the monolith or by the method of production of the honeycomb or of the honeycomb form.
- channels are preferred which have a polygonal shape, preferably the shape of a regular polyhedron with three or more corners, preferably with three, four or six corners and more preferably with four corners.
- the dimensions of the channels in the preferred embodiments of the honeycomb monoliths is in principle not limited, provided that the dimensions selected at least partially coating the honeycomb monolith as the carrier substrate in the catalyst according to the invention with the one or more zeolites MFI, MEL and / or allowed by the MWW structure type.
- FIG. 500 to 1100 cpsi more preferably those having 93 to 163 (600 to 1 .050 cpsi), more preferably those having 109 to 155 (700 to 1,000 cpsi), more preferably those having 124 to 147 (800 to 950 cpsi) and more preferably those with 132 to 144 (850 to
- the support substrate contains one or more honeycomb monoliths
- those having 136 to 141 channels per square centimeter (880 to 910 cpsi) are used.
- the catalyst-coated layer of the present invention further contains a binder
- honeycomb monoliths having 8 to 124 channels per square centimeter (50 to 800 cpsi) are used honeycomb monoliths having from 23 to 109 channels per square centimeter (150 to 700 cpsi), more preferably those having 31 to 93 (200 to 600 cpsi), more preferably those having 39 to 85 (250 to 550 cpsi), and further preferably those with 47 to 78 (300 to 500 cpsi).
- embodiments according to which the one or more honeycomb-type monoliths have 54 to 70 channels per square centimeter (350 to 450 cpsi) are particularly preferred.
- embodiments of the present invention which use one or more monoliths as a carrier substrate in the catalyst, no foam-like substrates are contained therein.
- the carrier substrate contains no foams and in particular no foams as monolith.
- any suitable material and / or composite may be used as the substrate for the support substrate, preferably using those materials which have high temperature resistance and / or are highly inert with respect to their chemical reactivity.
- the ceramic materials are preferably selected from the group consisting of alumina, silica, silicates, aluminosilicates, silicon carbide, cordierite, mullite, zircon, spinels, magnesia, titania, and mixtures of two or more thereof.
- the ceramic materials preferably used for the carrier substrate are selected from the group consisting of ⁇ -alumina, silicon carbide, cordierite and mixtures of two or more thereof.
- the carrier substrate contains cordierite, wherein more preferably the carrier substrate is a cordierite substrate.
- the carrier substrate ceramic and / or metallic materials preferably ceramics, more preferably one or more substances selected from the group consisting of alumina, silica, silicates , Aluminosilicates, silicon carbide, cordierite, mullite, zircon, spinels, magnesia, titania and mixtures of two or more thereof, preferably from the group consisting of alpha alumina, silicon carbide, cordierite and mixtures of two or more thereof, wherein the support substrate particularly preferred is a cordierite substrate.
- zeolites contained in the catalyst there are no limitations whatsoever on the nature or the number of zeolites which can be used herein, provided that they are zeolites of one or more of the structural types MFI, MEL and MWW. If one or more of the zeolites contained in the catalyst are of the MWW structure type, again there is no restriction on the type and / or number of MWW zeolites which can be used according to the present invention.
- these may be selected from the group of MWW structure type zeolites consisting of MCM-22, MCM-36, [Ga-Si-O] -MWW, [Ti-Si-O] -MWW, ERB-1, ITQ-1 , PSH-3, SSZ-25 and mixtures of two or more thereof, preference being given to using MWW structure-type zeolites which are suitable for the conversion of oxygenates to olefins, in particular MCM-22 and / or MCM- 36th
- the zeolites of the MEL structure type which can be used in the catalyst according to the present invention, these being selected, for example, from the group consisting of ZSM-1 1, [Si-B-0] -MEL, boron-D (MFI / MEL solid solution), Boralite D, SSZ-46, Silicalite 2, TS-2, and mixtures of two or more thereof.
- those zeolites of the MEL structure type which are suitable for the conversion of oxygenates to olefins, in particular [Si-B-0] -MEL, are preferably used.
- MFI-type zeolites are used in the catalyst of the present invention for the conversion of oxygenates to olefins.
- the one or more MFI-type zeolites used in the catalyst according to the invention are preferably selected from the group consisting of ZSM-5, ZBM-10, [As-Si-O] MFI, [Fe-Si-O] MFI, [Ga-Si-O] MFI, AMS-1 B, AZ-1, Boron-C, Boralite C, Encilite, FZ- 1, LZ-105, monoclinic H-ZSM-5, mutinaite, NU-4, NU-5, silicalite, TS-1, TSZ, TSZ-III, TZ-01, USC-4, USI-108, ZBH, ZKQ -1 B, ZMQ-TB and mixture
- the catalyst contains ZSM-5 and / or ZBM-10 as an MFI-type zeolite, more preferably ZSM-5 is used as a zeolite.
- ZSM-5 is used as a zeolite.
- the zeolitic material ZBM-10 and its preparation reference is made, for example, to EP 0 007 081 A1 and to EP 0 034 727 A2, the contents of which, in particular with regard to the preparation and characterization of the material, are included in the present invention.
- the one or more zeolites are of the MFI structure type, and are preferably selected from the group consisting of ZSM-5, ZBM-10, As-Si-0] MFI, [Fe-Si-O] MFI, [Ga-Si-O] MFI, AMS-1 B, AZ-1, Boron-C, Boralite C, Encilite, FZ-1 , LZ-105, monoclinic H-ZSM-5, mutinaite, NU-4, NU-5, silicalite, TS-1, TSZ, TSZ-III, TZ-01, USC-4, USI-108, ZBH, ZKQ- 1 B, ZMQ-TB and mixtures of two or more thereof, more preferably from the group consisting of ZSM-5, ZBM-10, and mixtures thereof, wherein the MFI-type zeolite is preferably ZSM-5.
- the catalyst does not contain significant amounts of one or more non-zeolitic materials and, in particular, no substantial amounts of one or more aluminosilicophosphates (SAPO).
- SAPO aluminosilicophosphates
- the catalyst is substantially free of or does not contain substantial amounts of a specific material in cases where this specific material is present in an amount of 0.1% by weight or less in the catalyst relative to 100% by weight % of the total amount and the one or more MFI, MEL and / or MWW structural type zeolites, preferably in an amount of 0.05% by weight or less, more preferably 0.001% by weight or less, further preferably, 0.0005 wt% or less, and more preferably, 0.0001 wt% or less.
- a specific material within the meaning of the present invention particularly denotes a particular element or a particular combination of elements, a specific substance or a specific substance mixture, as well as combinations and / or mixtures of two or more thereof.
- the aluminosilicophosphates include in particular the SAPO materials SAPO-1 1, SAPO-47, SAPO-40, SAPO-43, SAPO-5, SAPO-31, SAPO-34, SAPO-37, SAPO-35, SAPO-42, SAPO-56, SAPO-18, SAPO-41, SAPO-39 and CFSAPO-1A.
- the one or more MFI, MEL and / or MWW type zeolites contain one or more alkaline earth metals.
- the present invention has no limitation whatsoever on the type and / or amount of alkaline earth metals contained in the one or more zeolites, nor on the manner in which they are contained in the one or more zeolites are included.
- the one or more zeolites may contain one or more alkaline earth metals, for example, selected from the group consisting of magnesium, calcium, strontium, barium and combinations of two or more thereof.
- the one or more alkaline earth metals are preferably selected from the group consisting of magnesium, calcium, strontium, and combinations of two or more thereof, and in particularly preferred embodiments of the catalyst of the present invention, the alkaline earth metal is magnesium.
- the catalyst contains no or no substantial amounts of calcium and / or strontium.
- embodiments of the catalyst for the conversion of oxygenates to olefins are preferred in which the alkaline earth metals contained in the one or more MFI, MEL and / or MWW structural type zeolites are selected from the group consisting of Mg, Ca, Sr, Ba and combinations of two or more thereof, preferably consisting of Mg, Ca, Sr and combinations of two or more thereof, wherein the alkaline earth metal is more preferably Mg.
- the one or more alkaline earth metals are contained in the one or more zeolites of the catalyst, they may in principle be contained in the micropores of the one or more zeolites and / or as part of the zeolitic one Skeleton present, in particular at least partially in isomorphous substitution to an element of the zeolite skeleton preferably to silicon and / or aluminum as a constituent of the zeolite skeleton and particularly preferably at least partially in isomorphous substitution to aluminum.
- the one or more alkaline earth metals in the micropores of the one or more zeolites, these may be present there as an independent compound such as salt and / or oxide and / or as a positive counterion to the zeolite framework.
- the one or more alkaline earth metals are present at least partially in the pores and preferably in the micropores of the one or more zeolites, more preferably wherein the one or more alkaline earth metals are at least partially present as the counterion of the zeolite framework, such as This may arise, for example, in the preparation of the one or more zeolites in the presence of the one or more alkaline earth metals and / or may be effected by carrying out an ion exchange with the one or more alkaline earth metals on the zeolite already prepared.
- any amount of the one or more alkaline earth metals may be present in the one or more zeolites, such as a total amount of the one or more alkaline earth metals of from 0.1 to 20% by weight, based on the total amount of one or more several zeolites.
- the one or more alkaline earth metals be present in a total amount in the range of 0.5-15% by weight based on 100% by weight of the total amount of the one or more zeolites from 1 to 10% by weight, more preferably from 2 to 7% by weight, more preferably from 3 to 5% by weight, and even more preferably from 3.5 to 4.5% by weight.
- the one or more alkaline earth metals are present in a total amount in the range of 3.8-4.2 wt% in the one or more zeolites. In all of the above-mentioned weight percentages of alkaline earth metal in the one or more zeolites, these are calculated as starting from the one or more alkaline earth metals as metal.
- the one or more MFI, MEL and / or MWW structural type zeolites contain the one or more alkaline earth metals in a total amount in the range of zero , 1 to 20 wt .-%, preferably from 0.5 to 15 wt .-%, more preferably from 1 to 10 wt .-%, more preferably from 2 to 7 wt .-%, more preferably from 3 to 5 wt .-%, more preferably from 3.5 to 4.5 wt .-%, and more preferably in the range of 3.8 to 4.2 wt .-%, each based on the total amount of the one or more zeolites of MFI, MEL and / or MWW structure type and calculated as metal.
- the layer applied to the substrate may be comprised of the one or more MFI, MEL, and / or MWW structure type zeolites containing one or more alkaline earth metals.
- the layer applied to the substrate contains one or more further components to said zeolites.
- the layer applied to the substrate for example, further catalytically active components, co-catalysts, fillers, vehicles and / or binders and combinations of two or more of them.
- the layer applied to the substrate further contains a binder.
- any suitable binder may be included in the layer so that one or more additional components may be included in the applied layer which act as a binder and in particular the cohesion of the further components and in particular the one or more zeolites improve.
- one or more components in the layer may be contained as a binder selected from the group consisting of S1O2, Al2O3, ⁇ 2, ZrÜ2, MgO, clay minerals and mixtures of two or more thereof, wherein according to a particularly preferred embodiment, the layer S1O2 as a binder in addition to the one or more zeolites of the MFI, MEL and / or MWW structure type.
- catalysts of the invention example 3 have the one or more zeolites of the MFI, MEL and / or the type of structure to MWW- in a total loading of 0.005-1 g / cm.
- the term "loading" means the amount of applied components of a layer in grams of dry matter per total volume of the carrier substrate, where volume refers to the volume of the coated carrier substrate, and in hollow bodies and / or cavities containing bodies and molds
- the volume in the loading of the carrier substrate in embodiments containing fillings refers to the respective volume of the fill including the interstices and cavities contained therein
- the catalyst contains the one or more MFI, MEL and / or MWW-type zeolites in a total loading of 0.01-0.5 g / cm 3, based on the volume of the coated carrier substrate and in particular on its Vo lumen according to the abovementioned specific and preferred definitions, more preferably in a total loading of 0.02-0.2 g / cm 3 , more preferably of 0.04-0.1 g / cm 3 , further preferably of 0.055-0, 08 g / cm 3 and more preferably 0.065-0.075
- the catalyst contains the one or more MFI, MEL and / or MWW-type zeolites in a total loading of 0.07-0.072 g / cm 3, based on the volume of the coated support substrate according to the particular and preferred definitions of the present application.
- the catalyst comprises the one or more zeolites of the MFI, MEL and / or MWW structure type in a total loading of 0.005 to 1 g / cm 3 based on the volume of the coated carrier substrate, preferably in a total loading of 0.01 to 0.5 g / cm 3 , more preferably from 0.02 to 0.2 g / cm 3 , more preferably from 0.04 to 0, 1 g / cm 3 , more preferably from 0.055 to 0.08 g / cm 3 , more preferably from 0.065 to 0.075 g / cm 3 , and further preferably in a total loading of from 0.07 to 0.072 g / cm 3 .
- the catalyst for the conversion of oxygenates to olefins contains the one or more zeolites from the MFI , MEL and / or of the MWW structure type in a total loading of 0.01 to 0.8 g / cm 3 based on the volume of the coated carrier substrate, preferably in a total loading of 0.05 to 0.5 g / cm 3 , on preferably from 0.08 to 0.3 g / cm 3 , more preferably from 0.12 to 0.25 g / cm 3 , more preferably from 0.15 to 0.23 g / cm 3 , further preferably from 0.17 to 0.21 g / cm 3 , and more preferably in a total loading of 0.18 to 0.2 g / cm 3 .
- the catalyst according to the present invention may be prepared in any suitable manner, provided it contains one or more zeolites of the MFI, MEL and / or MWW structure type contained in a layer applied to a support substrate according to the present invention Invention and in particular according to one of the specific and preferred embodiments of the invention, as described in the present application.
- the present invention also relates to a process for preparing a catalyst according to the present invention, and more particularly according to one of the particular or preferred embodiments thereof
- step (ix) optionally calcining the coated carrier substrate obtained in (vii) or (viii).
- the impregnation may be carried out by any suitable method, such as impregnation by impregnation, spray impregnation and / or capillary impregnation. According to particularly preferred embodiments of the method according to the invention, however, the impregnation in step (ii) is achieved by spray impregnation.
- step (i) MFI, MEL and / or MWW structure type.
- step (i) MFI, MEL and / or MWW structure type.
- steps are optionally carried out during the process according to the invention, preferably after the impregnation in step (ii) or after the mixture has been prepared in step (v) to bring several zeolites to a preferred particle size.
- the particle size of the one or more zeolites there is initially no particular restriction as regards the particle size of the one or more zeolites, provided that it is suitable for carrying out the further steps in the process according to the invention, in particular according to the particular and preferred embodiments of the present invention, wherein the particle size especially suitable for carrying out the coating in step (vii), in particular depending on the type and form of the carrier substrate used according to the present invention and in particular according to the particular or preferred embodiments of the carrier substrate as described in the present application.
- one or more steps are carried out after impregnation in step (ii) or after preparation of the mixture in step (v), preferably after preparation of the mixture in step (v) and particularly preferably in step ( vi) homogenizing the mixture obtained in (v) to obtain the one or more impregnated and optionally dried and / or calcined zeolites of the MFI, MEL and / or MWW type to a particle size D 5 o in the range of 0, 01 to 200 ⁇ bring.
- the one or more impregnated and optionally dried and / or calcined zeolites are prepared after preparing the mixture in step (v) and preferably in step (vi) homogenizing the mixture obtained in (v) one or more steps to a particle size D 5 o in the range of 0.5 to 15 ⁇ brought.
- one or more steps are carried out after impregnation in step (ii) or after preparation of the mixture in step (v), preferably after preparation of the mixture in step (v) and particularly preferably in step (vi) homogenizing the mixture obtained in (v) to obtain the one or more impregnated and optionally dried and / or calcined zeolites of the MFI, MEL and / or MWW structure type to a particle size Dgo in the range of 0.5 to 50 ⁇ m bring to.
- the one or more impregnated and optionally dried and / or calcined zeolites are prepared after preparing the mixture in step (v) and preferably in step (vi) homogenizing the mixture obtained in (v) one or more steps brought to a particle size Dgo in the range of 7 to 13 ⁇ .
- the one or more zeolites are preferably subjected to one or more of the milling steps of one or more of steps (ii) and (v), wherein the one or more zeolites are most preferably processed through homogenization in step (vi), in particular according to the particular and preferred embodiments of the present invention, to one of the particular or preferred particle sizes D 5 o is brought.
- embodiments of the method for producing a catalyst according to the present invention are preferred, according to which after impregnation in step (ii) or after preparation of the mixture in step (v), preferably after preparing the mixture in step (v) and more preferably in step (vi) homogenizing the mixture obtained in (v) containing one or more impregnated zeolites from the MFI, MEL and / or MWW structure type to a particle size D 5 o in the range of 0.01 to 200 ⁇ , more preferably from 0.03 to 150 ⁇ , more preferably from 0.05 to 100 ⁇ , more preferably from 0.1 to 50 ⁇ , further preferably from 0.3 to 30 ⁇ , more preferably from 0.4 to 20 ⁇ , even more preferably from 0.5 to 15 ⁇ are brought.
- embodiments of the method for producing a catalyst, and in particular a catalyst according to one of the particular or preferred embodiments thereof, are also preferred according to which after impregnation in step (ii) or after preparation of the mixture in step (v ), preferably after preparing the mixture in step (v) and more preferably in step (vi) homogenizing the mixture obtained in (v), the one or more impregnated zeolites of the MFI, MEL and / or of the MWW structure type to a particle size D90 in the range from 0.5 to 50 ⁇ m, more preferably from 1 to 30 ⁇ , more preferably from 3 to 20 ⁇ , more preferably from 5 to 15 ⁇ , more preferably from 9 to 1 1 ⁇ , and even more preferably from 7 to 13 ⁇ be brought.
- a step of drying after step (iii) and / or (viii) is carried out in the process according to the invention.
- the optional drying can be carried out at any suitable temperature and in any suitable atmosphere.
- the optional drying can be carried out under a protective gas atmosphere or in air, wherein the optional drying is preferably carried out in air.
- a temperature can be selected which is in the range of 50 to 220 ° C.
- the optional drying after step (iii) and / or (viii) is carried out at a temperature in the range from 70 to 180 ° C, more preferably from 80 to 150 ° C, more preferably from 90 to 130 ° C and more preferably in the range of 100 to 125 ° C.
- the drying after step (iii) and / or (viii) takes place at a temperature in the range of 1 10 to 120 ° C.
- the duration of the one or more optional drying steps in particular according to particular and preferred embodiments of the method according to the invention, there is no particular restriction, provided that drying suitable for the further process steps can be achieved, for example after a drying step with a duration of 1 to 50 hours.
- the optional drying is carried out for a period of from 5 to 40 hours, more preferably from 8 to 30 hours, more preferably from 10 to 25 hours, more preferably from 12 to 20 hours and even more preferably from 14 to 18 h.
- embodiments of the process for preparing a catalyst according to the present invention are preferred according to which the drying in (iii) and / or (viii) in a Temperature in the range of 50 to 220 ° C, preferably from 70 to 180 ° C, more preferably from 80 to 150 ° C, more preferably from 90 to 130 ° C, more preferably from 100 to 125 ° C, and further preferably from 1 10 to 120 ° C takes place.
- a temperature in the range of 300 to 850 ° C may be selected, preferably a temperature in the range of 350 to 750 ° C, more preferably of 400 to 700 ° C, more preferably from 450 to 650 ° C and even more preferably from 480 to 600 ° C is selected.
- the calcination in the optional step (iv) and / or (ix) is carried out at a temperature of 500 to 550 ° C.
- the optional calcination in step (iv) and / or or (ix) is preferably carried out in air.
- the duration of the calcining step in the optional step (iv) and / or (ix) if the product of the calcination is suitable for further use, in particular as an intermediate according to the optional step (iv), in the process according to the invention for the preparation of a catalyst, in particular a catalyst according to one of the specific or preferred embodiments of the present application.
- the duration of calcination after one or more of the optional calcination steps in (iv) and / or (ix) may be, for example, 0.5 to 20 hours, with a duration of 1 to 15 hours being preferred, more preferably 2 to 10 hours , more preferably from 3 to 7 hours and a duration of 4 to 5 hours is particularly preferred.
- embodiments of the process for producing a catalyst according to the present invention are preferred according to which the calcination in (iv) and / or (ix) in a Temperature in the range of 300 to 850 ° C, preferably from 350 to 750 ° C, more preferably from 400 to 700 ° C, more preferably from 450 to 650 ° C, more preferably from 480 to 600 ° C, and further preferably from 500 up to 550 ° C takes place.
- step (ii) of the process according to the invention the one or more zeolites of the MFI, MEL and / or MWW structure type are first impregnated with a solution containing one or more alkaline earth metals.
- a solution containing one or more alkaline earth metals there is no limitation in step (ii) as regards the type and / or number of solvents used therefor.
- any suitable solvent or solvent mixture can be used in step (ii), provided that it is suitable to bring about a corresponding impregnation of the materials defined there, in particular according to the particular and preferred embodiments of the present invention.
- step (v) for preparing the mixture defined therein, if the one or more solvents used are suitable, homogenizing in step (vi) and coating in step (vii) to enable.
- one or more solvents selected from the group consisting of alcohols, water, mixtures of two or more alcohols, and mixtures of water and one or more alcohols.
- the one or more solvents used in (ii) and / or (v) are selected from the group consisting of (C 1 -C 6) -alcohols, water, mixtures of two or more (C 1 -C 6) Alcohols and mixtures of water and one or more (C 1 -C 6) -alcohols, where the one or more solvents are more preferably selected from the group consisting of (C 1 -C 4) -alcohols, water, mixtures of two or more (C 1 -C 4) -alcohols. C4) alcohols and mixtures of water and one or more (Ci-C4) alcohols.
- the one or more solvents in steps (ii) and / or (v) are selected from the group consisting of methanol, ethanol, n-propanol, isopropanol, water and mixtures of two or more thereof, more preferably from the group consisting of methanol, ethanol, water and mixtures of two or more thereof, wherein even more preferably the solvent is water, preferably distilled water.
- embodiments of the method for producing a catalyst according to the present invention are preferred according to which the solution used in (ii) and / or that produced in (v) Mixture contains one or more solvents selected from the group consisting of alcohols, water, mixtures of two or more alcohols, and mixtures of water and one or more alcohols, preferably from the group consisting of (C1-C6) alcohols, water, mixtures of two or more (Ci-Ce) alcohols, and mixtures of water and one or more (Ci-Ce) alcohols, more preferably (C1-C4) alcohols, water, mixtures of two or more (C1-C4) alcohols, and Mixtures of water and one or more (C 1 -C 4) alcohols, more preferably consisting of methanol, ethanol, n-propanol, isopropanol, water r and mixtures of two or more thereof, more preferably consisting of
- the solids concentration of the mixture provided in (v) may be, for example, in the range of 5-50% by weight, the solids concentration according to the present invention preferably in the range of 10-30% by weight and more preferably in the range of 15 -25 wt .-% is. According to particularly preferred embodiments of the method according to the invention for the preparation of a catalyst, the solids concentration of the mixture provided in (v) is in the range of 18-22% by weight.
- embodiments of the process for producing a catalyst according to the present invention are preferred according to which the solid concentration of the mixture prepared in (v) is in the range of 5 to 50 wt %, preferably from 10 to 30% by weight, more preferably from 15 to 25% by weight, and more preferably from 18 to 22% by weight.
- the solids concentration of the mixture provided in (v) is in the range of 10-70% by weight, the solids concentration according to the present invention preferably in the range of 20-50 wt .-% and more preferably in the range of 30-40 wt .-% is. According to particularly preferred embodiments of the method according to the invention for the preparation of a catalyst, the solids concentration of the mixture provided in (v) is in the range of 32-36% by weight.
- the homogenization in step (vi) there is no particular limitation on the present invention, so that any conceivable procedure can be selected to produce a homogeneous mixture of the mixture prepared in step (v) using, for example, one or more methods may be selected from the group consisting of stirring, kneading, shaking, vibration or combination of two or more thereof.
- the mixture prepared in step (v) is preferably homogenized by stirring and / or vibration in step (vi), more preferably the homogenization in step (vi) is by vibration, preferably by ultrasound such as by using an ultrasonic bath into which the mixture to be homogenized is brought.
- embodiments of the process for producing a catalyst according to the present invention are preferred according to which the homogenization in (vi) is effected by stirring, kneading, shaking, vibration or combinations of two or more thereof, preferably by stirring and / or vibration, more preferably by vibration, and more preferably by ultrasound.
- the mixture produced in (v) and / or homogenized in (vi) may be one or more impregnated and optionally dried and / or calcined zeolites of the MFI, MEL and / or MWW structure type and one or more Solvent exist.
- the mixture produced in (v) and / or homogenized in (vi) contains one or more further components to the zeolites and the solvent.
- the mixture in (v) and / or (vi) contains, for example, further catalytic components, co-catalysts, fillers, auxiliaries, vehicles, binders and combinations of may contain two or more of them.
- the mixture in (v) and / or in (vi) contains a binder, wherein the binder may contain one or more substances.
- the binder can be added to the mixture in
- the binder in (vi) is added, this may be added either before homogenizing the mixture or at any time during homogenization, as long as a homogenized mixture is obtained in (vi).
- the one or more zeolites in step (vi) are brought to a specific D 5 o and / or D90 particle size
- embodiments are particularly preferred in which the addition of one or more further components to the zeolites and the solvent , And in particular in which the addition of an aid takes place, takes place only after the adjustment of the particle size.
- binders which are optionally added in the process
- any substance suitable for this purpose and any suitable substance mixture can be used, provided this leads to the desired increase in the cohesion of the layer in the coated carrier substrate.
- S1O2, Al2O3, T1O2, ZrO2, MgO, clay minerals, and mixtures of two or more thereof, as well as their respective precursor compounds and mixtures of two or more thereof, as well as mixtures of two or more of the former with two or more the precursor compounds thereof are used as binders in the process according to the invention.
- clay minerals and naturally occurring or synthetic aluminas such as alpha, beta, gamma, delta, eta, kappa, chi or theta alumina, and their inorganic and / or metalorganic precursor compounds can be used as the Al 2 O 3 binder and its precursor compounds such as gibbsite, bayerite, boehmite, pseudoboehmite, or trialkoxyaluminates such as aluminum triisopropylate.
- binders that can be used in the process are montmorillonite, kaolin, bentonite, halloysite, dickite, or nacrite.
- Preferred binders contain S1O2 and / or one or more of their precursor bonds, particularly preferably S1O2, preference being given to using colloidal S1O2.
- colloidal S1O2 is added as a binder in (v) and / or (vi) and preferably in (vi).
- concentration of the binder in the homogenized mixture obtained in (vi) there are no limitations, so that in principle any suitable amount of binder can be used, as long as the resulting catalyst can be used for the reaction of at least one oxygenate to at least one olefin.
- the binder may be present in an amount of from 0.1 to 50% by weight in (v) and / or (vi) and preferably in (vi) based on the total solids content of the homogenized mixture obtained in (vi).
- from 0.5 to 35% by weight of binder in (v) and / or (vi) and preferably in (vi) is added based on the total solids content of the homogenized mixture obtained in (vi), more preferably from From 1 to 30% by weight, more preferably from 5 to 25% by weight, more preferably from 7 to 20% by weight, more preferably from 9 to 17% by weight, more preferably from 10 to 15% by weight. %, and more preferably from 1 1 to 13% by weight.
- the coating of the carrier substrate in step (vii) of the method according to the invention in principle there is no restriction as regards its implementation, provided that a corresponding layer is at least partially formed on the carrier substrate.
- any suitable form of coating may be employed in the process of the present invention for preparing the catalyst of the present invention, wherein the coating in step (vii) is preferably by spray coating and / or wash coating.
- the coating in step (vii) is carried out by washcoating, the washcoating preferably taking place by dip coating.
- Such a preferred dip coating is carried out, for example, by immersing the carrier substrate one or more times in the mixture prepared in step (v) and homogenized in step (vi), wherein according to the present invention, the dip coating is preferably followed by a treatment to remove excess mixture from the carrier substrate.
- the further preferred treatment for removing excess mixture may, in principle, be after repeated dipping and / or between two or more dipping steps, wherein preferably after each step of the immersion excess mixture is removed by a suitable treatment from the coated carrier substrate.
- a step of immersion is carried out in the mixture prepared in step (v) and homogenized in step (vi), followed by a corresponding treatment for removing excess mixture.
- a step of immersion is carried out in the mixture prepared in step (v) and homogenized in step (vi), followed by a corresponding treatment for removing excess mixture.
- the particularly preferable removal of excess mixture according to the particular embodiments of the present method in which dip coating is carried out in step (vii), there is basically no limitation on the manner in which excess mixture is removed.
- removal may be achieved, for example, by appropriately suspending and / or leaving the coated support substrate and / or directly or indirectly by mechanical or other means, such as mechanical Stripping and / or by removal with a suitable gas blower and / or by appropriate application of centripetal forces, such as by suitably directed centrifugal forces.
- it is particularly preferred to remove the removal of excess mixture by a gas blower, more preferably by means of compressed air, by suitable blowing out of the excess mixture.
- step (vii) is repeated one or more times, preferably step (viii) and / or step (ix) and preferably both step (viii) and Step (ix) between repetitions.
- step (v) in which two or more layers of different composition, in particular with respect to the one or more zeolites, are applied to the carrier substrate, the steps (v) and (vi) are also correspondingly repeated in the preparation of the different compositions of the invention Mixture in step (v), which may refer not only to the chemical composition, but also to other properties of the mixture, such as the average particle size and / or the optional drying and / or the optional calcination of one or the several zeolites of MFI, MEL and / or MWW structure type.
- step (v) for producing the different layers on the carrier substrate according to these preferred embodiments also relate to the impregnation of the MFI, MEL and / or MWW structure type zeolites in step ( ii) the process of the invention and / or optional drying and / or optional calcining, as well as the manner of impregnation in step (ii) and / or drying in step (iii) and / or calcination in step (iv), according to these embodiments, the steps (ii) and optionally (iii) and / or (iv) are repeated accordingly.
- steps (vii) and (viii) and / or (ix) preferably steps (vii) - (ix) are repeated one or more times in order to coat the carrier several times. gersubstrats with a prepared in step (v) and in step (vi) homogenized mixture.
- step (vii) is repeated one or more times, preferably the steps ( vii) and (viii), more preferably steps (vii) to (ix), wherein the steps are preferably repeated once to five times, more preferably once to four times, more preferably once to three times, more preferably once or twice, and most preferably repeated twice.
- step (viii) is repeated one or more times, preferably the steps ( vii) and (viii), more preferably steps (vii) to (ix), wherein the steps are preferably repeated once to five times, more preferably once to four times, more preferably once to three times, more preferably once or twice, and most preferably repeated twice.
- the optional drying in (viii) may be at a temperature in the range of 50 to 220 ° C, preferably drying at a temperature in the range of 80 to 200 ° C, more preferably in the range of 100 to 180 ° C , more preferably in the range of 1 10 to 170 ° C, more preferably in the range of 120 to 160 ° C, more preferably in the range of 130 to 150 ° C, and more preferably in the range of 135 to 145 ° C.
- drying in step (viii) is preferably carried out for a period of 0.2 to 2 h, more preferably from 0.3 to 1.5 h, more preferably from 0.4 to 1.2 h, more preferably from 0.5 to 1 h, further preferably from 0.6 to 0.9 h, and further preferably from 0.7 to 0.8 h.
- the optional calcination in (ix) can be carried out, for example, at a temperature in the range from 250 to 1 .100 ° C., the calcination preferably taking place at a temperature in the range from 350 to 900 ° C., more preferably in the range from 400 to 800 ° C, more preferably in the range of 450 to 750 ° C, more preferably in the range of 500 to 700 ° C, more preferably in the range of 550 to 650 ° C, and more preferably in the range of 580 to 600 ° C.
- the duration of the calcination is also no restriction on the duration of the calcination, so that it can be carried out, for example, for a period of 0.5 to 20 h, wherein the calcination in step (ix) is preferably carried out for a period of 0.75 to 15 h, further from 1 to 10 h, more preferably from 1.5 to 5 h, more preferably from 2 to 4 h, more preferably from 2.5 to 3.5 h, and more preferably from 2.8 to 3.2 h.
- the coated substrate obtained in (vii) is both dried and subsequently calcined.
- the present invention also relates to such catalysts for the conversion of oxygenates to olefins, which are obtainable according to the manufacturing method of the invention , d. H. also catalysts per se, which can be obtained, for example, according to the manufacturing method according to the invention, without having to be prepared by this method.
- the present invention thus relates to catalysts for the conversion of oxygenates to olefins which can be obtained according to the process of the invention, in particular according to the particular and preferred embodiments described in the present application, but which can or have been prepared by another suitable process ,
- the catalyst and in particular the catalyst according to one of the particular or preferred embodiments of the present invention, is obtainable by the process according to the invention for the preparation of a catalyst according to one of the particular or preferred embodiments of the method according to the invention.
- the present invention also relates to a process for the conversion of oxygenates to olefins.
- the present invention relates to such a method comprising:
- the catalyst which can be used in the process according to the invention for the conversion of oxygenates to olefins, there is in principle no restriction, provided that it is a catalyst according to the present invention, as it is also obtainable by the process according to the invention, and if this catalyst is suitable for the conversion of at least one oxygenate to at least one olefin.
- the one or more oxygenates contained in the gas stream of (1) are selected from the group consisting of aliphatic alcohols, ethers, carbonyl compounds and mixtures of two or more thereof.
- the one or more oxygenates is selected from the group consisting of (Ci-C6) alcohols, di (Ci-C3) alkyl ethers, (Ci-Ce) -Aldehyden, (C2-Ce) -Ketonen and mixtures of two or more thereof, more preferably consisting of (C 1 -C 4 ) -alcohols, di- (C 1 -C 2) -alkyl ethers, (C 1 -C 4 ) -aldehydes, (C 2 -C 4 ) -ketones and mixtures of two or more thereof.
- the gas stream according to (1) contains one or more oxygenates selected from the group consisting of methanol, ethanol, n-propanol, isopropanol, butanol, dimethyl ether, diethyl ether, ethyl methyl ether, diisopropyl ether, di-n propyl ether, formaldehyde, dimethyl ketone and mixtures of two or more thereof, more preferably wherein the one or more oxygenates are selected from the group consisting of methanol, ethanol, dimethyl ether, diethyl ether, ethyl methyl ether and mixtures of two or more thereof.
- the gas stream according to (1) contains methanol and / or dimethyl ether as the one or more oxygenates, with dimethyl ether being particularly preferably the oxygenate contained in the gas stream according to (1).
- the gas stream of (1) contains one or more oxygenates selected from the group consisting of aliphatic alcohols, ethers, carbonyl compounds and mixtures of two or more thereof , preferably consisting ethers from (Ci-C 6) alcohols, di- (Ci-C 3) (Ci-C6) aldehydes, (C 2 -C 6) keto NEN, and mixtures of two or more thereof, more preferably consisting of (C 1 -C 4) alcohols, di (C 1 -C 2) alkyl ethers, (C 1 -C 4) aldehydes, (C 2 -C 4) ketones and mixtures of two or more thereof, more preferably from the group consisting of methanol, ethanol, n-propanol, isopropanol, butanol, dimethyl ether, diethyl ether, ethyl methyl
- the content of oxygenates in the gas stream according to (1) in the range of 30 to 100 vol.% Based on the total volume, wherein the content in particular to a gas stream at a temperature in the range of 200 to 700 ° C and at a pressure of 101, 3 kPa, preferably at a temperature in the range from 250 to 650 ° C, more preferably from 300 to 600 ° C, more preferably from 350 to 560 ° C, more preferably from 400 to 540 ° C, more preferably from 430 to 520 ° C, and more preferably in the range from 450 to 500 ° C and at a pressure of 101, 3 kPa.
- the content of oxygenates in the gas stream of (1) is in the range of 30 to 99% by volume, more preferably 30 to 95% by volume, further preferably 30 to 90% by volume %, more preferably from 30 to 80% by volume, more preferably from 30 to 70% by volume, further preferably from 30 to 60% by volume and more preferably from 30 to 50% by volume.
- the content of oxygenates in the gas stream according to (1) is in the range from 30 to 45% by volume.
- embodiments of the process for converting oxygenates to olefins are preferred in which the content of oxygenates in the gas stream according to (1) is in the range from 30 to 100% by volume, based on the total volume From 30 to 99% by volume, more preferably from 30 to 95% by volume, more preferably from 30 to 90% by volume, more preferably from 30 to 80% by volume, further preferably from 30 to 70% by volume %, more preferably from 30 to 60% by volume, more preferably from 30 to 50% by volume, and further preferably from 30 to 45% by volume.
- the gas stream according to (1) in the process according to the invention there is in principle no restriction, provided that the gas stream is altogether suitable for converting at least one of the oxygenates to at least one olefin in step (2) when brought into contact with a catalyst according to the present invention .
- one or more inert gases may be contained therein, such as one or more noble gases, nitrogen, water and mixtures of two or more thereof.
- the gas stream according to (1) of the process according to the invention contains water in addition to the one or more oxygenates.
- the content of water in the gas stream is in the range of 5 to 60% by volume based on the total volume, and the content of water is more preferably in the range of 10 to 55% by volume. is more preferably from 20 to 50 vol .-% and more preferably from 30 to 45 vol .-%.
- the gas stream provided in (1) originates from a pre-reaction, preferably from the conversion of one or more alcohols to one or more ethers, in particular from the conversion of one or more alcohols from the group consisting of methanol, ethanol, n-propanol, isopropanol and mixtures of two or more thereof, more preferably from the group consisting of methanol, ethanol, n-propanol and mixtures of two or more thereof, particularly preferably the in (1) provided gas stream of a pre-reaction of methanol and / or ethanol and more preferably methanol is at least partially converted to one or more di (Ci- C2) alkyl ethers, preferably to one or more di (Ci-C2) alkyl ethers selected from the group consisting of dimethyl ether, diethyl ether, ethyl methyl ether and mixtures of two or more of that.
- a pre-reaction preferably from the conversion of one or more alcohols to one or more ethers,
- the gas stream provided in (1) originates from a preliminary reaction of one or more alcohols
- the reaction product of the conversion of one or more alcohols provided this results in a gas stream containing one or more oxygenates which, when contacted in (2) with a catalyst according to the present invention, allows the conversion of at least one of the oxygenates to at least one olefin.
- the pre-reaction leads to the conversion of at least one alcohol to at least one ether and in particular to at least one dialkyl ether, wherein the pre-reaction is particularly preferably a dehydration in which water is the co-product one or more dialkyl ethers is obtained.
- the gas stream provided in (1) originates from a pre-reaction
- it is particularly preferred in accordance with the method according to the invention that one of such a pre-reaction tion gas stream is fed directly and without processing the process of the invention in step (1).
- step (2) of the process according to the invention for the conversion of oxygenates to olefins there is in principle no restriction provided that the conversion of at least one oxygenate to at least one olefin can be realized , This applies, for example, to the temperature at which contacting (2) takes place.
- the contacting in step (2) of the process according to the invention may take place at a temperature in the range from 200 to 700 ° C., preferably temperatures in the range from 250 to 650 ° C., more preferably from 300 to 600 ° C., more preferably from 350 to 560 ° C, more preferably from 400 to 540 ° C and more preferably from 430 to 520 ° C are selected.
- the contacting according to (2) of the inventive method is carried out at a temperature in the range of 450 to 500 ° C.
- embodiments of the process for converting oxygenates to olefins are preferred in which the contacting according to (2) at a temperature in the range from 200 to 700 ° C, preferably from 250 to 650 ° C, more preferably from 300 to 600 ° C, more preferably from 350 to 560 ° C, more preferably from 400 to 540 ° C, more preferably from 430 to 520 ° C, and more preferably from 450 to 500 ° C.
- contacting may in principle take place at any pressure, provided that it permits the conversion of at least one oxygenate to at least one olefin by contacting the gas flow with the catalyst.
- the pressure for example, when contacting in step (2) in the range of 0, 1 to 10 bar, the pressure in the present application indicates the absolute pressure, so that a pressure of 1 bar when contacting corresponding to the normal pressure of 1, 03 kPa corresponds.
- the contacting in step (2) preferably takes place at a pressure of 0.3 to 7 bar, more preferably from 0.5 to 5 bar, more preferably from 0.7 to 3 bar, further preferably from 0.8 to 2.5 bar and more preferably from 0.9 to 2.2 bar instead.
- the contacting takes place in step (2) at a pressure of 1 to 2 bar.
- embodiments of the process for the conversion of oxygenates to olefins are preferred in which the contacting according to (2) at a pressure in the range of 0.1 to 10 bar, preferably from 0.3 to 7 bar, more preferably from 0.5 to 5 bar, more preferably from 0.7 to 3 bar, more preferably from 0.8 to 2.5 bar, more preferably from 0.9 to 2.2 bar, and more preferably from 1 to 2 bar ,
- the mode of carrying out the process according to the invention for the conversion of oxygenates to olefins so that both a continuous and a non-continuous process can be used, wherein the non-continuous process can be carried out for example in the form of a batch process.
- preferred space velocities weight hourly space yelocity is defined as the ratio of oxygenates-reactant stream in kg / h to the amount calculated from zeolite in the reactor in kg
- space velocities for contacting the gas stream in step (2) are chosen in the range from 9 to 11 hr -1 .
- space velocities in contacting in step (2) can be chosen which range from 0.1 to 20 hr -1 space velocities of 0.5 to 15 hr 1 are preferably selected, more preferably from 1 to 10 hr 1 , more preferably from 1.5 to 8 hr 1 , more preferably from 2 to 7 hr 1 , further preferably from 2, 5 to 6 hr 1 , more preferably from 3 to 5 hr 1 , and more preferably from 3.5 to 4.5 hr 1 .
- embodiments of the process for converting oxygenates to olefins are preferred in which the space velocity in contacting in (2) is in the range of 0.5 to 50 hr 1 , preferably 1 to 30 hr 1 , more preferably 3 is up to 25 hr 1, more preferably 5 to 20 hr 1, more preferably 7-15 hr 1, more preferably 8 to 12 hr 1, and more preferably from 9 to 1 1 hr.
- the space velocity in contacting in step (2) is in the range from 0.1 to 20 hr 1 , preferably from 0.5 to 15 hr 1 , more preferably from 1 to 10 hr 1 , more preferably from 1.5 to 8 hr 1 , more preferably from 2 to 7 hr 1 , even more preferably from 2.5 to 6 hr 1 , more preferably from 3 to 5 hr 1 , and more preferably from 3.5 to 4.5 hr 1 .
- lifetimes are preferred which are in the range of 15 to 400 h, more preferably in the range of 20 to 300 h, more preferably from 60 to 250 h, more preferably from 90 to 220 h, more preferably from 1 10 to 200 h, more preferably from 130 to 180 hours, more preferably from 150 to 170 hours and more preferably from 155 to 165 hours.
- space velocities at which the erfindungsge- MAESSEN method is performed prior speeds of 15 to 400 hours at a space velocity in the range of 0.5 to 50 h -1 are preferred Thus, for example.
- a service life of 20 to 300 h at a space velocity of 1 to 30 hr 1 is preferably a service life of 60 to 250 h at a space velocity of 1 to 30 hr 1 , more preferably a service life of 90 to 220 h at a Space velocity of 3 to 25 hr 1 , more preferably a service life of 1 10 to 200 h at a space velocity in the range of 5 to 20 hr 1 , more preferably a service life of 130 to 180 h at a space velocity in the range of 7 to 15 hr 1 and more preferably from 150 to 170 h at a space velocity of 8 to 12 hl -1 .
- a life of the catalyst is selected during the continuous Liehe process is carried out without interruption, which is in the range of 155 to 165 H at a room rate of 9 to 1 1 hr. 1
- residence times are preferred which are in the range of 5 to 800 h, more preferably in the range of 10 to 600 h more preferably in the range of 30 to 550 hours, more preferably in the range of 50 to 500 hours, more preferably in the range of 70 to 450 hours, more preferably in the range of 80 to 420 hours, more preferably in the range from 90 to 400 hours, and more preferably in the range of 100 to 380 hours.
- the layer applied to the substrate further contains a binder
- service lives of, for example, 5 to 800 hours at a space velocity in the range from 0.1 to 20 hr.sup.- 1 are preferred.
- a service life of 10 to 600 h at a space velocity of 0.5 to 15 hr 1 more preferably a service life of 30 to 550 h at a space velocity of 1 to 10 hr 1 , more preferably a service life of 50 to 500 h at a space velocity of 1.5 to 8 hr 1 , more preferably a service life of 70 to 450 h at a space velocity of 2 to 7 hr 1 , more preferably a service life of 80 to 420 h at a space velocity of 2.5 to 6 hr 1 , more preferably a service life of 90 to 400 h at a space velocity of 3 to 5 hr 1 , and more preferably a service life of 100 to 380 h at a space velocity of 3.5 to 4.5 hr. 1
- the particular and preferred embodiments with regard to the selected service life and in particular the selected service lives in combination with certain space velocities, preferably relate to a minimum conversion of the one or more oxygenates contained in the gas stream according to (1) of the method according to the invention whose permanent drop below the regeneration of the catalyst is subsequently carried out.
- the selected minimum conversion which preferably allows full conversion of the one or more oxygenates contained in the gas stream according to (1) of the process according to the invention during the service life of the catalyst.
- a minimum conversion of 60% of the one or more oxygenates contained in the gas stream according to (1) of the process according to the invention is selected, at whose permanent underrun the regeneration of the catalyst is carried out, preferably a minimum conversion of 70% or more, more preferably 80% or more, further preferably 85% or more, still more preferably 90% or more, still more preferably 95% or more, still more preferably 97% or more, still more preferably 98% or more, and more preferably 99% or more, of the one or more oxygenates contained in the gas stream according to (1) of the process of the invention.
- embodiments of the process for the conversion of oxygenates to olefins are further preferred in which the service life of the coated carrier substrate as a catalyst, during which the continuous process is carried out without interruption, in the range of 15 to 400 h, preferably from 20 to 300 h, more preferably from 60 to 250 h, more preferably from 90 to 220 h, more preferably from 110 to 200 h, more preferably from 130 to 180 h, more preferably from 150 to 170 h, and still more preferably from 155 up to 165 h.
- the present invention also relates to the use of the catalyst according to the invention as described above, and in particular the use of the catalyst according to the invention according to the particular and preferred embodiments as described in the present application.
- the present invention in principle, there is no Restriction on the use of the catalyst according to the invention, so that it can be used both for the conversion of oxygenates to olefins and in any conceivable catalytic process in which the catalyst exhibits a corresponding catalytic effect with respect to a chemical reaction.
- the catalyst according to the invention is preferably used in a methanol-to-olefin process (MTO process) and furthermore preferably in a methanol-to-gasoline process (MTG process), in a methanol-to-methanol process.
- MTO process methanol-to-olefin process
- MTG process methanol-to-gasoline process
- Hydrocarbon process in a methanol-to-propylene process (MTP process), in a methanol-to-propylene / butylene process (MT3 / 4 process) and for the alkylation of aromatics or in a fluid catalytic - Cracking method (FCC method).
- the catalyst of the present invention is preferably used in a methanol-to-olefin (MTO) process, more preferably in a methanol-to-propylene / butylene process (MT3 / 4 process), especially in a process for the conversion of oxygenates to olefins according to one of the particular or preferred processes for the conversion of oxygenates to olefins according to the present invention.
- MTO methanol-to-olefin
- MT3 / 4 process methanol-to-propylene / butylene process
- H-ZSM-5 ZO-cat PZ2-100 H from Zeochem
- the initial weight was chosen such that the zeolite / binder ratio in the calcined extrudates corresponds to 60:40. This putty was pushed with the aid of an extruder at about 100 bar through a 2.5 mm die.
- the strands were anschmanend 16 h at 120 ° C in a drying oven dried and calcined (after 4 h heating) for 4 h at 500 ° C in a muffle furnace. Thereafter, the strands were processed in a screening machine with 2 steel balls (diameter about 2 cm, 258 g / ball) to 1, 6- 2.0 mm grit.
- the amount of Mg was weighed so that the powder after calcination contains 4% by weight of Mg.
- 58.7 g of zeolite powder were placed in a round bottom flask and placed in a rotary evaporator. 43.9 g of magnesium nitrate were dissolved in water with heating, and with dist. Water is made up to 54 ml of total fluid.
- the resulting magnesium nitrate solution was charged into a dropping funnel and slowly sprayed onto the powder while rotating through a glass spray nozzle flooded with 100 l / h of N 2. At regular intervals, the piston was suspended and shaken by hand to achieve an even distribution. After complete addition of the magnesium nitrate solution, the powder was 10 min. continues to rotate. The powder was then dried for 16 hours at 120 ° C. in a quartz rotary flask, then calcined for 5 hours at 500 ° C. under air (20 L / h), and then the calcined powder was ground to a small size by means of an analytical mill and through a sieve with a mesh size of Sieved 1 mm.
- the BET surface area of the obtained magnesium-impregnated zeolite was 303 m 2 / g.
- Mg-ZSM-5 powder prepared according to Example 1 was slowly added until a solids content of 33% by weight was reached. Subsequently, the grinding of the Mg-ZSM-5 starting suspension was carried out in a stirred ball mill to a particle size D90 of 10 ⁇ . The temperature during grinding did not exceed 30 ° C. After milling, Ludox AS-40 was added as a binder. The solids content of the binder was in total 12% by weight, based on the total solids content of the final suspension.
- the suspension was applied to a honeycomb body (cordierite honeycomb body with a cell density of 400 cpsi (62 cells / cm 2 ) and a wall thickness of 6). 7 mil (152.4 ⁇ - 177.8 ⁇ )) applied.
- the suspension was diluted to a solids content of 28%.
- the catalyst was immersed in the suspension over the full height so that all cells were completely filled. After waiting for 10 seconds, the substrate was withdrawn from the suspension, inverted, and freed of excess suspension with inlet side to outlet side compressed air.
- the catalyst was dried in a dryer by means of hot air (140 ° C) alternately from both sides with a respective cycle time of 10 seconds for a total of 45 minutes. Thereafter, the catalyst was calcined in the continuous calciner at a maximum temperature of 590 ° C, during which process the catalyst underwent three warm-up, holding and cooling zones within three hours.
- Example 3 Preparation of Mg-ZSM-5 coated carrier (load: -150 g / L)
- Example 4 Preparation of Mg-ZSM-5 coated carrier (load: -190 g / L)
- Example 5 Comparative Experiments in the Methanol-to-Propylene / Butylene Process (MT3 / 4 Process)
- WHSV weight hourly space yelocity
- Table 1 Average selectivities of one cycle (methanol conversion of> 95%).
- a catalyst for the conversion of oxygenates an unexpectedly high selectivity to C3 and C4 olefins is by the present invention provided to olefins which, as was shown in Example 5 on the basis of the test results in MT3 / 4 method, which comprises using surprisingly long service life is associated, in particular in comparison to a catalyst which is present as an extrudate (see Comparative Example 1) or which was applied to a carrier substrate, but no alkaline earth metal has (see Comparative Example 2).
- the present invention also provides a catalyst for the conversion of oxygenates to olefins which, through the use of a binder, not only increases the resistance of the catalyst, but also its service life by the possibility of using higher loadings of the catalyst on the carrier substrate.
- a binder could cause in the catalyst of the invention to a further improvement in the selectivity toward C 4 olefins and in particular also towards C3 olefins. Accordingly, a much improved catalyst for the conversion of oxygenates to olefins is provided by the present invention, which has particularly long service life at the same time high selectivities towards C3 and C4 olefins.
- Ciambelli et al "Acid-base catalysis in the conversion of methanol to olefins over Mg-modified ZSM-5 zeolite", Successful Design of Catalysts, Elsevier Science Publishers B.V., Amsterdam, 1988, pp. 239-246
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- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Crystallography & Structural Chemistry (AREA)
- Catalysts (AREA)
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Abstract
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Priority Applications (9)
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BR112014031094A BR112014031094A8 (pt) | 2012-06-29 | 2013-06-26 | catalisador para conversão de oxigenados em olefinas, processo para a sua preparação e usos relacionados |
AU2013283349A AU2013283349B2 (en) | 2012-06-29 | 2013-06-26 | Catalyst coating and method for the conversion of oxygenates to olefins |
MX2014015736A MX2014015736A (es) | 2012-06-29 | 2013-06-26 | Recubrimiento de catalizador y proceso para la conversión de oxigenatos en olefinas. |
EP13732467.9A EP2866934A2 (de) | 2012-06-29 | 2013-06-26 | Katalysatorbeschichtung und verfahren für die umwandlung von oxygenaten zu olefinen |
RU2015102718A RU2015102718A (ru) | 2012-06-29 | 2013-06-26 | Покрытый катализатор и способ превращения оксигенатов в олефины |
CN201380042077.9A CN104582841A (zh) | 2012-06-29 | 2013-06-26 | 将氧合物转化成烯烃的催化剂涂层和方法 |
CA2877796A CA2877796C (en) | 2012-06-29 | 2013-06-26 | Catalyst coating and process for the conversion of oxygenates to olefins |
JP2015519079A JP6466325B2 (ja) | 2012-06-29 | 2013-06-26 | オキシジェネートからオレフィンへの転化のための触媒コーティングおよび方法 |
ZA2015/00361A ZA201500361B (en) | 2012-06-29 | 2015-01-19 | Catalyst coating and method for the conversion of oxygenates to olefins |
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EP12174293 | 2012-06-29 |
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EP (1) | EP2866934A2 (de) |
JP (1) | JP6466325B2 (de) |
CN (2) | CN109453804A (de) |
AU (1) | AU2013283349B2 (de) |
BR (1) | BR112014031094A8 (de) |
CA (1) | CA2877796C (de) |
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Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9597669B2 (en) | 2012-06-29 | 2017-03-21 | Basf Se | Catalyst and process for the conversion of oxygenates to olefins |
US9675971B2 (en) | 2014-10-22 | 2017-06-13 | King Fahd University Of Petroleum And Minerals | Honeycomb monolith structure loaded with nanozeolites for enhanced propylene selectivity in methanol conversion |
US9682367B2 (en) | 2014-10-22 | 2017-06-20 | King Fahd University Of Petroleum And Minerals | Monolith structure loaded with metal promoted nanozeolites for enhanced propylene selectivity in methanol conversion |
US10005702B2 (en) | 2012-06-29 | 2018-06-26 | Basf Se | Catalyst coating and process for the conversion of oxygenates to olefins |
US10213773B2 (en) | 2012-06-29 | 2019-02-26 | Basf Se | Process for the conversion of oxygenates to olefins |
CN111760589A (zh) * | 2020-07-10 | 2020-10-13 | 大唐国际化工技术研究院有限公司 | 分子筛催化剂及其制备方法和应用 |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4049573A (en) | 1976-02-05 | 1977-09-20 | Mobil Oil Corporation | Zeolite catalyst containing oxide of boron or magnesium |
EP0007081A1 (de) | 1978-07-13 | 1980-01-23 | BASF Aktiengesellschaft | Verfahren zur Herstellung von stickstoffhaltigen kristallinen Metallsilikaten mit Zeolithstruktur, nach dem Verfahren hergestellte Metallsilikate sowie deren Verwendung als Katalysatoren |
EP0034727A2 (de) | 1980-02-21 | 1981-09-02 | BASF Aktiengesellschaft | Kristalline isotaktische Zeolithe, Verfahren zur Herstellung derselben sowie deren Verwendung als Katalysatoren |
DD238733A1 (de) | 1984-12-29 | 1986-09-03 | Leuna Werke Veb | Herstellung selektiver olefinkatalysatoren |
US4692423A (en) | 1985-12-04 | 1987-09-08 | Mobil Oil Corporation | Method for preparing structured catalytic solids |
WO1994025151A1 (en) | 1993-04-23 | 1994-11-10 | Exxon Chemical Patents Inc. | Molecular sieve layers and processes for their manufacture |
WO1998029519A1 (en) | 1996-12-31 | 1998-07-09 | Exxon Chemical Patents Inc. | Conversion of oxygenates to hydrocarbons with monolith supported non-zeolitic molecular sieve catalysts |
Family Cites Families (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6251630A (ja) * | 1985-08-29 | 1987-03-06 | Agency Of Ind Science & Technol | 低級オレフインの製造方法 |
DE4009459A1 (de) * | 1990-03-23 | 1991-09-26 | Metallgesellschaft Ag | Verfahren zur erzeugung von niederen olefinen |
JPH07241471A (ja) * | 1994-03-04 | 1995-09-19 | Nissan Motor Co Ltd | 排ガス浄化用吸着触媒の製造方法 |
JP3498410B2 (ja) * | 1995-03-07 | 2004-02-16 | 日産自動車株式会社 | 排気ガス浄化用触媒 |
JP2005514319A (ja) * | 2002-10-24 | 2005-05-19 | エクソンモービル・ケミカル・パテンツ・インク | 酸触媒の安定化 |
ZA200607799B (en) * | 2004-03-22 | 2008-06-25 | Celgene Corp | Methods of using and compositions comprising immuno-modulatory compounds for the treatment and management of skin diseases or disorders |
JP2008080301A (ja) * | 2006-08-30 | 2008-04-10 | Jgc Corp | アルカリ土類金属化合物含有ゼオライト触媒およびその調製方法、並びに、低級炭化水素の製造方法 |
JP5303131B2 (ja) * | 2006-09-19 | 2013-10-02 | 株式会社日本自動車部品総合研究所 | 炭素系物質燃焼触媒及びその製造方法、触媒担持体及びその製造方法 |
CN101239875B (zh) * | 2007-02-07 | 2010-11-10 | 中国石油化工股份有限公司 | 由甲醇制取丙烯的方法 |
JP5744730B2 (ja) * | 2009-06-22 | 2015-07-08 | 日揮株式会社 | 低級オレフィン製造用触媒およびそれを用いた低級オレフィンの製造方法 |
EP2335810B1 (de) * | 2009-12-11 | 2012-08-01 | Umicore AG & Co. KG | Selektive katalytische Reduktion von Stickoxiden im Abgas von Dieselmotoren |
CA2877560C (en) * | 2012-06-29 | 2020-07-21 | Basf Se | Catalyst and process for the conversion of oxygenates to olefins |
-
2013
- 2013-06-26 JP JP2015519079A patent/JP6466325B2/ja not_active Expired - Fee Related
- 2013-06-26 CN CN201811397259.9A patent/CN109453804A/zh active Pending
- 2013-06-26 AU AU2013283349A patent/AU2013283349B2/en not_active Ceased
- 2013-06-26 CA CA2877796A patent/CA2877796C/en not_active Expired - Fee Related
- 2013-06-26 CN CN201380042077.9A patent/CN104582841A/zh active Pending
- 2013-06-26 MX MX2014015736A patent/MX2014015736A/es unknown
- 2013-06-26 BR BR112014031094A patent/BR112014031094A8/pt not_active IP Right Cessation
- 2013-06-26 WO PCT/EP2013/063436 patent/WO2014001412A2/de active Application Filing
- 2013-06-26 RU RU2015102718A patent/RU2015102718A/ru not_active Application Discontinuation
- 2013-06-26 EP EP13732467.9A patent/EP2866934A2/de not_active Withdrawn
-
2015
- 2015-01-19 ZA ZA2015/00361A patent/ZA201500361B/en unknown
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4049573A (en) | 1976-02-05 | 1977-09-20 | Mobil Oil Corporation | Zeolite catalyst containing oxide of boron or magnesium |
EP0007081A1 (de) | 1978-07-13 | 1980-01-23 | BASF Aktiengesellschaft | Verfahren zur Herstellung von stickstoffhaltigen kristallinen Metallsilikaten mit Zeolithstruktur, nach dem Verfahren hergestellte Metallsilikate sowie deren Verwendung als Katalysatoren |
EP0034727A2 (de) | 1980-02-21 | 1981-09-02 | BASF Aktiengesellschaft | Kristalline isotaktische Zeolithe, Verfahren zur Herstellung derselben sowie deren Verwendung als Katalysatoren |
DD238733A1 (de) | 1984-12-29 | 1986-09-03 | Leuna Werke Veb | Herstellung selektiver olefinkatalysatoren |
US4692423A (en) | 1985-12-04 | 1987-09-08 | Mobil Oil Corporation | Method for preparing structured catalytic solids |
WO1994025151A1 (en) | 1993-04-23 | 1994-11-10 | Exxon Chemical Patents Inc. | Molecular sieve layers and processes for their manufacture |
WO1998029519A1 (en) | 1996-12-31 | 1998-07-09 | Exxon Chemical Patents Inc. | Conversion of oxygenates to hydrocarbons with monolith supported non-zeolitic molecular sieve catalysts |
Non-Patent Citations (11)
Title |
---|
ANTIA ET AL., IND. ENG. CHEM. RES., vol. 34, 1995, pages 140 - 147 |
CIAMBELLI ET AL.: "Successful Design of Catalysts", 1988, ELSEVIER SCIENCE PUBLISHERS, article "Acid-base catalysis in the conversion of methanol to olefins over Mg- modified ZSM-5 zeolite", pages: 239 - 246 |
CIAMBELLI ET AL.: "Successful Design of Catalysts", 1988, ELSEVIER SCIENCE PUBLISHERS, article "Acid-base catalysis in the conversion of methanol to olefins over Mg-modified ZSM-5 zeolite", pages: 239 - 246 |
GORYAINOVA ET AL., PETROLEUM CHEMISTRY, vol. 51, no. 3, 2011, pages 169 - 173 |
HAMMON ET AL., APPLIED CATALYSIS, vol. 37, 1988, pages 155 - 174 |
IVANOVA ET AL., J. PHYS. CHEM. C, vol. 111, 2007, pages 4368 - 4374 |
LI ET AL., CATAL. LETT., vol. 129, 2009, pages 408 - 415 |
MCLNTOSH ET AL., APPLIED CATALYSIS, vol. 6, 1983, pages 307 - 314 |
OKADO ET AL., APPLIED CATALYSIS, vol. 41, 1988, pages 121 - 135 |
PATCAS, F. C., JOURNAL OF CATALYSIS, vol. 231, 2005, pages 194 - 200 |
See also references of EP2866934A2 |
Cited By (8)
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US9597669B2 (en) | 2012-06-29 | 2017-03-21 | Basf Se | Catalyst and process for the conversion of oxygenates to olefins |
US10005702B2 (en) | 2012-06-29 | 2018-06-26 | Basf Se | Catalyst coating and process for the conversion of oxygenates to olefins |
US10213773B2 (en) | 2012-06-29 | 2019-02-26 | Basf Se | Process for the conversion of oxygenates to olefins |
US9675971B2 (en) | 2014-10-22 | 2017-06-13 | King Fahd University Of Petroleum And Minerals | Honeycomb monolith structure loaded with nanozeolites for enhanced propylene selectivity in methanol conversion |
US9682367B2 (en) | 2014-10-22 | 2017-06-20 | King Fahd University Of Petroleum And Minerals | Monolith structure loaded with metal promoted nanozeolites for enhanced propylene selectivity in methanol conversion |
US9738570B1 (en) | 2014-10-22 | 2017-08-22 | King Fahd University Of Petroleum And Minerals | Method for methanol conversion to propylene over a monolithic catalyst system |
US9845271B2 (en) | 2014-10-22 | 2017-12-19 | King Fahd University Of Petroleum And Minerals | Method for forming light olefins from methanol |
CN111760589A (zh) * | 2020-07-10 | 2020-10-13 | 大唐国际化工技术研究院有限公司 | 分子筛催化剂及其制备方法和应用 |
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BR112014031094A2 (pt) | 2017-06-27 |
BR112014031094A8 (pt) | 2021-01-26 |
CN104582841A (zh) | 2015-04-29 |
AU2013283349B2 (en) | 2017-05-04 |
ZA201500361B (en) | 2016-03-30 |
AU2013283349A1 (en) | 2015-01-22 |
JP2015522408A (ja) | 2015-08-06 |
RU2015102718A (ru) | 2016-08-20 |
CA2877796A1 (en) | 2014-01-03 |
EP2866934A2 (de) | 2015-05-06 |
WO2014001412A3 (de) | 2014-02-27 |
CN109453804A (zh) | 2019-03-12 |
CA2877796C (en) | 2020-06-30 |
MX2014015736A (es) | 2015-09-04 |
JP6466325B2 (ja) | 2019-02-06 |
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