WO2010150676A1 - 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 - Google Patents
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 Download PDFInfo
- Publication number
- WO2010150676A1 WO2010150676A1 PCT/JP2010/060035 JP2010060035W WO2010150676A1 WO 2010150676 A1 WO2010150676 A1 WO 2010150676A1 JP 2010060035 W JP2010060035 W JP 2010060035W WO 2010150676 A1 WO2010150676 A1 WO 2010150676A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- catalyst
- producing
- lower olefin
- less
- zeolite
- Prior art date
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 212
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 107
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title abstract description 15
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract description 98
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 54
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 51
- 239000010457 zeolite Substances 0.000 claims abstract description 51
- 239000011949 solid catalyst Substances 0.000 claims abstract description 45
- 150000001875 compounds Chemical class 0.000 claims abstract description 33
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000001301 oxygen Substances 0.000 claims abstract description 25
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 25
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 60
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 claims description 57
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 29
- 150000001342 alkaline earth metals Chemical class 0.000 claims description 27
- 239000000203 mixture Substances 0.000 claims description 25
- 239000011575 calcium Substances 0.000 claims description 14
- 239000011230 binding agent Substances 0.000 claims description 13
- 229910052782 aluminium Inorganic materials 0.000 claims description 9
- 238000012856 packing Methods 0.000 claims description 9
- 238000000465 moulding Methods 0.000 claims description 8
- 239000002798 polar solvent Substances 0.000 claims description 8
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 7
- 229910052710 silicon Inorganic materials 0.000 claims description 6
- 239000010703 silicon Substances 0.000 claims description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 4
- 229910052791 calcium Inorganic materials 0.000 claims description 4
- 239000004927 clay Substances 0.000 claims description 4
- 229910052570 clay Inorganic materials 0.000 claims description 4
- 238000010304 firing Methods 0.000 claims description 4
- 150000004679 hydroxides Chemical class 0.000 claims description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 3
- 238000004898 kneading Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims description 2
- 229910052814 silicon oxide Inorganic materials 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 9
- 238000006243 chemical reaction Methods 0.000 description 39
- 239000002994 raw material Substances 0.000 description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- 230000000052 comparative effect Effects 0.000 description 12
- 239000007789 gas Substances 0.000 description 11
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 9
- 238000001125 extrusion Methods 0.000 description 9
- 239000008188 pellet Substances 0.000 description 7
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 230000000717 retained effect Effects 0.000 description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 5
- 239000011777 magnesium Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 4
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 description 4
- 239000013078 crystal Substances 0.000 description 4
- -1 dimethyl ether Chemical class 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 4
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 3
- 229910004283 SiO 4 Inorganic materials 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 150000001341 alkaline earth metal compounds Chemical class 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- 239000002243 precursor Substances 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 2
- 229910001593 boehmite Inorganic materials 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- VSGNNIFQASZAOI-UHFFFAOYSA-L calcium acetate Chemical compound [Ca+2].CC([O-])=O.CC([O-])=O VSGNNIFQASZAOI-UHFFFAOYSA-L 0.000 description 2
- 239000001639 calcium acetate Substances 0.000 description 2
- 235000011092 calcium acetate Nutrition 0.000 description 2
- 229960005147 calcium acetate Drugs 0.000 description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 description 2
- 235000012241 calcium silicate Nutrition 0.000 description 2
- 229910052918 calcium silicate Inorganic materials 0.000 description 2
- XFWJKVMFIVXPKK-UHFFFAOYSA-N calcium;oxido(oxo)alumane Chemical compound [Ca+2].[O-][Al]=O.[O-][Al]=O XFWJKVMFIVXPKK-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003085 diluting agent Substances 0.000 description 2
- 150000002170 ethers Chemical class 0.000 description 2
- 238000001027 hydrothermal synthesis Methods 0.000 description 2
- FAHBNUUHRFUEAI-UHFFFAOYSA-M hydroxidooxidoaluminium Chemical compound O[Al]=O FAHBNUUHRFUEAI-UHFFFAOYSA-M 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- YIXJRHPUWRPCBB-UHFFFAOYSA-N magnesium nitrate Chemical compound [Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O YIXJRHPUWRPCBB-UHFFFAOYSA-N 0.000 description 2
- 239000000395 magnesium oxide Substances 0.000 description 2
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 2
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 1
- 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
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 229910015999 BaAl Inorganic materials 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 229910003668 SrAl Inorganic materials 0.000 description 1
- 239000005084 Strontium aluminate Substances 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 229910001413 alkali metal ion Inorganic materials 0.000 description 1
- 229910000323 aluminium silicate Inorganic materials 0.000 description 1
- 150000001408 amides Chemical class 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- ITHZDDVSAWDQPZ-UHFFFAOYSA-L barium acetate Chemical compound [Ba+2].CC([O-])=O.CC([O-])=O ITHZDDVSAWDQPZ-UHFFFAOYSA-L 0.000 description 1
- AYJRCSIUFZENHW-UHFFFAOYSA-L barium carbonate Chemical compound [Ba+2].[O-]C([O-])=O AYJRCSIUFZENHW-UHFFFAOYSA-L 0.000 description 1
- RQPZNWPYLFFXCP-UHFFFAOYSA-L barium dihydroxide Chemical compound [OH-].[OH-].[Ba+2] RQPZNWPYLFFXCP-UHFFFAOYSA-L 0.000 description 1
- 229910001863 barium hydroxide Inorganic materials 0.000 description 1
- IWOUKMZUPDVPGQ-UHFFFAOYSA-N barium nitrate Chemical compound [Ba+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O IWOUKMZUPDVPGQ-UHFFFAOYSA-N 0.000 description 1
- QVQLCTNNEUAWMS-UHFFFAOYSA-N barium oxide Chemical compound [Ba]=O QVQLCTNNEUAWMS-UHFFFAOYSA-N 0.000 description 1
- 229910052916 barium silicate Inorganic materials 0.000 description 1
- HMOQPOVBDRFNIU-UHFFFAOYSA-N barium(2+);dioxido(oxo)silane Chemical compound [Ba+2].[O-][Si]([O-])=O HMOQPOVBDRFNIU-UHFFFAOYSA-N 0.000 description 1
- QKYBEKAEVQPNIN-UHFFFAOYSA-N barium(2+);oxido(oxo)alumane Chemical compound [Ba+2].[O-][Al]=O.[O-][Al]=O QKYBEKAEVQPNIN-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229940043430 calcium compound Drugs 0.000 description 1
- 150000001674 calcium compounds Chemical class 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- JHLNERQLKQQLRZ-UHFFFAOYSA-N calcium silicate Chemical compound [Ca+2].[Ca+2].[O-][Si]([O-])([O-])[O-] JHLNERQLKQQLRZ-UHFFFAOYSA-N 0.000 description 1
- 239000000378 calcium silicate Substances 0.000 description 1
- OYACROKNLOSFPA-UHFFFAOYSA-N calcium;dioxido(oxo)silane Chemical compound [Ca+2].[O-][Si]([O-])=O OYACROKNLOSFPA-UHFFFAOYSA-N 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000006482 condensation reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- UAMZXLIURMNTHD-UHFFFAOYSA-N dialuminum;magnesium;oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[O-2].[Mg+2].[Al+3].[Al+3] UAMZXLIURMNTHD-UHFFFAOYSA-N 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- IEJIGPNLZYLLBP-UHFFFAOYSA-N dimethyl carbonate Chemical compound COC(=O)OC IEJIGPNLZYLLBP-UHFFFAOYSA-N 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- BDAGIHXWWSANSR-NJFSPNSNSA-N hydroxyformaldehyde Chemical compound O[14CH]=O BDAGIHXWWSANSR-NJFSPNSNSA-N 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- HCWCAKKEBCNQJP-UHFFFAOYSA-N magnesium orthosilicate Chemical compound [Mg+2].[Mg+2].[O-][Si]([O-])([O-])[O-] HCWCAKKEBCNQJP-UHFFFAOYSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- 150000007522 mineralic acids Chemical class 0.000 description 1
- 239000004570 mortar (masonry) Substances 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 150000002825 nitriles Chemical class 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- UFQXGXDIJMBKTC-UHFFFAOYSA-N oxostrontium Chemical compound [Sr]=O UFQXGXDIJMBKTC-UHFFFAOYSA-N 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 235000019353 potassium silicate Nutrition 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000011164 primary particle Substances 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000010079 rubber tapping Methods 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- FNWBQFMGIFLWII-UHFFFAOYSA-N strontium aluminate Chemical compound [O-2].[O-2].[O-2].[O-2].[O-2].[Al+3].[Al+3].[Sr+2].[Sr+2] FNWBQFMGIFLWII-UHFFFAOYSA-N 0.000 description 1
- 229910000018 strontium carbonate Inorganic materials 0.000 description 1
- UUCCCPNEFXQJEL-UHFFFAOYSA-L strontium dihydroxide Chemical compound [OH-].[OH-].[Sr+2] UUCCCPNEFXQJEL-UHFFFAOYSA-L 0.000 description 1
- 229910001866 strontium hydroxide Inorganic materials 0.000 description 1
- DHEQXMRUPNDRPG-UHFFFAOYSA-N strontium nitrate Chemical compound [Sr+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O DHEQXMRUPNDRPG-UHFFFAOYSA-N 0.000 description 1
- 229910052917 strontium silicate Inorganic materials 0.000 description 1
- RXSHXLOMRZJCLB-UHFFFAOYSA-L strontium;diacetate Chemical compound [Sr+2].CC([O-])=O.CC([O-])=O RXSHXLOMRZJCLB-UHFFFAOYSA-L 0.000 description 1
- QSQXISIULMTHLV-UHFFFAOYSA-N strontium;dioxido(oxo)silane Chemical compound [Sr+2].[O-][Si]([O-])=O QSQXISIULMTHLV-UHFFFAOYSA-N 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 150000003462 sulfoxides Chemical class 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 1
- BGQMOFGZRJUORO-UHFFFAOYSA-M tetrapropylammonium bromide Chemical compound [Br-].CCC[N+](CCC)(CCC)CCC BGQMOFGZRJUORO-UHFFFAOYSA-M 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
Images
Classifications
-
- 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
- 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
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
- B01J35/31—Density
-
- 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
- B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
-
- 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
- B01J2229/186—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/42—Addition of matrix or binder particles
-
- 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
- B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
-
- 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
- B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
- B01J35/56—Foraminous structures having flow-through passages or channels, e.g. grids or three-dimensional monoliths
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/02—Boron or aluminium; Oxides or hydroxides thereof
- C07C2521/04—Alumina
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- C07C2521/08—Silica
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/16—Clays or other mineral silicates
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
-
- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- 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
-
- 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
- Y02P30/40—Ethylene production
Definitions
- the present invention relates to a catalyst for producing a lower olefin and a method for producing a lower olefin using the same. More specifically, the present invention relates to a catalyst having a high lower olefin selectivity and an excellent catalyst life, which is used when producing a lower olefin such as propylene from an oxygen-containing compound such as dimethyl ether, and a method for producing a lower olefin using the same.
- a catalyst having a high lower olefin selectivity and an excellent catalyst life which is used when producing a lower olefin such as propylene from an oxygen-containing compound such as dimethyl ether, and a method for producing a lower olefin using the same.
- Patent Document 1 a technique of diluting a raw material with a gas inert to the reaction is known (Patent Document 1).
- a catalyst having a high yield of lower hydrocarbons synthesized from dimethyl ether and / or methanol has a Si / Al atomic ratio of 30 to 400 and an alkaline earth metal / Al atomic ratio of 0.1.
- An alkaline earth metal-containing MFI zeolite catalyst having an average particle diameter of 75 to 15 and an average particle diameter of 0.05 to 2 ⁇ m has been proposed (Patent Document 2).
- Patent Document 3 discloses that a proton having an MFI structure is used as a catalyst that hardly causes elimination of aluminum from a zeolite skeleton and has a long catalyst life when used as a catalyst for producing a lower hydrocarbon from dimethyl ether and / or methanol.
- a zeolite catalyst which is a composite of a type zeolite or an ammonium type zeolite, an alkaline earth metal compound and a specific binder component.
- Patent Document 5 discloses a pentasil type having a primary particle diameter of 0.01 to 0.1 ⁇ m as a catalyst having good selectivity and catalyst life when used as a catalyst for producing olefins by contacting methanol as a catalyst.
- a zeolite catalyst obtained by molding aluminosilicate with aluminum oxide has been proposed.
- An object of the present invention is to provide a catalyst for producing a lower olefin, which is excellent in production efficiency of the lower olefin and maintains the activity for a long period of time, and a method for producing the lower olefin, in producing the lower olefin from the oxygen-containing compound. Yes.
- the catalyst for producing a lower olefin of the present invention is a solid catalyst used for producing a lower olefin from an oxygen-containing compound,
- a solid catalyst component containing an MFI structure zeolite Of all the positions inside the structure of the solid catalyst, the thickness indicated by the double distance of the shortest distance at the position where the shortest distance to the outer surface is maximum is 0.1 mm or more and 2.0 mm or less,
- the catalyst is characterized by having a CBD (Compacted Bulk Density) of 800 kg / m 3 or less.
- Such a catalyst for producing a lower olefin of the present invention comprises: A solid catalyst component containing an MFI structure zeolite; It is preferably obtained by molding a mixture containing one or more binders selected from the group consisting of oxides or hydroxides of aluminum or silicon and clay.
- the catalyst for producing a lower olefin of the present invention is preferably a catalyst used for producing a lower olefin from dimethyl ether and / or methanol.
- the solid catalyst component preferably contains an alkaline earth metal, and the solid catalyst component contains the alkaline earth metal component as a metal with respect to 100 parts by weight of the MFI structure zeolite. More preferably, the content is 0.3 to 10 parts by weight.
- the alkaline earth metal is preferably calcium.
- the catalyst for producing a lower olefin of the present invention preferably has a CBD (Compacted Bulk Density) of 800 kg / m 3 or less.
- the catalyst for producing a lower olefin of the present invention preferably has a honeycomb shape.
- the atomic ratio Si / Al in the zeolite framework of the MFI structure zeolite is preferably in the range of 10 to 2,000.
- the method for producing a catalyst for producing a lower olefin of the present invention is a method for producing a catalyst for use in producing a lower olefin from an oxygen-containing compound, A solid catalyst component containing an MFI structure zeolite; One or more binders selected from the group consisting of oxides or hydroxides of aluminum or silicon, and clay, Mixing and kneading in the presence of a polar solvent to obtain a mixture; Forming and firing the mixture, Of all the positions in the solid catalyst component, the thickness indicated by the double distance of the shortest distance at the position where the shortest distance to the outer surface is maximum is 0.1 mm or more and 2.0 mm or less, and A catalyst having a CBD of 800 kg / m 3 or less is obtained.
- the method for producing a lower olefin of the present invention is characterized by comprising a step of bringing an oxygen-containing compound and the above-mentioned catalyst for producing a lower olefin of the present invention into contact in a reactor filled with the catalyst.
- the method for producing a lower olefin according to the present invention comprises reacting an oxygen-containing compound and the catalyst for producing the lower olefin at a reactor outlet temperature of 500 ° C. or higher and 650 ° C. or lower in a reactor filled with the catalyst. It has the process of making it contact in vessel inlet pressure 0.12MPa or more and 1.0MPa or less.
- the oxygen-containing compound preferably contains dimethyl ether and / or methanol, and the catalyst packing density in the reactor is preferably 800 kg / m 3 or less.
- the catalyst life is long, the number of times of catalyst regeneration can be reduced, the cost for catalyst replacement and regeneration can be reduced, and an efficient method for producing a lower olefin with reduced catalyst filling amount Can be provided.
- the catalyst packing density in the reactor can be reduced, the length / diameter ratio of the reactor can be increased.
- FIG. 1 is a diagram illustrating the thickness when the catalyst shape is cylindrical or spherical.
- FIG. 2 is a diagram illustrating the thickness when the catalyst shape is a ring shape, a honeycomb shape, or a four-leaf shape.
- FIG. 3 shows the change over time of the raw material conversion rates of the catalysts A, B, C, and F obtained in Examples and Comparative Examples.
- the catalyst for producing a lower olefin according to the present invention is a solid catalyst used when producing a lower olefin from an oxygen-containing compound, and includes a solid catalyst component containing an MFI structure zeolite.
- Examples of the MFI structure zeolite constituting the catalyst for producing a lower olefin of the present invention include proton type zeolite and / or ammonium type zeolite.
- the MFI structure zeolite used in the present invention desirably has a Si / Al molar ratio of preferably 10 to 2000, more preferably 50 to 1000.
- the Si / Al molar ratio is less than 10, the effective acid sites of the zeolite are excessive, and the carbonaceous precipitation on the catalyst surface is promoted, which may shorten the catalyst life.
- the Si / Al molar ratio exceeds 2000, the effective acid point of the zeolite becomes too small, and the catalytic activity may be lowered.
- the catalyst for producing a lower olefin of the present invention preferably contains an alkaline earth metal or a compound (alkaline earth metal component) such as an oxide or hydroxide thereof.
- the content of the alkaline earth metal or a compound thereof is preferably about 0.3 to 10 parts by weight, more preferably about 0.5 to 5 parts by weight, based on 100 parts by weight of the MFI structure zeolite, in terms of metal.
- the alkaline earth metal is contained in the above range, the control of the acid property of the catalyst and the effect of suppressing dealumination can be sufficiently obtained.
- the alkaline earth metal contained in the catalyst is preferably calcium.
- the catalyst for producing a lower olefin of the present invention has a thickness indicated by a distance twice as long as the shortest distance at a position where the shortest distance to the outer surface is the maximum among all the positions inside the solid catalyst component. .1 mm or more and 2.0 mm or less, preferably 0.1 mm or more and 1.8 mm or less.
- the solid catalyst only needs to satisfy the above thickness, and the shape is not particularly limited.
- the shape is spherical, prismatic, columnar, cylindrical, ring-shaped, rectangular tube-shaped, cylinder-shaped, wheel, etc.
- Any shape such as a mold, a disk shape, a square plate shape, a wave shape, a structure with irregularities on the surface, a honeycomb shape, a cross-section three-leaf shape, a cross-section four-leaf shape may be used.
- a bulky shape is preferable, a four-leaf shape is preferable, a structure having a void inside and a hollow type are preferable, and a honeycomb shape is also preferable.
- the thickness of the catalyst for producing a lower olefin of the present invention is twice the shortest distance at the position where the shortest distance to the outer surface is maximum among all the positions inside the solid catalyst structure.
- this thickness d is specifically calculated
- the thickness d is T if T ⁇ L. If T> L, the thickness d corresponds to L. In the case of a honeycomb having prismatic cavities in the height direction in a prism of height L, and the shortest distance between the cavities is T (see FIG. 2), the thickness d is T if T ⁇ L. If L ⁇ T, the thickness d corresponds to L. In the case of a rectangular parallelepiped, the thickness d corresponds to the length of the shortest side. When the height L is a four-leaf type having a diagonal outer diameter D and the length between the diagonal recesses is T (see FIG. 2), the thickness d is T if T ⁇ L. If L ⁇ T, the thickness d corresponds to L.
- Such a catalyst for producing a lower olefin of the present invention has a CBD (Compacted Bulk Density) of 800 kg / m 3 or less, further 700 kg / m 3 or less, preferably 670 kg / m 3 or less, more preferably 650 kg / m. It is desirable that it is 3 or less, more preferably 200 to 650 kg / m 3 .
- the catalyst packing density in the reactor is usually 800 kg / m 3 or less, further 700 kg / m 3 or less, preferably 670 kg / m 3 or less, more preferably 650 kg.
- CBD is a bulk density when a sample is dispersed and placed in a container, and then the container is subjected to an impact by tapping and the volume of the sample is not changed.
- the catalyst for producing a lower olefin of the present invention has a low CBD of 800 kg / m 3 or less, it is easy to reduce the catalyst packing density when the catalyst is charged into the reactor. It becomes a low pressure loss type catalyst that can easily reduce pressure loss. Thus, when the pressure loss is low, the size can be reduced, the reactor can be easily designed and manufactured, and the construction cost can be reduced.
- the CBD of the lower olefin production catalyst can be easily controlled by selecting the catalyst shape.
- the catalyst in a low CBD of 800 kg / m 3 or less, the catalyst has a general shape that is not complicated and has a small thickness. The catalyst can be designed.
- CBD when CBD is smaller than 200 kg / m 3, there are disadvantages that the reactor size is increased and the production cost is increased.
- the lower olefin production catalyst of the present invention having the thickness as described above may be produced directly from the precursor of the MFI structure zeolite, and the MFI structure zeolite such as a powder is formed with a binder or a solvent as necessary. May be manufactured.
- the catalyst for producing a lower olefin according to the present invention is prepared by preparing a mixture containing a solid catalyst component containing an MFI structure zeolite and a binder, and molding the mixture.
- the catalyst for producing a lower olefin of the present invention contains an alkaline earth metal or a compound thereof, the alkaline earth metal component may be contained in the solid catalyst component, or may be added together with the binder, It is preferably contained in the solid catalyst component.
- the solid catalyst component containing the alkaline earth metal component may be produced by mixing an alkaline earth metal or a compound thereof with a precursor of the MFI structure zeolite and calcining. You may manufacture by impregnating or mixing the compound.
- Examples of the alkaline earth metal compound used in the production of the catalyst for producing the lower olefin of the present invention include magnesium carbonate (MgCO 3 ), magnesium hydroxide (Mg (OH) 2 ), magnesium oxide (MgO), and acetic acid.
- calcium compounds are preferred in the present invention.
- Calcium nitrate (Ca (NO 3 ) 2 ), calcium aluminate (CaAl 2 O 4 ), calcium orthosilicate (Ca 2 SiO 4 ) and the like are used.
- a solid catalyst component containing an alkaline earth metal component is produced by mixing an alkaline earth metal or a compound thereof with a precursor of an MFI structure zeolite and calcining, specifically, for example, as follows: Can be manufactured. First, 100 mol parts of SiO 2 source, 0.2 to 4.0 mol parts of metal oxide source, 2 to 1000 mol parts of alkali metal ion source, and 2.0 to 200 mol parts of skeletal structure adjustment 1 to 60% by mass of the amount of zeolite produced when a zeolite raw material solution containing an agent is dissolved in water and synthesized without adding 0.1 to 60 mol parts of an alkaline earth metal salt and seed crystals Coexist with the zeolite seed crystal in an amount corresponding to By this mixing step, the mixed liquid containing the zeolite raw material liquid, the alkaline earth metal salt, and the zeolite seed crystal becomes an aqueous gel mixture.
- this aqueous gel mixture is transferred to a container and hydrothermally synthesized by heating and stirring at 60 to 250 ° C. for 1 to 200 hours under self-pressure.
- the hydrothermally synthesized reaction product is separated by filtration or centrifugation, washed with water, dried, and calcined at 300 to 700 ° C. for 1 to 100 hours.
- a solid catalyst component which is an alkaline earth metal-containing MFI zeolite is prepared.
- alkaline earth metal-containing MFI structure zeolite is in a proton type
- an inorganic acid such as hydrochloric acid, sulfuric acid or nitric acid, or an organic acid such as formic acid or acetic acid is used.
- hydrochloric acid is preferable.
- the ion exchange to the ammonium type can be carried out in an aqueous solution of an ammonium salt such as ammonium water, ammonium chloride, ammonium nitrate, or ammonium sulfate.
- the catalyst for producing a lower olefin according to the present invention has a shape having the above-described thickness, but such a catalyst shape may be imparted when producing an MFI-type zeolite, or a powdery MFI-type zeolite. You may shape
- a mixture containing the solid catalyst component and a binder can be prepared and molded to produce the mixture.
- the catalyst for producing a lower olefin contains an alkaline earth metal component
- the alkaline earth metal or a compound thereof may be contained in the solid catalyst component or used together with a binder.
- the alkaline earth metal or the compound thereof is about 0.3 to 10 parts by weight, more preferably about 0.5 to 5 parts by weight with respect to 100 parts by weight of the MFI structure zeolite in terms of alkaline earth metal. It is desirable to be in the range.
- the binder one or more selected from the group consisting of oxides or hydroxides of aluminum or silicon and clay are preferably used.
- the amount of the binder used is not particularly limited, but is used in the range of 200 parts by weight or less, preferably 10 to 50 parts by weight, more preferably 15 to 30 parts by weight with respect to 100 parts by weight of the solid catalyst component. Is desirable.
- the solvent is preferably a polar solvent.
- polar solvent polar substances such as water, alcohols such as methanol, ethanol and propanol, ethers such as diethyl ether and tetrahydrofuran, esters, nitriles, amides and sulfoxides are used.
- An organic solvent can also be used. Of these polar solvents, water is preferred.
- an organic acid such as acetic acid or ammonia water which is removed during drying and baking may be added.
- the amount of the polar solvent used is not particularly limited as long as the mixture has moldability, but usually 10 to 150 parts by weight with respect to 100 parts by weight of the total components other than the polar solvent It can be a range.
- the mixture can be prepared by mixing these components and kneading as necessary.
- the obtained mixture is molded into a predetermined shape to obtain a molded body.
- the molding method include extrusion molding using an extruder and spherical body molding using a malmerizer.
- a slurry containing a solid catalyst to a substrate having a shape such as a honeycomb by a dipping method or a coating method, a desired catalyst shape having a thickness of 0.1 mm to 2.0 mm can be obtained. Good.
- the obtained molded body can be dried as necessary, and then fired to obtain a catalyst for producing a lower olefin.
- the molded body can be dried, for example, at 80 ° C. or higher and 150 ° C. or lower for 0.5 hour or longer and 30 hours or shorter.
- baking of the molded object after drying as needed can be performed at 350 degreeC or more and 750 degrees C or less, for 1 hour or more and 50 hours or less conditions, for example.
- the catalyst for producing a lower olefin according to the present invention is a solid catalyst used for producing a lower olefin from an oxygen-containing compound, and is preferably used for producing a lower olefin from dimethyl ether and / or methanol.
- the method for producing a lower olefin of the present invention is carried out using the above-described catalyst for producing a lower olefin of the present invention. That is, in the present invention, a lower olefin is produced by reacting an oxygen-containing compound as a raw material with a catalyst for producing a lower olefin in a reactor filled with the catalyst for producing a lower olefin according to the present invention. can do.
- the catalytic reaction method include a fixed bed reaction method and a fluidized bed reaction method.
- oxygen-containing compound used as a raw material examples include alcohols and ethers having 1 to 10 carbon atoms such as dimethyl ether, methanol, diethyl ether, ethanol, propanol, and butanol, dimethyl carbonate, formaldehyde, and acetone.
- alcohols and ethers having 1 to 10 carbon atoms such as dimethyl ether, methanol, diethyl ether, ethanol, propanol, and butanol, dimethyl carbonate, formaldehyde, and acetone.
- dimethyl ether and / or methanol is preferably used.
- the reaction temperature and pressure conditions are not particularly limited.
- the reaction temperature ranges from 300 to 750 ° C.
- 400 to 650 ° C. is more preferable.
- a temperature lower than 300 ° C. is advantageous in terms of energy, but the catalyst activity is insufficient.
- the temperature exceeds 750 ° C. the coking speed is high, the deterioration is rapid, and the catalyst is altered (such as structural destruction).
- Dimethyl ether and / or methanol as a raw material can be diluted with water vapor, saturated hydrocarbon, inert gas or the like and supplied onto the catalyst.
- the unit catalyst mass and the weight-based space velocity (hereinafter referred to as “WHSV”) of the raw material gas supplied per unit time are referred to as dimethyl ether (hereinafter referred to as “DME”).
- DME dimethyl ether
- the equivalent mass is preferably 0.025 to 50 g-DME / (g-catalyst ⁇ hour).
- WHSV weight-based space velocity
- DME dimethyl ether
- a reactor outlet temperature of 500 to 650 ° C. and a reactor inlet pressure of 0.12 to 1.0 MPa it is preferable to operate at a reactor outlet temperature of 500 to 650 ° C. and a reactor inlet pressure of 0.12 to 1.0 MPa.
- the outlet temperature of the reactor is 500 to 650 ° C.
- the lower olefin can be obtained with a high yield.
- the reactor inlet pressure is 0.12 to 1.0 MPa, the production rate of the lower olefin can be increased.
- the packing density of the lower olefin production catalyst in the reactor is usually 800 kg / m 3 or less, preferably 700 kg / m 3 or less, more preferably 670 kg / m 3 or less, and further preferably 650 kg / m 3 or less. Particularly preferably, it is desirable to be 200 to 650 kg / m 3 . If the catalyst packing density is in such a range, it is easy to reduce the pressure loss in the reactor, the reactor can be designed at a low reaction pressure, and the thickness of the catalyst layer is reduced even in a commercial plant with a large amount of raw material supply. The reaction can be carried out with low pressure loss. For this reason, it is possible to avoid problems such as the dispersion of the raw material gas that occurs when a flat reactor having a reduced reactor length / diameter is used as the catalyst layer is made thinner.
- the thickness indicated by the double distance of the shortest distance at the position where the shortest distance to the outer surface is the maximum among all the positions inside the structure of the solid catalyst is 0.1 mm or more.
- the above-mentioned catalyst for producing a lower olefin of the present invention which is 2.0 mm or less, preferably 0.1 mm or more and 1.8 mm or less is used.
- the catalyst can have sufficient strength to withstand practical use.
- the activity fall by precipitation of carbonaceous matter can be suppressed by using the catalyst for lower olefin manufacture whose thickness of a solid catalyst is 2.0 mm or less.
- the pressure loss can be reduced, but the deposition of carbonaceous material on the surface of the catalyst will increase, resulting in an early decrease in activity, and a catalyst life commensurate with the packed catalyst weight will not be obtained. This is not preferable.
- the reaction apparatus used for the reaction is not particularly limited, and the reactor may be provided alone, or a plurality of reactors may be provided in series or in parallel.
- the catalyst for producing a lower olefin of the present invention by using the catalyst for producing a lower olefin of the present invention, it is possible to synthesize the lower olefin from the oxygen-containing compound raw material in a high yield, improve the reaction efficiency, and further to the catalyst deactivation. It is possible to provide a method for producing a lower olefin that takes a long time and can reduce the cost of catalyst regeneration.
- an oxygen-containing compound introduced as a raw material gas such as dimethyl ether and / or methanol
- conversion of reaction components It is desirable that the rate is 95% or more, preferably 99% or more, and more preferably 99.9% or more.
- the conversion rate can be obtained by the following equation. In Examples to be described later, the conversion rate is obtained by the following formula.
- the reaction component means the total of oxygen-containing compounds (for example, the total of dimethyl ether and methanol), and the supply speed and the outlet speed mean the speed based on carbon.
- the time when the predetermined conversion rate cannot be achieved can be treated as the catalyst life.
- Example 1 (Production of catalyst A) 9.50 g of A1 (NO 3 ) 3 .9H 2 O and 10.92 g of Ca (CH 3 COO) 2 .H 2 O were dissolved in 750 g of water, and 500 g of cataloid Si— was added to 333 g of water.
- this aqueous gel mixture was put into a 3 L autoclave container, and hydrothermal synthesis was performed by stirring at 160 ° C. for 18 hours under self-pressure.
- the white solid product produced by hydrothermal synthesis was filtered and washed with water, dried at 120 ° C. for 5 hours, and calcined in air at 520 ° C. for 10 hours.
- the calcined product was immersed in 0.6N hydrochloric acid and stirred at room temperature for 24 hours to make the zeolite type proton type.
- the product was filtered, washed with water, dried at 120 ° C. for 5 hours, and calcined in air at 520 ° C. for 10 hours to obtain a proton-type alkaline earth metal-containing MFI zeolite solid catalyst component.
- the atomic ratio Si / Al of Si and Al at the time of raw material charging is 100
- the atomic ratio Ca / Al of Ca and Al is 2.5
- the atomic ratio Si / Al in the synthesized zeolite solid catalyst component is 100
- the atomic ratio Ca / Al was 3.7.
- each atomic ratio at the time of raw material preparation was calculated
- each atomic ratio after synthesis was determined by measuring with a fluorescent X-ray analyzer.
- the average particle diameter of the obtained zeolite solid catalyst component was measured by a scanning electron microscope and the specific surface area was measured by the BET adsorption method, the average particle diameter of the catalyst was 1.5 ⁇ m and the specific surface area was 320 m 2 / g. It was.
- boehmite 28 g was mixed with 100 g of the obtained powdered zeolite solid catalyst component, and an appropriate amount of ion-exchanged water was added and kneaded. This mixture was formed into cylindrical pellets having a diameter of 1.8 mm ⁇ and an average length of 4.2 mm by an extruder.
- the molded body obtained by extrusion molding was dried at 120 ° C. and then air calcined at 550 ° C. for 12 hours to obtain Catalyst A.
- the obtained catalyst A retained the shape formed by extrusion molding, and the thickness was 1.8 mm.
- Example 1 (Production of catalyst B)
- Catalyst B was produced in the same manner as in Example 1 except that it was formed into a cylindrical pellet having a diameter of 3.6 mm ⁇ and an average length of 5.9 mm by molding with an extruder.
- the obtained catalyst B retained the shape formed by extrusion molding, and the thickness was 3.6 mm.
- Example 2 (Production of Catalyst C)
- Catalyst C was produced in the same manner as in Example 1 except that it was molded into a cylindrical pellet having a diameter of 5.0 mm ⁇ and an average length of 5.4 mm in molding by an extruder.
- the obtained catalyst C retained the shape formed by extrusion molding, and the thickness was 5.0 mm.
- Example 2 (Production of catalyst D)
- a catalyst was formed in the same manner as in Example 1 except that it was molded into a ring-shaped pellet having an outer diameter of 5.0 mm ⁇ , an inner diameter of 2.0 mm ⁇ , and an average length of 7.8 mm. D was produced. The obtained catalyst D retained the shape formed by extrusion molding, and the thickness was 1.5 mm.
- Example 3 (Production of catalyst E) Catalyst C obtained in Comparative Example 2 was pulverized in a mortar and passed through a sieve having an opening of 0.50 mm to 0.59 mm to produce Catalyst E. The thickness of this catalyst is 0.59 mm or less.
- Example 4 (Production of catalyst F)
- the catalyst F was produced in the same manner as in Example 1 except that the thickness was 1.3 mm and the hole diameter was 1.0 mm in the extrusion molding machine, and the honeycomb shape was 75 mm square. did.
- the obtained catalyst F retained the shape formed by extrusion molding, and the thickness was 1.3 mm.
- Example 5 (Production of catalyst G) 100 g of the zeolite solid catalyst component obtained in the same manner as in Example 1 and 28 g of boehmite were mixed and kneaded with an appropriate amount of ion-exchanged water to obtain a mixture. This mixture was coated on a honeycomb-shaped silica carrier 106g having a thickness of 0.2 mm, a pore diameter of 2.0 mm, and an average length of 24.0 mm, and dried and fired in the same manner as in Example 1 to obtain a honeycomb-type catalyst. G was obtained. The thickness of the obtained catalyst G was 0.3 mm.
- Example 5b (Production of catalyst H)
- Example 6 (Production of lower olefin) A mixed gas comprising a mixture of methanol (0.9 NL / min), dimethyl ether (1.9 NL / min) and water (1.9 NL / min) and nitrogen as a diluent gas (11.1 NL / min), The lower olefin production reaction was carried out continuously by feeding to the fixed bed flow reactor filled with the catalyst A obtained in Example 1.
- Table 1 shows the characteristics of the catalyst used (catalyst thickness, CBD, catalyst shape and catalyst diameter) and catalyst packing density in the reactor.
- the reaction conditions were WHSV (DME) of 1.0 h ⁇ 1 , reactor inlet pressure of 0.5 MPa, and reactor inlet temperature of 400 ° C.
- the weight space velocity (WHSV (DME)) is the supply weight of the reaction component (total of dimethyl ether and methanol) converted to dimethyl ether per unit time (h) and unit catalyst weight (g-cat). DME), the unit is h ⁇ 1 .
- the reaction was continuously carried out under the above conditions, and the composition of the gas at the outlet of the reactor was analyzed to determine the conversion rate of the raw material.
- the catalyst life referred to here is the total amount of dimethyl ether supplied per gram of catalyst weight up to that time when the conversion rate of the raw material determined from the outlet gas composition was less than 99.9% on the basis of dimethyl ether. Defined as a scale.
- the catalyst life determined in this example is expressed as relative catalyst life 100. In other examples, it was obtained by proportional calculation.
- Example 6 a lower olefin was produced in the same manner as in Example 6 except that instead of the catalyst A, the catalyst B obtained in Comparative Example 1 was used. The results are shown in Table 1.
- Example 6 a lower olefin was produced in the same manner as in Example 6 except that instead of the catalyst A, the catalyst C obtained in Comparative Example 2 was used. The results are shown in Table 1.
- Example 7 In Example 6, a lower olefin was produced in the same manner as in Example 6 except that instead of the catalyst A, the catalyst D obtained in Example 2 was used. The results are shown in Table 1.
- Example 8 A mixed gas composed of dimethyl ether (20 Ncc / min) and nitrogen as a diluent gas (20 Ncc / min) was continuously supplied to the fixed bed flow reactor filled with catalyst E obtained in Example 3. The lower olefin production reaction was carried out. Table 1 shows the characteristics of the catalyst used (catalyst thickness, CBD, catalyst shape and catalyst diameter) and catalyst packing density in the reactor.
- reaction conditions were WHSV (DME) 10 h ⁇ 1 , reactor inlet pressure 0 MPa, and catalyst layer temperature 530 ° C.
- Example 9 In Example 6, the production of the lower olefin was conducted in the same manner as in Example 6 except that instead of the catalyst A, the catalyst F obtained in Example 4 was cut into a size that could be filled in the reaction tube. went. The results are shown in Table 1.
- Example 10 In Example 6, a lower olefin was produced in the same manner as in Example 6 except that instead of the catalyst A, the catalyst G obtained in Example 5 was used. The results are shown in Table 1.
- Example 11 In Example 9, a lower olefin was produced in the same manner as in Example 9, except that the reactor inlet pressure was 0.3 MPa. When the reaction was continuously performed, the reactor outlet temperature was 560 ° C. The results are shown in Table 1.
- Example 12 In Example 6, a lower olefin was produced in the same manner as in Example 6 except that instead of the catalyst A, the catalyst H obtained in Example 5b was used. The results are shown in Table 1.
- the relative catalyst life in Comparative Examples 3 and 4 and Examples 7 to 11 is a value expressed as a relative value when the catalyst life of Example 6 is 100.
- the catalyst A (Example 6) in which the ordinate represents the dimethyl ether conversion rate and the abscissa represents the amount of dimethyl ether supplied per gram of catalyst weight when the catalyst life of the catalyst A is 100.
- B (Comparative Example 3)
- C (Comparative Example 4)
- F (Example 9) shows the change over time of the raw material conversion.
- a catalyst having a large thickness also has a catalyst life equivalent to that of a catalyst having a small thickness by being reduced to a thickness of 2.0 mm or less by pulverization or the like.
- the thickness of the catalyst has a great influence on the life of the catalyst, but has little effect on the properties of the product, It can be seen that the physical shape of the catalyst such as the cylindrical pellet type, the ring-shaped pellet type, and the honeycomb type has little influence on the performance of the catalyst, but the influence of the size or thickness of the catalyst has a great influence.
- a catalyst having a long catalyst life and an economically economically low-olefin produced from a oxygen-containing compound such as dimethyl ether or methanol According to the catalyst for producing a lower olefin and the method for producing a lower olefin of the present invention, a catalyst having a long catalyst life and an economically economically low-olefin produced from a oxygen-containing compound such as dimethyl ether or methanol.
- a method for producing olefins can be provided.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Description
MFI構造ゼオライトを含有する固体状触媒成分を含み、
固体触媒の構成体内部のすべての位置のうち、外表面までの最短距離が最大となる位置における当該最短距離の2倍の距離で示される厚みが、0.1mm以上2.0mm以下であり、かつ触媒のCBD(Compacted Bulk Density)が800kg/m3以下であることを特徴としている。
MFI構造ゼオライトを含有する固体状触媒成分と、
アルミニウムまたはケイ素の、酸化物または水酸化物、および粘土よりなる群から選ばれる1種以上のバインダーとを含む混合体を成形して得られることが好ましい。
MFI構造ゼオライトを含有する固体状触媒成分と、
アルミニウムまたはケイ素の、酸化物または水酸化物、および粘土よりなる群から選ばれる1種以上のバインダーとを、
極性溶媒の存在下に混合・混練して、混合体を得る工程と、
該混合体を成形し、焼成する工程と
を有し、
固体触媒の構成体内部のすべての位置のうち、外表面までの最短距離が最大となる位置における当該最短距離の2倍の距離で示される厚みが0.1mm以上2.0mm以下であり、かつ触媒のCBDが800kg/m3以下である触媒を得ることを特徴としている。
本発明の低級オレフィンの製造方法は、含酸素化合物と、上記本発明の低級オレフィン製造用触媒とを、該触媒が充填された反応器内で接触させる工程を有することを特徴としている。
本発明に係る低級オレフィン製造用触媒は、含酸素化合物から低級オレフィンを製造する際に用いる固体触媒であって、MFI構造ゼオライトを含有する固体状触媒成分を含む。
・円の直径がDで長さがLである円柱状(図1参照)であれば、D<Lならば厚みdはDに相当し、D>Lならば厚みdはLに相当する。
・球の直径がRである球状(図1参照)であれば、厚みdはRに相当する。
・同心円の内径と外径とを有し、内径と外径との距離がTであり、長さがLであるリング状(図2参照)であれば、T<Lならば厚みdはTに相当し、T>Lならば厚みdはLに相当する。
・高さLの角柱内に高さ方向に角柱状の空洞を有するハニカム状で、空洞間の最短距離がTである場合(図2参照)であれば、T<Lならば厚みdはTに相当し、L<Tならば厚みdはLに相当する。
・直方体であれば厚みdは最短辺の長さに相当する。
・高さLで対角の外径Dである四つ葉型で、対角するくぼみ部間の長さがTである場合(図2参照)、T<Lであれば厚みdはTに相当し、L<Tであれば厚みdはLに相当する。
本発明において、CBDとは、試料を分散させて容器に入れた後、容器にタップによる衝撃を加え、試料の体積変化がなくなった時の嵩密度である。
本発明の低級オレフィン製造用触媒が、800kg/m3以下の低いCBDを有する場合には、触媒を反応器に充填した際の触媒充填密度を低いものとすることが容易で、反応器内の圧力損失を低減しやすい、低圧損失型の触媒となる。このように圧力損失が低い場合にはサイズの小型化が図られ、反応器の設計および製作が容易となり、建設コストが低減できる。また、低級オレフィン製造用触媒のCBDは、触媒形状を選択することにより容易に制御することができるが、800kg/m3以下の低いCBDにおいては、複雑とならない一般的形状の触媒で厚みの小さい触媒を設計できる。
一方、CBDが200kg/m3より小さくなると、反応器サイズが大型になる他、製造コストが高くなるという欠点がある。
本発明の低級オレフィンの製造方法は、上述した本発明の低級オレフィン製造用触媒を用いて行う。すなわち、本発明では、上記本発明に係る低級オレフィン製造用触媒が充填された反応器内で、原料である含酸素化合物を、低級オレフィン製造用触媒と接触させることにより反応させ、低級オレフィンを製造することができる。接触反応の方式としては、固定床反応方式、流動床反応方式などが挙げられる。
9.50gのA1(NO3)3・9H2Oと、10.92gのCa(CH3COO)2・H2Oを750gの水に溶かし、これに、水333g中に500gのキャタロイドSi-30水ガラス(触媒化成工業製)を溶かした溶液と、6質量%NaOH水溶液177.5gと、21.3質量%臭化テトラプロピルアンモニウム水溶液317.6gと、ゼオライト種結晶として平均粒子径0.5μmのアンモニウム型のMFI構造ゼオライト(Zeolyst社製、Si/Al原子比は70)15.0g(種結晶を添加せずに合成したゼオライト触媒量の10質量%に相当する量)とを攪拌しながら加えて、水性ゲル混合物を得た。
実施例1において、押出成形機での成形において、直径3.6mmφ、平均長さ5.9mmの円柱状ペレットに成形したことの他は、実施例1と同様にして触媒Bを製造した。得られた触媒Bは、押出成形で形成した形状を保持しており、厚みは3.6mmであった。
実施例1において、押出成形機での成形において、直径5.0mmφ、平均長さ5.4mmの円柱状ペレットに成形したことの他は、実施例1と同様にして触媒Cを製造した。得られた触媒Cは、押出成形で形成した形状を保持しており、厚みは5.0mmであった。
実施例1において、押出成形機での成形において、外径5.0mmφ、内径2.0mmφ、平均長さ7.8mmのリング状ペレットに成形したことの他は、実施例1と同様にして触媒Dを製造した。得られた触媒Dは、押出成形で形成した形状を保持しており、厚みは1.5mmであった。
比較例2で得た触媒Cを乳鉢で粉砕し、目開き0.50mm~0.59mmの篩にかけて、触媒Eを製造した。この触媒の厚さは0.59mm以下である。
実施例1において、押出成形機での成形において、厚みが1.3mm、孔径1.0mmであり、75mm四方のハニカム形状に成形したことの他は、実施例1と同様にして触媒Fを製造した。得られた触媒Fは、押出成形で形成した形状を保持しており、厚みは1.3mmであった。
実施例1と同様にして得たゼオライト固体触媒成分100gと、ベーマイト28gとを混合し、適当量のイオン交換水で混練して混合物を得た。この混合物を、厚み0.2mm、孔径2.0mmであり、平均長さ24.0mmのハニカム形状のシリカ担体106g上にコーティングし、実施例1と同様にして乾燥、焼成してハニカム型の触媒Gを得た。得られた触媒Gの厚みは0.3mmであった。
実施例1において、押出成形機での成形において、外径1.8mm、T=1.1mm、平均長さ7.7mmの四つ葉型ペレットに成形したこと以外は、実施例1と同様にして触媒Hを製造した。得られた触媒Hは、押出成形で形成した形状を保持しており、厚みは1.1mmであった。
メタノール(0.9NL/分)、ジメチルエーテル(1.9NL/分)および水(1.9NL/分)の混合物と、希釈ガスとしての窒素(11.1NL/分)とをからなる混合ガスを、実施例1で得た触媒Aを充填した固定床流通型反応器に連続的に供給して、低級オレフィン製造反応を行った。用いた触媒の特性(触媒厚み、CBD、触媒形状および触媒径)および、反応器内の触媒充填密度を表1に示す。
実施例6において、触媒Aに代えて、比較例1で得た触媒Bを用いたこと以外は、実施例6と同様にして低級オレフィンの製造を行った。結果を表1に示す。
実施例6において、触媒Aに代えて、比較例2で得た触媒Cを用いたこと以外は、実施例6と同様にして低級オレフィンの製造を行った。結果を表1に示す。
実施例6において、触媒Aに代えて、実施例2で得た触媒Dを用いたこと以外は、実施例6と同様にして低級オレフィンの製造を行った。結果を表1に示す。
ジメチルエーテル(20Ncc/分)と、希釈ガスとしての窒素(20Ncc/分)とをからなる混合ガスを、実施例3で得た触媒Eを充填した固定床流通型反応器に連続的に供給して、低級オレフィン製造反応を行った。用いた触媒の特性(触媒厚み、CBD、触媒形状および触媒径)および、反応器内の触媒充填密度を表1に示す。
実施例6において、触媒Aに代えて、実施例4で得た触媒Fを、反応管に充填できる大きさに切りだして用いたこと以外は、実施例6と同様にして低級オレフィンの製造を行った。結果を表1に示す。
実施例6において、触媒Aに代えて、実施例5で得た触媒Gを用いたこと以外は、実施例6と同様にして低級オレフィンの製造を行った。結果を表1に示す。
実施例9において、反応器入口圧力を0.3MPaとしたこと以外は、実施例9と同様にして低級オレフィンの製造を行った。連続的に反応を行ったところ、反応器出口温度は560℃であった。結果を表1に示す。
実施例6において、触媒Aに代えて、実施例5bで得た触媒Hを用いたこと以外は、実施例6と同様にして低級オレフィンの製造を行った。結果を表1に示す。
触媒の厚みが2.0mm以下である場合には、良好な触媒寿命を示すが、2.0mmを超えると、触媒の厚みに応じて触媒寿命が短くなる傾向が示されていること、
厚みの大きな触媒も、粉砕などにより2.0mm以下の厚みとすることで、厚みの小さい触媒と同等の触媒寿命を示すようになること、
触媒の厚みは触媒寿命に大きな影響を与えるが、生成物の性状に与える影響は少ないこと、
円柱状ペレット型、リング状ペレット型、ハニカム型などの触媒の物理的形状が、触媒の性能に与える影響は少ないが、触媒の大きさあるいは厚みが与える影響は大きいことなどがわかる。
Claims (12)
- 含酸素化合物から、低級オレフィンを製造する際に用いる固体触媒であって、
MFI構造ゼオライトを含有する固体状触媒成分を含み、
固体触媒の構成体内部のすべての位置のうち、外表面までの最短距離が最大となる位置における当該最短距離の2倍の距離で示される厚みが、0.1mm以上2.0mm以下であり、かつ触媒のCBD(Compacted Bulk Density)が800kg/m3以下であることを特徴とする低級オレフィン製造用触媒。 - MFI構造ゼオライトを含有する固体状触媒成分と、
アルミニウムまたはケイ素の、酸化物または水酸化物、および粘土よりなる群から選ばれる1種以上のバインダーとを含む混合体を成形して得られることを特徴とする請求項1に記載の低級オレフィン製造用触媒。 - ジメチルエーテルおよび/またはメタノールから、低級オレフィンを製造する際に用いる触媒であることを特徴とする請求項1または2に記載の低級オレフィン製造用触媒。
- 固体状触媒成分が、アルカリ土類金属を含有することを特徴とする請求項1~3のいずれかに記載の低級オレフィン製造用触媒。
- 固体状触媒成分が、アルカリ土類金属を、MFI構造ゼオライト100重量部に対して0.3~10重量部含有することを特徴とする請求項4に記載の低級オレフィン製造用触媒。
- アルカリ土類金属がカルシウムであることを特徴とする請求項4または5に記載の低級オレフィン製造用触媒。
- ハニカム形状であることを特徴とする請求項1~6のいずれかに記載の低級オレフィン製造用触媒。
- MFI構造ゼオライトの、ゼオライト骨格中のケイ素とアルミニウムの原子比Si/Alが10~2000の範囲であることを特徴とする請求項1~7のいずれかに記載の低級オレフィン製造用触媒。
- 含酸素化合物から低級オレフィンを製造する際に用いる触媒を製造する方法であって、
MFI構造ゼオライトを含有する固体状触媒成分と、
アルミニウムまたはケイ素の、酸化物または水酸化物、および粘土よりなる群から選ばれる1種以上のバインダーとを、
極性溶媒の存在下に混合・混練して、混合体を得る工程と、
該混合体を成形し、焼成する工程と
を有し、
固体触媒の構成体内部のすべての位置のうち、外表面までの最短距離が最大となる位置における当該最短距離の2倍の距離で示される厚みが0.1mm以上2.0mm以下であり、かつCBD(Compacted Bulk Density)が800kg/m3以下である触媒を得ることを特徴とする低級オレフィン製造用触媒の製造方法。 - 含酸素化合物と、請求項1~8のいずれかに記載の低級オレフィン製造用触媒とを、該触媒が充填された反応器内で、反応器出口温度500℃以上650℃以下で、かつ反応器入口圧力が0.12MPa以上1.0MPa以下で接触させる工程を有することを特徴とする低級オレフィンの製造方法。
- 含酸素化合物がジメチルエーテルおよび/またはメタノールを含有することを特徴とする請求項10に記載の低級オレフィンの製造方法。
- 反応器内の触媒充填密度が800kg/m3以下であることを特徴とする請求項10または11に記載の低級オレフィンの製造方法。
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP10791994.6A EP2446964A4 (en) | 2009-06-22 | 2010-06-14 | CATALYST FOR THE PRODUCTION OF LOWER OLEFINS AND PROCESS FOR PRODUCING LOWER OLEFINS USING SAID CATALYST |
CN2010800272222A CN102802792A (zh) | 2009-06-22 | 2010-06-14 | 低级烯烃制造用催化剂及使用其制造低级烯烃的方法 |
EA201270055A EA021772B1 (ru) | 2009-06-22 | 2010-06-14 | Катализатор для получения низших олефинов и способ получения низших олефинов с его использованием |
JP2011519771A JP5744730B2 (ja) | 2009-06-22 | 2010-06-14 | 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 |
US13/333,383 US9382169B2 (en) | 2009-06-22 | 2011-12-21 | Lower olefins producing catalyst and method for producing lower olefins using same |
ZA2012/00486A ZA201200486B (en) | 2009-06-22 | 2012-01-20 | Lower olefins producing catalyst and method for producing lower olefins using same |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2009147805 | 2009-06-22 | ||
JP2009-147805 | 2009-06-22 |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US13/333,383 Continuation US9382169B2 (en) | 2009-06-22 | 2011-12-21 | Lower olefins producing catalyst and method for producing lower olefins using same |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2010150676A1 true WO2010150676A1 (ja) | 2010-12-29 |
Family
ID=43386447
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2010/060035 WO2010150676A1 (ja) | 2009-06-22 | 2010-06-14 | 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 |
Country Status (7)
Country | Link |
---|---|
US (1) | US9382169B2 (ja) |
EP (1) | EP2446964A4 (ja) |
JP (1) | JP5744730B2 (ja) |
CN (1) | CN102802792A (ja) |
EA (1) | EA021772B1 (ja) |
WO (1) | WO2010150676A1 (ja) |
ZA (1) | ZA201200486B (ja) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2015526401A (ja) * | 2012-06-29 | 2015-09-10 | ビーエーエスエフ ソシエタス・ヨーロピアBasf Se | 酸素含有物質からオレフィンへの転化のための方法 |
US10213773B2 (en) | 2012-06-29 | 2019-02-26 | Basf Se | Process for the conversion of oxygenates to olefins |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US10005702B2 (en) | 2012-06-29 | 2018-06-26 | Basf Se | Catalyst coating and process for the conversion of oxygenates to olefins |
JP6466325B2 (ja) * | 2012-06-29 | 2019-02-06 | ビーエーエスエフ ソシエタス・ヨーロピアBasf Se | 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 |
CN104689846A (zh) * | 2013-12-09 | 2015-06-10 | 中国科学院大连化学物理研究所 | 一种调整含氧化合物制芳烃过程产物组成的催化剂及应用 |
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 |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS57197228A (en) | 1981-05-13 | 1982-12-03 | Hoechst Ag | Olefin manufacture |
JP2004181454A (ja) | 2002-12-01 | 2004-07-02 | Sued-Chemie Ag | 結晶アルモシリケートに基づく触媒 |
JP2005138000A (ja) | 2003-11-05 | 2005-06-02 | Jgc Corp | 触媒及び該触媒の調製方法並びに該触媒を用いた低級炭化水素の製造方法 |
JP2005314339A (ja) | 2004-04-30 | 2005-11-10 | Maruzen Petrochem Co Ltd | 低級オレフィンの製造法 |
JP2008074764A (ja) * | 2006-09-21 | 2008-04-03 | Mitsubishi Chemicals Corp | プロピレンの製造方法 |
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 |
JP2008513448A (ja) * | 2004-09-16 | 2008-05-01 | ユーオーピー エルエルシー | 移動床技術及びエーテル化工程を利用したアルコール性オキシジェネートのプロピレンへの転化 |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4801567A (en) * | 1981-06-19 | 1989-01-31 | Union Oil Company Of California | Oxidation catalyst |
US4564603A (en) * | 1981-12-07 | 1986-01-14 | Union Oil Company Of California | Oxidative-dehydrogenation catalyst and process |
US6046373A (en) * | 1998-04-29 | 2000-04-04 | Exxon Chemical Patents Inc. | Catalytic conversion of oxygenates to olefins |
EP1396481A1 (en) * | 2002-08-14 | 2004-03-10 | ATOFINA Research | Production of olefins |
US20040064008A1 (en) * | 2002-09-30 | 2004-04-01 | Torsten Maurer | Molecular sieve catalyst composition |
US7192900B2 (en) * | 2002-11-27 | 2007-03-20 | Shell Oil Company | Hydrocracking catalyst |
WO2004058400A1 (en) * | 2002-12-27 | 2004-07-15 | Council Of Scientific And Industrial Research | PROCESS FOR PRODUCTION OF HIGH OCTANE GASOLINE FROM STRAIGHT RUN LIGHT NAPHTHA ON Pt CONTAINING HZSM - 5 MOLECULAR SIEVE CATALYST |
US7312369B2 (en) * | 2004-04-28 | 2007-12-25 | Exxonmobil Chemical Patents Inc. | Attrition resistant molecular sieve catalyst, method of making and process for using |
JP4631609B2 (ja) * | 2005-08-29 | 2011-02-16 | セイコーエプソン株式会社 | 機能膜の形成方法、有機el表示パネルの製造方法、液晶表示パネルの製造方法、プラズマディスプレイパネルの製造方法、カラーフィルタの製造方法 |
TWI406707B (zh) * | 2006-08-30 | 2013-09-01 | Jgc Corp | 含鹼土類金屬化合物之沸石催化劑及其調製方法與再生方法、以及低級烴之製造方法 |
US7825204B2 (en) * | 2006-12-19 | 2010-11-02 | Lyondell Chemical Technology, L.P. | Inorganic oxide extrudates |
-
2010
- 2010-06-14 WO PCT/JP2010/060035 patent/WO2010150676A1/ja active Application Filing
- 2010-06-14 EP EP10791994.6A patent/EP2446964A4/en not_active Withdrawn
- 2010-06-14 JP JP2011519771A patent/JP5744730B2/ja active Active
- 2010-06-14 EA EA201270055A patent/EA021772B1/ru not_active IP Right Cessation
- 2010-06-14 CN CN2010800272222A patent/CN102802792A/zh active Pending
-
2011
- 2011-12-21 US US13/333,383 patent/US9382169B2/en active Active
-
2012
- 2012-01-20 ZA ZA2012/00486A patent/ZA201200486B/en unknown
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS57197228A (en) | 1981-05-13 | 1982-12-03 | Hoechst Ag | Olefin manufacture |
JP2004181454A (ja) | 2002-12-01 | 2004-07-02 | Sued-Chemie Ag | 結晶アルモシリケートに基づく触媒 |
JP2005138000A (ja) | 2003-11-05 | 2005-06-02 | Jgc Corp | 触媒及び該触媒の調製方法並びに該触媒を用いた低級炭化水素の製造方法 |
JP2005314339A (ja) | 2004-04-30 | 2005-11-10 | Maruzen Petrochem Co Ltd | 低級オレフィンの製造法 |
JP2008513448A (ja) * | 2004-09-16 | 2008-05-01 | ユーオーピー エルエルシー | 移動床技術及びエーテル化工程を利用したアルコール性オキシジェネートのプロピレンへの転化 |
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 |
JP2008074764A (ja) * | 2006-09-21 | 2008-04-03 | Mitsubishi Chemicals Corp | プロピレンの製造方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP2446964A4 |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2015526401A (ja) * | 2012-06-29 | 2015-09-10 | ビーエーエスエフ ソシエタス・ヨーロピアBasf Se | 酸素含有物質からオレフィンへの転化のための方法 |
US10213773B2 (en) | 2012-06-29 | 2019-02-26 | Basf Se | Process for the conversion of oxygenates to olefins |
Also Published As
Publication number | Publication date |
---|---|
CN102802792A (zh) | 2012-11-28 |
JPWO2010150676A1 (ja) | 2012-12-10 |
EA201270055A1 (ru) | 2012-05-30 |
EP2446964A4 (en) | 2015-04-29 |
ZA201200486B (en) | 2013-04-24 |
JP5744730B2 (ja) | 2015-07-08 |
US9382169B2 (en) | 2016-07-05 |
US20120116143A1 (en) | 2012-05-10 |
EP2446964A1 (en) | 2012-05-02 |
EA021772B1 (ru) | 2015-08-31 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US9242236B2 (en) | Catalytic composition for producing olefins by catalytic cracking | |
JP5744730B2 (ja) | 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 | |
US8680356B2 (en) | Catalyst and process for preparing isoolefins | |
KR102171666B1 (ko) | 제올라이트계 물질의 제조 및 옥시게네이트의 올레핀으로의 전환 공정을 위한 용도 | |
US9861969B2 (en) | Binderless molecular sieve catalyst and a preparation method thereof | |
US10786807B2 (en) | ZSM-5 catalyst | |
JP6053366B2 (ja) | ゼオライト触媒、ゼオライト触媒の製造方法および低級オレフィンの製造方法 | |
WO2011013780A1 (ja) | プロピレンの製造方法及びプロピレン製造用触媒 | |
JP2011121859A (ja) | アルミノシリケートの製造方法 | |
JP5050466B2 (ja) | プロピレンの製造方法 | |
JP2011102209A (ja) | アルミノシリケートの製造方法 | |
CA2891248C (en) | Process for the conversion of oxygenates to olefins | |
JP2007516078A (ja) | 炭化水素クラッキング触媒及びその製造方法 | |
US9636668B2 (en) | Production and use of a zeolitic material in a process for the conversion of oxygenates to olefins | |
US9598326B2 (en) | Process for the conversion of oxygenates to olefins | |
Yang et al. | Synthesis of SAPO-34 Zeolite with Different Template Agents and DTO Catalytic Studies | |
CN117299188A (zh) | 含氧化合物制芳烃催化剂及其制备方法和应用 | |
CN112125771A (zh) | 二甲苯的生产方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 201080027222.2 Country of ref document: CN |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 10791994 Country of ref document: EP Kind code of ref document: A1 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2011519771 Country of ref document: JP |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
WWE | Wipo information: entry into national phase |
Ref document number: 10284/DELNP/2011 Country of ref document: IN |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2010791994 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 201270055 Country of ref document: EA |