WO2010128644A1 - プロピレンの製造方法 - Google Patents
プロピレンの製造方法 Download PDFInfo
- Publication number
- WO2010128644A1 WO2010128644A1 PCT/JP2010/057632 JP2010057632W WO2010128644A1 WO 2010128644 A1 WO2010128644 A1 WO 2010128644A1 JP 2010057632 W JP2010057632 W JP 2010057632W WO 2010128644 A1 WO2010128644 A1 WO 2010128644A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- zeolite
- producing propylene
- amount
- acid amount
- catalyst
- Prior art date
Links
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 81
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 44
- 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 185
- 239000010457 zeolite Substances 0.000 claims abstract description 156
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 155
- 239000002253 acid Substances 0.000 claims abstract description 88
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 66
- 239000005977 Ethylene Substances 0.000 claims abstract description 66
- 239000003054 catalyst Substances 0.000 claims abstract description 51
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 52
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 claims description 52
- 239000011148 porous material Substances 0.000 claims description 46
- 238000000034 method Methods 0.000 claims description 43
- 229910000323 aluminium silicate Inorganic materials 0.000 claims description 31
- 229910021529 ammonia Inorganic materials 0.000 claims description 26
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 claims description 26
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 17
- 239000001301 oxygen Substances 0.000 claims description 17
- 229910052760 oxygen Inorganic materials 0.000 claims description 17
- 238000003795 desorption Methods 0.000 claims description 15
- 229910052734 helium Inorganic materials 0.000 claims description 14
- 239000001307 helium Substances 0.000 claims description 14
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 claims description 14
- 150000001336 alkenes Chemical class 0.000 claims description 13
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 229910001868 water Inorganic materials 0.000 claims description 8
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 6
- 150000001342 alkaline earth metals Chemical class 0.000 claims description 6
- 150000001875 compounds Chemical class 0.000 claims description 6
- 230000000630 rising effect Effects 0.000 claims description 6
- -1 polypropylene Polymers 0.000 claims description 5
- 239000004743 Polypropylene Substances 0.000 claims description 3
- 230000000379 polymerizing effect Effects 0.000 claims description 3
- 229920001155 polypropylene Polymers 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 description 58
- 238000006884 silylation reaction Methods 0.000 description 19
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 17
- 229910052799 carbon Inorganic materials 0.000 description 17
- 239000007789 gas Substances 0.000 description 17
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 14
- 239000002994 raw material Substances 0.000 description 14
- 239000000126 substance Substances 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 229910004298 SiO 2 Inorganic materials 0.000 description 12
- 239000003795 chemical substances by application Substances 0.000 description 12
- OFOBLEOULBTSOW-UHFFFAOYSA-N Malonic acid Chemical compound OC(=O)CC(O)=O OFOBLEOULBTSOW-UHFFFAOYSA-N 0.000 description 11
- 229910052782 aluminium Inorganic materials 0.000 description 11
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 11
- 230000007423 decrease Effects 0.000 description 11
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 10
- 239000011230 binding agent Substances 0.000 description 10
- 238000002360 preparation method Methods 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- 239000000203 mixture Substances 0.000 description 9
- 238000010025 steaming Methods 0.000 description 9
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 8
- 150000001491 aromatic compounds Chemical class 0.000 description 8
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 8
- 229910052751 metal Inorganic materials 0.000 description 8
- 239000002184 metal Substances 0.000 description 8
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 7
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 7
- 239000006227 byproduct Substances 0.000 description 7
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 6
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- 239000000571 coke Substances 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 239000002904 solvent Substances 0.000 description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 5
- 229910000019 calcium carbonate Inorganic materials 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- 239000012188 paraffin wax Substances 0.000 description 5
- 229910052698 phosphorus Inorganic materials 0.000 description 5
- 229910052710 silicon Inorganic materials 0.000 description 5
- 239000000758 substrate Substances 0.000 description 5
- 239000005046 Chlorosilane Substances 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 4
- 239000006004 Quartz sand Substances 0.000 description 4
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 4
- BOTDANWDWHJENH-UHFFFAOYSA-N Tetraethyl orthosilicate Chemical compound CCO[Si](OCC)(OCC)OCC BOTDANWDWHJENH-UHFFFAOYSA-N 0.000 description 4
- 125000004432 carbon atom Chemical group C* 0.000 description 4
- KOPOQZFJUQMUML-UHFFFAOYSA-N chlorosilane Chemical compound Cl[SiH3] KOPOQZFJUQMUML-UHFFFAOYSA-N 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000000465 moulding Methods 0.000 description 4
- 239000011574 phosphorus Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000010703 silicon Substances 0.000 description 4
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 3
- 239000012298 atmosphere Substances 0.000 description 3
- 125000004429 atom Chemical group 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 239000003085 diluting agent Substances 0.000 description 3
- JJQZDUKDJDQPMQ-UHFFFAOYSA-N dimethoxy(dimethyl)silane Chemical compound CO[Si](C)(C)OC JJQZDUKDJDQPMQ-UHFFFAOYSA-N 0.000 description 3
- 229910052733 gallium Inorganic materials 0.000 description 3
- UQEAIHBTYFGYIE-UHFFFAOYSA-N hexamethyldisiloxane Chemical compound C[Si](C)(C)O[Si](C)(C)C UQEAIHBTYFGYIE-UHFFFAOYSA-N 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 239000010453 quartz Substances 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- 238000004230 steam cracking Methods 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- YIWUKEYIRIRTPP-UHFFFAOYSA-N 2-ethylhexan-1-ol Chemical compound CCCCC(CC)CO YIWUKEYIRIRTPP-UHFFFAOYSA-N 0.000 description 2
- HGINCPLSRVDWNT-UHFFFAOYSA-N Acrolein Chemical compound C=CC=O HGINCPLSRVDWNT-UHFFFAOYSA-N 0.000 description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- VZCYOOQTPOCHFL-OWOJBTEDSA-N Fumaric acid Chemical compound OC(=O)\C=C\C(O)=O VZCYOOQTPOCHFL-OWOJBTEDSA-N 0.000 description 2
- GYHNNYVSQQEPJS-UHFFFAOYSA-N Gallium Chemical compound [Ga] GYHNNYVSQQEPJS-UHFFFAOYSA-N 0.000 description 2
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 2
- WNLRTRBMVRJNCN-UHFFFAOYSA-N adipic acid Chemical compound OC(=O)CCCCC(O)=O WNLRTRBMVRJNCN-UHFFFAOYSA-N 0.000 description 2
- IISBACLAFKSPIT-UHFFFAOYSA-N bisphenol A Chemical compound C=1C=C(O)C=CC=1C(C)(C)C1=CC=C(O)C=C1 IISBACLAFKSPIT-UHFFFAOYSA-N 0.000 description 2
- 229910052796 boron Inorganic materials 0.000 description 2
- 238000004523 catalytic cracking Methods 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- IJOOHPMOJXWVHK-UHFFFAOYSA-N chlorotrimethylsilane Chemical compound C[Si](C)(C)Cl IJOOHPMOJXWVHK-UHFFFAOYSA-N 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 2
- 230000009849 deactivation Effects 0.000 description 2
- 230000008030 elimination Effects 0.000 description 2
- 238000003379 elimination reaction Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000004817 gas chromatography Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 238000001027 hydrothermal synthesis Methods 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- QQVIHTHCMHWDBS-UHFFFAOYSA-N isophthalic acid Chemical compound OC(=O)C1=CC=CC(C(O)=O)=C1 QQVIHTHCMHWDBS-UHFFFAOYSA-N 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000004949 mass spectrometry Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 235000006408 oxalic acid Nutrition 0.000 description 2
- GJVFBWCTGUSGDD-UHFFFAOYSA-L pentamethonium bromide Chemical compound [Br-].[Br-].C[N+](C)(C)CCCCC[N+](C)(C)C GJVFBWCTGUSGDD-UHFFFAOYSA-L 0.000 description 2
- YWAKXRMUMFPDSH-UHFFFAOYSA-N pentene Chemical compound CCCC=C YWAKXRMUMFPDSH-UHFFFAOYSA-N 0.000 description 2
- 150000004965 peroxy acids Chemical class 0.000 description 2
- XNGIFLGASWRNHJ-UHFFFAOYSA-N phthalic acid Chemical compound OC(=O)C1=CC=CC=C1C(O)=O XNGIFLGASWRNHJ-UHFFFAOYSA-N 0.000 description 2
- 238000006116 polymerization reaction Methods 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- FDNAPBUWERUEDA-UHFFFAOYSA-N silicon tetrachloride Chemical compound Cl[Si](Cl)(Cl)Cl FDNAPBUWERUEDA-UHFFFAOYSA-N 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- VZCYOOQTPOCHFL-UHFFFAOYSA-N trans-butenedioic acid Natural products OC(=O)C=CC(O)=O VZCYOOQTPOCHFL-UHFFFAOYSA-N 0.000 description 2
- RTBFRGCFXZNCOE-UHFFFAOYSA-N 1-methylsulfonylpiperidin-4-one Chemical compound CS(=O)(=O)N1CCC(=O)CC1 RTBFRGCFXZNCOE-UHFFFAOYSA-N 0.000 description 1
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
- MWFMGBPGAXYFAR-UHFFFAOYSA-N 2-hydroxy-2-methylpropanenitrile Chemical compound CC(C)(O)C#N MWFMGBPGAXYFAR-UHFFFAOYSA-N 0.000 description 1
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 1
- DJHGAFSJWGLOIV-UHFFFAOYSA-K Arsenate3- Chemical class [O-][As]([O-])([O-])=O DJHGAFSJWGLOIV-UHFFFAOYSA-K 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- FEWJPZIEWOKRBE-JCYAYHJZSA-N Dextrotartaric acid Chemical compound OC(=O)[C@H](O)[C@@H](O)C(O)=O FEWJPZIEWOKRBE-JCYAYHJZSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- NTIZESTWPVYFNL-UHFFFAOYSA-N Methyl isobutyl ketone Chemical compound CC(C)CC(C)=O NTIZESTWPVYFNL-UHFFFAOYSA-N 0.000 description 1
- UIHCLUNTQKBZGK-UHFFFAOYSA-N Methyl isobutyl ketone Natural products CCC(C)C(C)=O UIHCLUNTQKBZGK-UHFFFAOYSA-N 0.000 description 1
- VVQNEPGJFQJSBK-UHFFFAOYSA-N Methyl methacrylate Chemical compound COC(=O)C(C)=C VVQNEPGJFQJSBK-UHFFFAOYSA-N 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- 239000004435 Oxo alcohol Substances 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 1
- KDYFGRWQOYBRFD-UHFFFAOYSA-N Succinic acid Natural products OC(=O)CCC(O)=O KDYFGRWQOYBRFD-UHFFFAOYSA-N 0.000 description 1
- FEWJPZIEWOKRBE-UHFFFAOYSA-N Tartaric acid Natural products [H+].[H+].[O-]C(=O)C(O)C(O)C([O-])=O FEWJPZIEWOKRBE-UHFFFAOYSA-N 0.000 description 1
- 229920004482 WACKER® Polymers 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 150000001252 acrylic acid derivatives Chemical class 0.000 description 1
- 239000001361 adipic acid Substances 0.000 description 1
- 235000011037 adipic acid Nutrition 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- JFCQEDHGNNZCLN-UHFFFAOYSA-N anhydrous glutaric acid Natural products OC(=O)CCCC(O)=O JFCQEDHGNNZCLN-UHFFFAOYSA-N 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- KDYFGRWQOYBRFD-NUQCWPJISA-N butanedioic acid Chemical compound O[14C](=O)CC[14C](O)=O KDYFGRWQOYBRFD-NUQCWPJISA-N 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000013480 data collection Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- LIKFHECYJZWXFJ-UHFFFAOYSA-N dimethyldichlorosilane Chemical compound C[Si](C)(Cl)Cl LIKFHECYJZWXFJ-UHFFFAOYSA-N 0.000 description 1
- YYLGKUPAFFKGRQ-UHFFFAOYSA-N dimethyldiethoxysilane Chemical compound CCO[Si](C)(C)OCC YYLGKUPAFFKGRQ-UHFFFAOYSA-N 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- UPUANNBILBRCST-UHFFFAOYSA-N ethanol;ethene Chemical group C=C.CCO UPUANNBILBRCST-UHFFFAOYSA-N 0.000 description 1
- RSIHJDGMBDPTIM-UHFFFAOYSA-N ethoxy(trimethyl)silane Chemical compound CCO[Si](C)(C)C RSIHJDGMBDPTIM-UHFFFAOYSA-N 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000001530 fumaric acid Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 150000002290 germanium Chemical class 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 238000007163 homologation reaction Methods 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- 239000001095 magnesium carbonate Substances 0.000 description 1
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 1
- VZCYOOQTPOCHFL-UPHRSURJSA-N maleic acid Chemical compound OC(=O)\C=C/C(O)=O VZCYOOQTPOCHFL-UPHRSURJSA-N 0.000 description 1
- 239000011976 maleic acid Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 230000010534 mechanism of action Effects 0.000 description 1
- 238000005649 metathesis reaction Methods 0.000 description 1
- POPACFLNWGUDSR-UHFFFAOYSA-N methoxy(trimethyl)silane Chemical compound CO[Si](C)(C)C POPACFLNWGUDSR-UHFFFAOYSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000005691 oxidative coupling reaction Methods 0.000 description 1
- 238000005839 oxidative dehydrogenation reaction Methods 0.000 description 1
- 125000004430 oxygen atom Chemical group O* 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 235000021317 phosphate Nutrition 0.000 description 1
- 150000003013 phosphoric acid derivatives Chemical class 0.000 description 1
- 239000006069 physical mixture Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 229920005668 polycarbonate resin Polymers 0.000 description 1
- 239000004431 polycarbonate resin Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 150000004760 silicates Chemical class 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000008279 sol Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000011975 tartaric acid Substances 0.000 description 1
- 235000002906 tartaric acid Nutrition 0.000 description 1
- LFQCEHFDDXELDD-UHFFFAOYSA-N tetramethyl orthosilicate Chemical compound CO[Si](OC)(OC)OC LFQCEHFDDXELDD-UHFFFAOYSA-N 0.000 description 1
- NKLYMYLJOXIVFB-UHFFFAOYSA-N triethoxymethylsilane Chemical compound CCOC([SiH3])(OCC)OCC NKLYMYLJOXIVFB-UHFFFAOYSA-N 0.000 description 1
- TUQLLQQWSNWKCF-UHFFFAOYSA-N trimethoxymethylsilane Chemical compound COC([SiH3])(OC)OC TUQLLQQWSNWKCF-UHFFFAOYSA-N 0.000 description 1
- 239000005051 trimethylchlorosilane Substances 0.000 description 1
- 239000008096 xylene 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
- B01J29/70—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
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/76—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/12—After treatment, characterised by the effect to be obtained to alter the outside of the crystallites, e.g. selectivation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/36—Steaming
-
- 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
Definitions
- the present invention relates to a method for producing propylene with high selectivity by contacting ethylene with a catalyst.
- Patent Document 1 discloses that propylene can be produced by using, as a catalyst, an aluminosilicate having a pore diameter of less than 0.5 nm by a propylene production method using ethylene as a raw material.
- an object of the present invention is to provide a method for producing propylene with high selectivity by using ethylene as a raw material, suppressing the selectivity of C 4 or higher components.
- the present inventors have made a catalyst with a high selectivity from ethylene by using zeolite as a catalyst whose acid amount on the outer surface is small relative to the total acid amount.
- the inventors have found that it can be produced and have arrived at the present invention. That is, the gist of the present invention is as follows. ⁇ 1> Including contacting the ethylene with the catalyst, Containing zeolite as an active component of the catalyst, The method for producing propylene, wherein the acid amount on the outer surface of the zeolite is 5% or less with respect to the acid amount of the whole zeolite.
- ⁇ 2> The method for producing propylene according to ⁇ 1>, wherein the acid amount on the outer surface of the zeolite is represented by a pyridine elimination amount defined by (I) below.
- a pyridine elimination amount defined by (I) below.
- the zeolite was dried at 500 ° C. under vacuum for 1 hour, and then the pretreated zeolite was brought into contact with pyridine vapor at 150 ° C. to adsorb pyridine to the zeolite, and evacuated at 150 ° C. and helium flow. The amount of pyridine desorbed per unit weight of zeolite at 150 to 800 ° C.
- ⁇ 5> The method for producing propylene according to any one of ⁇ 1> to ⁇ 4>, wherein the zeolite has an oxygen 8-membered ring structure or an oxygen 9-membered ring structure.
- ⁇ 6> The method for producing propylene according to any one of ⁇ 1> to ⁇ 5>, wherein the skeleton structure of the zeolite is a CHA type structure.
- ⁇ 7> The method for producing propylene according to any one of ⁇ 1> to ⁇ 6>, wherein an outer surface of the zeolite is silylated.
- ⁇ 8> The method for producing propylene according to any one of ⁇ 1> to ⁇ 6>, wherein the zeolite is steam-treated.
- ⁇ 9> The method for producing propylene according to ⁇ 8>, wherein the steam treatment temperature is 400 to 700 ° C.
- ⁇ 10> The method for producing propylene according to ⁇ 8> or ⁇ 9>, wherein the zeolite is steam-treated after being mixed with a compound containing an alkaline earth metal.
- ⁇ 12> A zeolite having a pore diameter of less than 0.5 nm and having an acid amount on the outer surface of 5% or less based on the total acid amount.
- ⁇ 13> The zeolite according to ⁇ 12>, which is an aluminosilicate.
- ⁇ 14> The zeolite according to ⁇ 12> or ⁇ 13>, which has an oxygen 8-membered ring structure or an oxygen 9-membered ring structure.
- ⁇ 15> The zeolite according to any one of ⁇ 12> to ⁇ 14>, which has a CHA-type skeleton structure.
- ⁇ 16> The zeolite according to any one of ⁇ 12> to ⁇ 15>, which has a silylated outer surface.
- a catalyst comprising the zeolite according to any one of ⁇ 12> to ⁇ 16>.
- ⁇ 18> The catalyst for olefin manufacture containing the zeolite as described in any one of ⁇ 12> to ⁇ 16> above.
- propylene can be produced with high selectivity by using ethylene as a raw material, suppressing the selectivity of C 4 or higher components.
- the method for producing propylene of the present invention is a method for producing propylene by contacting ethylene with a catalyst.
- the propylene production method includes zeolite as an active component of the catalyst, and the acid amount on the outer surface of the zeolite is 5 with respect to the acid amount of the whole zeolite. % Of propylene.
- the catalyst used in the present invention contains zeolite as a catalyst active component, and preferably uses zeolite as a catalyst active component.
- Zeolite refers to a crystalline substance in which TO 4 units having a tetrahedral structure (T is a central atom) share O atoms three-dimensionally to form open regular micropores.
- Specific examples include silicates, phosphates, germanium salts, and arsenates that are described in the Data Collection of the Structure Committee of the International Zeolite Association (IZA).
- the acid amount on the outer surface of the zeolite (hereinafter sometimes simply referred to as the outer surface acid amount) represents the total amount of acid sites present on the outer surface of the zeolite.
- the amount of acid on the outer surface is measured by adsorbing a substance that can be selectively adsorbed on the acid sites of the zeolite and cannot enter the pores of the zeolite, and quantifying the amount of adsorption. Can do.
- the said substance is not specifically limited, Specifically, a pyridine can be used.
- the method for determining the amount of pyridine adsorbed is not particularly limited, but it can usually be measured by the following procedure.
- the zeolite is dried and then contacted with pyridine vapor. Subsequently, excess pyridine is removed to obtain zeolite adsorbed with pyridine.
- the amount of pyridine desorbed per unit weight of zeolite adsorbed with pyridine can be measured by a temperature-programmed desorption method (hereinafter also referred to as “TPD”) to determine the amount of acid on the outer surface.
- TPD temperature-programmed desorption method
- the amount of acid on the outer surface is not particularly limited, but is usually 0.6 mmol / g or less, preferably 0.3 mmol / g or less. If the upper limit is exceeded, a reaction that is not shape-selective occurs on the outer surface, and the selectivity for propylene may decrease.
- the total acid amount of the zeolite in the present invention (hereinafter sometimes simply referred to as the total acid amount) is the total acid amount of the zeolite, specifically, the total acid amount on the outer surface and inside the pores.
- the total acid amount of the zeolite shall be measured by adsorbing a substance that can be selectively adsorbed on the acid sites of the zeolite and also entering the pores, and quantifying the adsorbed amount. Can do.
- the substance is not particularly limited, and specifically, ammonia can be used.
- the method for quantifying the amount of adsorbed ammonia is not particularly limited, but can usually be measured by the following procedure. As a pretreatment, after the zeolite is dried, ammonia is contact-adsorbed. Subsequently, excess ammonia is removed to obtain zeolite adsorbed with ammonia. The total amount of acid can be determined by measuring the desorption amount of ammonia per unit weight of the zeolite adsorbed with ammonia by a temperature-programmed desorption method.
- the total acid amount is not particularly limited, but is usually 4.8 mmol / g or less, preferably 2.8 mmol / g or less. Moreover, it is 0.15 mmol / g or more normally, Preferably it is 0.30 mmol / g or more.
- the upper limit is exceeded, deactivation due to coke adhesion is accelerated, aluminum tends to escape from the skeleton (so-called dealumination), and the acid strength per acid point tends to be weak. Below the lower limit, the acid amount is small. Therefore, the conversion rate of ethylene may decrease.
- the zeolite used in the present invention is characterized in that the acid amount on the outer surface of the zeolite is 5% or less with respect to the acid amount of the entire zeolite. Preferably it is 4.5% or less, More preferably, it is 3.5% or less.
- the lower limit is not particularly limited and is preferably as small as possible, but is usually 0.1% or more.
- the zeolite used in the present invention usually has pores (channels).
- the pore diameter of the zeolite used in the present invention is not particularly limited, but is preferably smaller, and the length of the pore diameter is usually less than 0.5 nm, preferably 0.4 nm or less.
- the pore diameter length of the zeolite is equal to or more than the above upper limit, there is a disadvantage that by-products other than propylene (butene, pentene, etc.) increase, and it may not be possible to produce propylene with high selectivity from ethylene.
- the term “pore diameter” as used herein refers to a crystallographic free diameter of the channels determined by International Zeolite Association (IZA).
- a pore diameter of less than 0.5 nm means that the diameter of the pore (channel) is less than 0.5 nm when the shape of the pore (channel) is a perfect circle, and a short diameter when the shape of the pore is an ellipse. It means that the diameter is less than 0.5 nm.
- propylene can be produced from ethylene with high selectivity by using a zeolite with a small pore diameter.
- ethylene is activated by the presence of strong acid sites in the zeolite.
- propylene can be selectively produced with a small pore diameter. That is, since the pore diameter is small, the target propylene produced by contact with the zeolite can come out of the pores.
- the C 4 or higher components such as butene and pentene, which are by-products, remain in the pores because the molecules are too large. It is considered that propylene can be obtained with a high selectivity by such a mechanism.
- the lower limit of the pore diameter of zeolite is not particularly limited, but is usually 0.2 nm or more, preferably 0.3 nm or more. If the pore diameter is less than the lower limit, neither ethylene nor propylene can pass through, and the reaction between ethylene and active sites is unlikely to occur, and the reaction rate may be reduced.
- zeolite used in the present invention there is no particular limitation on the zeolite used in the present invention, but usually a zeolite having an oxygen 8-membered ring structure or a 9-membered ring structure is preferable.
- the oxygen 8-membered ring structure or 9-membered ring structure means a ring structure in which the zeolite has 8 or 9 pores of TO 4 units (T is Si, P, Ge, Al, Ga, etc.). If it is an oxygen 8-membered ring structure or an oxygen 9-membered ring structure, it becomes a preferable pore diameter and high propylene selectivity is obtained.
- zeolites whose pores are composed of only oxygen 8-membered rings are preferable.
- the skeleton structure of the zeolite whose pores are composed of only an oxygen 8-membered ring can be expressed by a code defined by International Zeolite Association (IZA), for example, AFX, CAS, CHA, DDR, ERI. , ESV, GIS, GOO, ITE, JBW, KFI, LEV, LTA, MER, MON, MTF, PAU, PHI, RHO, RTE, RTH, and the like.
- IZA International Zeolite Association
- Specific examples of the zeolite containing an oxygen 9-membered ring and having only pores of oxygen 9-membered or less include NAT, RSN, STT, and the like when expressed by a code defined by International Zeolite Association (IZA).
- AFX, CHA, DDR, ERI, LEV, RHO, and RTH can be exemplified as preferred framework structures of the zeolite in the present invention, and CHA is more preferred.
- the framework density of the zeolite used in the present invention is not particularly limited, but a zeolite having a framework density of usually 18.0 T / nm 3 or less is preferable, and more preferably 17.0 T / nm 3 or less. In general, it is 13.0 T / nm 3 or more, preferably 14.0 T / nm 3 or more.
- the framework density (unit: T / nm 3 ) means the number of T atoms (among atoms constituting the zeolite skeleton, other than oxygen) present per unit volume (1 nm 3 ) of the zeolite. However, this value is determined by the structure of the zeolite.
- a metal is usually contained in the framework of the zeolite used in the present invention.
- the metal contained is not particularly limited, but is usually at least one selected from aluminum, gallium, iron, and boron, preferably aluminum.
- the catalyst having zeolite as an active component in the present invention is usually a proton exchange type, but a part thereof is exchanged with an alkali metal such as Na or K, or an alkaline earth metal such as Mg or Ca. Also good.
- the zeolite has a SiO 2 / M 2 O 3 molar ratio (hereinafter referred to as SiO 2 / metal molar ratio; M is a trivalent metal such as aluminum, gallium, iron, and boron), although it is not particularly limited. Yes, preferably 10 or more.
- SiO 2 / metal molar ratio is less than the lower limit, the durability of the catalyst may be lowered.
- the upper limit of the SiO 2 / metal molar ratio is not particularly limited, but is usually 1000 or less. When the SiO 2 / metal molar ratio exceeds the above upper limit, the catalytic activity may decrease.
- zeolite in the present invention examples include aluminosilicates whose constituent elements are silicon and aluminum, aluminophosphates (ALPO) consisting of aluminum and phosphorus, silicoaluminophosphates (SAPO) consisting of silicon, aluminum and phosphorus. .
- APO aluminophosphates
- SAPO silicoaluminophosphates
- aluminosilicate or silicoaluminophosphate is preferable, and aluminosilicate is more preferable.
- the zeolite in the present invention is preferably a zeolite having a CHA structure.
- the zeolite having a CHA structure is specifically an aluminosilicate comprising silicon and aluminum as constituent elements, an aluminophosphate comprising aluminum and phosphorus (ALPO-34), Examples thereof include silicoaluminophosphate (SAPO-34) composed of silicon, aluminum and phosphorus, among which aluminosilicate or silicoaluminophosphate is preferable, and aluminosilicate is more preferable.
- SAPO-34 silicoaluminophosphate
- the SiO 2 / Al 2 O 3 molar ratio in the aluminosilicate is not particularly limited, but is usually 5 or more and preferably 10 or more. If it is less than the lower limit, deactivation due to coke adhesion tends to be fast, aluminum tends to escape from the skeleton (so-called dealumination), and the acid strength per acid point tends to be weak. Also, SiO 2 / Al 2 O 3 molar ratio is usually 200 or less, preferably 100 or less. If the upper limit is exceeded, the acid amount is small, and the ethylene conversion rate may decrease.
- the method for producing the zeolite of the present invention is not particularly limited, and can be produced by a known method such as the production method described in US Pat. No. 4,544,538. In general, it can be prepared by a hydrothermal synthesis method. Moreover, what changed the composition by ion exchange, dealumination treatment, impregnation, etc. after hydrothermal synthesis can also be used.
- the zeolite used in the present invention is a zeolite having an acid amount on the outer surface of the zeolite of 5% or less with respect to the acid amount of the entire zeolite, and can be obtained by reducing the ratio of the acid amount of the outer surface of the zeolite.
- the method for reducing the ratio of the outer surface acid amount to the total acid amount is not particularly limited, but 1) a method for silylating the outer surface of the zeolite, 2) a method for steaming (steaming) the zeolite, 3 ) A method of treating zeolite with dicarboxylic acid.
- the method of silylating the outer surface of the zeolite is a method of reducing the acid amount on the outer surface by silylating the outer surface of the active component zeolite of the catalyst.
- the method of silylation is not particularly limited, and a known method can be used as appropriate. Specifically, it is carried out by liquid phase silylation using alkoxysilane or gas phase silylation using chlorosilane. Can do.
- the silylating agent is not particularly limited, but specific examples of the alkoxysilane include quaternary alkoxysilanes such as tetramethoxysilane and tetraethoxysilane; and 3 such as trimethoxymethylsilane and triethoxymethylsilane.
- chlorosilane examples include chlorosilanes such as tetrachlorosilane, dimethyldichlorosilane, and trimethylchlorosilane. Of these, tetraethoxysilane is preferable for alkoxysilane, and tetrachlorosilane is preferable for chlorosilane.
- a solvent can be appropriately used.
- the solvent to be used is not particularly limited, an organic solvent such as benzene, toluene, hexamethyldisiloxane, or water can be used.
- the amount ratio (mol / mol) of the silylating agent / zeolite in the treatment solution is not particularly limited, but is usually 5 or less, preferably 3 or less. Moreover, it is 0.005 or more normally, Preferably it is 0.1 or more. If this value exceeds the upper limit, pores may be blocked due to excessive silylation, and if it is less than the lower limit, silylation may be insufficient and acid sites on the outer surface may not be poisoned.
- the temperature of the silylation can be appropriately adjusted depending on the kind of the silylating agent and the solvent, and is not limited, but is usually 140 ° C. or lower, preferably 120 ° C. or lower. Moreover, it is 20 degreeC or more normally, Preferably it is 40 degreeC or more. If the upper limit is exceeded, silylation may not occur efficiently due to evaporation of the silylating agent, and if it is less than the lower limit, the reaction rate of silylation may be slow.
- the treatment time is not particularly limited as long as silylation for achieving the purpose of the present invention occurs, but usually 0.5 hours or more, preferably 2 hours or more, and there is no particular upper limit of the treatment time, but usually 48 hours or less. is there. If the treatment time is less than the lower limit, silylation does not occur sufficiently, and acid point poisoning may be insufficient.
- the gas phase silylation treatment is usually performed so that the weight of silica deposited on the zeolite is usually 20% by weight or less, preferably 18% by weight or less. Although there is no particular lower limit, it is usually 0.1% by weight or more, preferably 1% by weight or more. If the upper limit is exceeded, pores may be blocked due to excessive silylation, and if it is less than the lower limit, silylation may be insufficient and acid sites on the outer surface may not be poisoned.
- the temperature of the gas phase silylation can be appropriately adjusted depending on the silylating agent and is not limited, but is usually 20 ° C. or higher, preferably 100 ° C. or higher. Moreover, it is 500 degrees C or less normally, Preferably it is 400 degrees C or less. If the upper limit is exceeded, decomposition of the silylating agent, collapse of the skeleton of the zeolite may occur, and if it is less than the lower limit, the silylation reaction may not proceed.
- the method for steaming the zeolite is not particularly limited, but the steaming temperature is usually 400 ° C. or higher, preferably 500 ° C. or higher. Moreover, it is 700 degrees C or less normally, Preferably it is 650 degrees C or less. If it is less than the lower limit, the effect of steaming is small, and if it exceeds the upper limit, the structure of the zeolite may collapse. Steam can also be diluted with an inert gas such as helium or nitrogen. The steam concentration is not particularly limited, but is usually 3% by volume or more, preferably 5% by volume or more, and there is no upper limit, and treatment with 100% water vapor is possible.
- the compound containing an alkaline earth metal include calcium carbonate, calcium hydroxide, and magnesium carbonate, among which calcium carbonate is preferable.
- the amount of the compound containing an alkaline earth metal is preferably 0.5% to 45% by weight based on the zeolite. More preferably, it is 3 to 40% by weight.
- the steaming may be performed in a state where organic substances are present inside the pores for the purpose of selectively reducing the acid amount on the outer surface by dealumination.
- organic substance The structure directing agent used at the time of a zeolite synthesis
- the structure directing agent is present in the pores of the zeolite in a synthesized state.
- coke can be made to exist in the inside of a pore by the method of distribute
- the method for treating zeolite with dicarboxylic acid is not particularly limited as long as the object of the present application is achieved.
- Dicarboxylic acid is thought to reduce the amount of acid by accelerating the elimination of the metal in the framework such as dealumination of the zeolite, but the molecular size is larger than the zeolite pores, It cannot penetrate into the pores, and the acid amount on the outer surface can be selectively reduced.
- the dicarboxylic acid include oxalic acid, malonic acid, succinic acid, glutaric acid, adipic acid, maleic acid, phthalic acid, isophthalic acid, fumaric acid, tartaric acid, and the like. Of these, oxalic acid is preferred.
- the dicarboxylic acid is preferably dissolved in a solvent such as alcohol or water to form a solution and mixed with the zeolite.
- concentration of the dicarboxylic acid in the solution is generally 0.01M to 4M, preferably 1M to 3M.
- the temperature during mixing is usually 15 ° C to 95 ° C, preferably 50 ° C to 85 ° C.
- Mixing with zeolite may be carried out twice or more in order to promote dealumination of the zeolite surface.
- the dicarboxylic acid treatment may be performed in a state where organic substances are present inside the pores for the purpose of selectively reducing the acid amount on the outer surface by dealumination.
- generated by reaction are mentioned.
- the structure directing agent is present in the pores of the zeolite in a synthesized state.
- coke can be made to exist in the inside of a pore by the method of distribute
- the above-mentioned catalytically active component may be used as it is in the reaction as a catalyst, or may be used in the reaction by granulating and molding using a substance or binder that is inert to the reaction, or by mixing them.
- the outer surface acid amount can be decreased with respect to the total acid amount by molding.
- the substance or binder inert to the reaction include alumina or alumina sol, silica, silica gel, quartz, and a mixture thereof.
- a method for reducing the acid amount by molding for example, a method of bonding the acid sites on the surface of the binder and the zeolite can be mentioned.
- the outer surface acid amount and the total acid amount are measured as a total value including the acid amount of the binder as well as the acid amount of the zeolite. .
- the method for determining the acid amount of the binder is not particularly limited.
- the total acid amount of the zeolite is determined from the peak intensity of 4-coordinated Al derived from the zeolitic acid point, and determined by the ammonia temperature programmed desorption method. Examples include a method of subtracting from the total value of the total zeolite acid amount and the binder acid amount.
- the present invention relates to a process for producing propylene by reacting ethylene by contacting it with a catalyst.
- the raw material ethylene is not particularly limited.
- dehydrogenation of ethylene and ethane obtained by conducting Fischer-Tropsch synthesis using ethylene produced from a petroleum source by catalytic cracking or steam cracking, etc. and hydrogen / CO mixed gas obtained by gasification of coal Or obtained by oxidative dehydrogenation Ethylene obtained by metathesis reaction and homologation reaction of propylene, ethylene obtained by MTO (Methanol to Olefin) reaction, obtained by oxidative coupling of ethylene and methane obtained from dehydration reaction of ethanol Ethylene obtained by various known methods such as ethylene can be arbitrarily used.
- MTO Methanol to Olefin
- the olefin to be recycled is usually ethylene, but other olefins may be recycled.
- the olefin used as a raw material is preferably a lower olefin, and a branched olefin is not preferred because it is difficult to enter the zeolite pores due to its molecular size.
- the olefin is preferably ethylene or linear butene, and most preferably ethylene.
- the ethylene of the present invention is preferably contacted with a catalyst in a reactor to produce propylene.
- a catalyst in a reactor to produce propylene.
- a continuous type fixed bed reactor and a fluidized bed reactor are selected.
- a fluidized bed reactor is preferred.
- particulates inert to the reaction such as quartz sand, alumina, silica, silica-alumina, etc., are combined with the catalyst. You may mix and fill.
- this granular material is a particle size comparable as a catalyst from the surface of uniform mixing property with a catalyst.
- ⁇ Diluent> In the reactor, in addition to ethylene, helium, argon, nitrogen, carbon monoxide, carbon dioxide, hydrogen, water, paraffins, hydrocarbons such as methane, aromatic compounds, and mixtures thereof, A gas inert to the reaction can be present, but among these, water (water vapor) is preferably present together.
- Substrate concentration> There is no particular restriction on the concentration of ethylene in all feed components fed to the reactor (ie substrate concentration), but usually ethylene is less than 90 mol% in all feed components. Preferably it is 70 mol% or less. Moreover, it is 5 mol% or more normally.
- substrate concentration exceeds the above upper limit, the production of aromatic compounds and paraffins becomes remarkable, and the propylene selectivity tends to decrease.
- the substrate concentration is less than the lower limit, the reaction rate becomes slow, so a large amount of catalyst is required, and the reactor tends to be too large. Therefore, it is preferable to dilute ethylene with a diluent described below as necessary so as to obtain such a substrate concentration.
- the space velocity mentioned here is a flow rate (weight / hour) of ethylene as a reaction raw material per weight of the catalyst (catalytic active component).
- the weight of the catalyst is the weight of an inactive component used for granulation / molding of the catalyst or a catalytically active component not containing a binder.
- Space velocity but it is not particularly limited but is preferably between 0.01 hr -1 for 500HR -1, more preferably between 0.1 hr -1 to 100 Hr -1. If the space velocity is too high, the amount of ethylene in the reactor outlet gas increases, which is not preferable because the propylene yield decreases. On the other hand, when the space velocity is too low, undesirable by-products such as paraffins are generated, and the propylene selectivity is lowered, which is not preferable.
- the reaction temperature is not particularly limited as long as ethylene is brought into contact with the catalyst to produce propylene, but is usually about 200 ° C or higher, preferably 300 ° C or higher, and usually 700 ° C or lower, preferably 600 ° C or lower. It is. When the reaction temperature is less than the lower limit, the reaction rate is low, a large amount of unreacted raw material tends to remain, and the propylene yield also tends to decrease. On the other hand, if the reaction temperature exceeds the above upper limit, the yield of propylene may be significantly reduced.
- the reaction pressure is not particularly limited, but is usually 2 MPa (absolute pressure, the same shall apply hereinafter) or less, preferably 1 MPa or less, more preferably 0.7 MPa or less. Moreover, it is 1 kPa or more normally, Preferably it is 50 kPa or more.
- the reaction pressure exceeds the upper limit, the amount of undesired by-products such as paraffins increases, and the propylene selectivity tends to decrease.
- the reaction pressure is less than the lower limit, the reaction rate tends to be slow.
- the conversion is not particularly limited, but usually the conversion of ethylene is 20% or more, preferably 40% or more, more preferably 50% or more, and usually 95% or less, preferably 90%.
- the reaction is preferably performed under the following conditions. If this conversion rate is less than the lower limit, there are a lot of unreacted ethylene and the propylene yield is low, which is not preferable. On the other hand, when the amount is not less than the upper limit, undesirable by-products such as paraffins increase and the propylene selectivity decreases, which may not be preferable.
- the catalyst When the reaction is carried out in a fluidized bed reactor, the catalyst can be operated at a preferable conversion rate by adjusting the residence time of the catalyst in the reactor and the residence time in the regenerator.
- the selectivity in this specification is a value calculated by the following equations.
- propylene, butene, C 5 +, paraffin or aromatic compound-derived carbon (mol) means the number of moles of carbon atoms constituting each component.
- Paraffin is the sum of paraffins having 1 to 3 carbon atoms
- aromatic compounds are the sum of benzene, toluene and xylene
- C 5 + is the sum of C 5 or more hydrocarbons excluding the aromatic compounds.
- reaction product As the reactor outlet gas (reactor effluent), a mixed gas containing reaction product propylene, unreacted ethylene, by-products and a diluent is obtained.
- the propylene concentration in the mixed gas is usually 1% by weight or more, preferably 2% by weight or more, and usually 95% by weight or less, preferably 80% by weight or less.
- the mixed gas usually contains ethylene, but it is preferable that at least a part of the ethylene in the mixed gas is recycled to the reactor and reused as a reaction raw material.
- by-products include olefins having 4 or more carbon atoms and paraffins.
- Polypropylene can be produced by polymerizing propylene obtained according to the present invention.
- the method of polymerization is not particularly limited, but the obtained propylene can be directly used as a raw material for the polymerization system. It can also be used as a raw material for other propylene derivatives.
- acrylonitrile can be produced by ammonia oxidation, acrolein, acrylic acid and acrylate esters by selective oxidation, oxo alcohols such as normal butyl alcohol and 2-ethylhexanol by oxo reaction, and propylene oxide and propylene glycol by selective oxidation.
- acetone can be produced by Wacker reaction, and methyl isobutyl ketone can be produced from acetone.
- Acetone cyanohydrin can also be produced from acetone, which is ultimately converted to methyl methacrylate.
- Isopropyl alcohol can also be produced by propylene hydration.
- phenol, bisphenol A, or polycarbonate resin can be produced from a cumene produced by reacting propylene with benzene.
- Examples 1 to 6, Comparative Example 1 ⁇ Acid amount measurement>
- the total acid amount and the outer surface acid amount were measured by NH 3 -TPD and Pyridine-TPD, respectively.
- the measurement was performed as follows using an automatic temperature-programmed desorption analyzer TP5500 manufactured by Bell Japan. (Total acid amount) 30-50 mg of aluminosilicate as a sample was left to dry at 500 ° C. for 1 hour in a helium atmosphere to desorb adsorbed materials such as organic matter and water.
- the aluminosilicate adsorbed with pyridine was heated at 10 ° C./min in a helium atmosphere, and the amount of pyridine desorbed at 150 to 800 ° C. was detected by mass spectrometry.
- the amount of pyridine desorbed per unit weight is shown in Table 1 as the amount of acid on the outer surface of the aluminosilicate sample. Table 1 shows the ratio of the outer surface acid amount to the total acid amount.
- Example 5 For the reaction, an atmospheric pressure fixed bed flow reactor was used, and a mixture of 100 mg of aluminosilicate of Preparation Example 1 and 400 mg of quartz sand was packed in a quartz reaction tube having an inner diameter of 6 mm. A mixed gas of 30% by volume of ethylene and 70% by volume of nitrogen was supplied to the reactor so that the weight space velocity of ethylene was 0.36 Hr ⁇ 1 , and the reaction was performed at 350 ° C. and 0.1 MPa. After starting the reaction, the product was analyzed by gas chromatography after 1.92 hours and 3.17 hours. The results are shown in Table 1.
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)
- Silicates, Zeolites, And Molecular Sieves (AREA)
Abstract
Description
そこで、エチレンだけを原料として高収率でプロピレンを製造する技術が望まれていた。
すなわち、本発明の要旨は、下記に存する。
<1>
エチレンと触媒とを接触させる工程を含み、
前記触媒の活性成分としてゼオライトを含み、
前記ゼオライトの外表面の酸量が、ゼオライト全体の酸量に対して5%以下であることを特徴とするプロピレンの製造方法。
<2>
前記ゼオライトの外表面の酸量が、下記(I)により定義されるピリジン脱離量で表されることを特徴とする上記<1>に記載のプロピレンの製造方法。
(I)前処理としてゼオライトを真空下500℃で1時間乾燥させた後、前処理したゼオライトを150℃でピリジン蒸気と接触させてゼオライトにピリジンを吸着させ、150℃で減圧排気及びヘリウムフローにより該ゼオライトから余剰ピリジンを除いて得られた、ピリジンを吸着したゼオライトの、昇温速度10℃/分の昇温脱離法による150~800℃におけるゼオライト単位重量当たりのピリジンの脱離量。
<3>
前記ゼオライトの全体の酸量が、下記(II)により定義されるアンモニア脱離量で表されることを特徴とする上記<1>又は<2>に記載のプロピレンの製造方法。
(II)前処理としてゼオライトをヘリウムフロー下500℃で1時間乾燥させた後、前処理したゼオライトを100℃で5体積%アンモニア/ヘリウムと接触させてゼオライトにアンモニアを吸着させ、得られたゼオライトを100℃で水蒸気と接触させ該ゼオライトから余剰アンモニアを除いて得られた、アンモニアを吸着したゼオライトの、昇温速度10℃/分の昇温脱離法による100~800℃におけるゼオライト単位重量当たりのアンモニアの脱離量。
<4>
前記ゼオライトが、0.5nm未満の細孔径を有することを特徴とする上記<1>から<3>のいずれか1に記載のプロピレンの製造方法。
<5>
前記ゼオライトが酸素8員環構造または酸素9員環構造を有することを特徴とする上記<1>から<4>のいずれか1に記載のプロピレンの製造方法。
<6>
前記ゼオライトの骨格構造がCHA型構造であることを特徴とする上記<1>から<5>のいずれか1に記載のプロピレンの製造方法。
<7>
前記ゼオライトの外表面がシリル化されていることを特徴とする上記<1>から<6>のいずれか1に記載のプロピレンの製造方法。
<8>
前記ゼオライトが水蒸気処理されていることを特徴とする上記<1>から<6>のいずれか1に記載のプロピレンの製造方法。
<9>
前記水蒸気処理の温度が400~700℃であることを特徴とする上記<8>に記載のプロピレンの製造方法。
<10>
前記ゼオライトがアルカリ土類金属を含む化合物と混合後に水蒸気処理されていることを特徴とする上記<8>又は<9>に記載のプロピレンの製造方法。
<11>
上記<1>から<10>のいずれか1に記載の製造方法により得られたプロピレンを重合する工程を含むことを特徴とするポリプロピレンの製造方法。
<12>
0.5nm未満の細孔径を有し、外表面の酸量が、全体の酸量に対して5%以下であることを特徴とするゼオライト。
<13>
アルミノシリケートである上記<12>に記載のゼオライト。
<14>
酸素8員環構造または酸素9員環構造を有する上記<12>または<13>に記載のゼオライト。
<15>
CHA型構造の骨格構造を有する上記<12>から<14>のいずれか1に記載のゼオライト。
<16>
シリル化された外表面を有する上記<12>から<15>のいずれか1に記載のゼオライト。
<17>
上記<12>から<16>のいずれか1に記載のゼオライトを含む触媒。
<18>
上記<12>から<16>のいずれか1に記載のゼオライトを含むオレフィン製造用触媒。
以下、本発明における構成成分について説明する。
まず本発明に使用する触媒について説明する。本発明で用いる触媒は、ゼオライトを触媒活性成分として含むものであり、ゼオライトを触媒活性成分とするものが好ましい。
<ゼオライト>
ゼオライトとは四面体構造をもつTO4単位(Tは中心原子)がO原子を共有して三次元的に連結し、開かれた規則的なミクロ細孔を形成している結晶性物質を指す。具体的には国際ゼオライト学会(International Zeolite Association, (IZA))の構造委員会データ集に記載のあるケイ酸塩、リン酸塩、ゲルマニウム塩、およびヒ酸塩が含まれる。
本発明におけるゼオライトの外表面の酸量(以下、単に外表面酸量ということがある。)とは、ゼオライトの外表面に存在する酸点の総量を表す。
外表面酸量は、ゼオライトの酸点に選択的に吸着させることができ、且つゼオライトの細孔内部に入ることができない物質を、ゼオライトに吸着させ、その吸着量を定量することにより測定することができる。前記の物質は、特に限定されるものではないが、具体的にはピリジンを用いることができる。
ピリジン吸着量の定量方法は特に限定されないが、通常以下の手順により測定することができる。前処理としてゼオライトを乾燥させた後、ピリジン蒸気と接触吸着させる。引き続き余剰ピリジンを除き、ピリジンを吸着させたゼオライトを得る。前記ピリジンを吸着させたゼオライトの、単位重量当たりのピリジンの脱離量を、昇温脱離法(以下「TPD」とも称する)により測定し、外表面酸量を求めることができる。
ゼオライトの全体の酸量は、ゼオライトの酸点に選択的に吸着させることができ且つ細孔内部にも入ることができる物質を、ゼオライトに吸着させ、その吸着量を定量することにより測定することができる。前記の物質は、特に限定されるものではないが、具体的には、アンモニアを用いることができる。
本発明で用いるゼオライトは通常、細孔(チャネル)を有する。
本発明で用いるゼオライトの細孔径は、特に限定されるものではないが、小さい方が好ましく、通常細孔径の長さが0.5nm未満であり、好ましくは0.4nm以下である。
ゼオライトの細孔径の長さが前記上限以上では、プロピレン以外の副生成物(ブテン、ペンテン等)が多くなるという不都合が生じ、エチレンから高い選択率でプロピレンを製造することはできない場合がある。
ここで言う細孔径とは、International Zeolite Association(IZA)が定める結晶学的なチャネル直径(Crystallographic free diameter of the channels)を示す。細孔径が0.5nm未満とは、細孔(チャネル)の形状が真円形の場合は、その直径が0.5nm未満であることを意味し、細孔の形状が楕円形の場合は、短径が0.5nm未満であることを意味する。
細孔径が前記下限未満ではエチレンもプロピレンも通り抜けられなくなり、エチレンと活性点との作用が起こりにくくなり反応速度が低下する場合が考えられる。
酸素8員環構造または9員環構造とは、ゼオライトのもつ細孔がTO4単位(TはSi、P、Ge、Al、Ga等)8個または9個からなる環構造を意味する。酸素8員環構造または酸素9員環構造であれば、好ましい細孔径となり、高いプロピレン選択率が得られる。
なかでも細孔が酸素の8員環のみで構成されているゼオライトが好ましい。
酸素9員環を含みかつ酸素9員環以下の細孔だけを有するゼオライトとしては、具体的にInternational Zeolite Association(IZA)が規定するコードで表すと、NAT、RSN、STT等が挙げられる。
ここでフレームワーク密度(単位:T/nm3)とは、ゼオライトの単位体積(1nm3)当たりに存在するT原子(ゼオライトの骨格を構成する原子のうち、酸素以外の原子)の個数を意味し、この値はゼオライトの構造により決まるものである。
本発明のゼオライトの製造方法は、特に限定はなく、例えば米国特許第4544538号明細書に記載の製造方法のような公知の方法で製造することができる。一般的に水熱合成法により調製することが可能である。また水熱合成後にイオン交換、脱アルミニウム処理、含浸等で組成を変えたものも使用できる。
本発明において用いられるゼオライトは、ゼオライトの外表面の酸量が、ゼオライト全体の酸量に対して5%以下のゼオライトであり、通常ゼオライトの外表面酸量の割合を低下させて得ることができる。
全体酸量に対する外表面酸量の割合を低下させる方法としては、特に限定はないが、1)ゼオライトの外表面をシリル化する方法、2)ゼオライトに水蒸気処理(スチーミング)を行う方法、3)ゼオライトをジカルボン酸で処理する方法が挙げられる。
ゼオライトの外表面をシリル化する方法とは、触媒の活性成分のゼオライトに対して外表面のシリル化を行うことにより、外表面酸量を低下させる方法である。シリル化の方法は特に限定されるものではなく、公知の方法を適宜用いることができ、具体的にはアルコキシシランを用いた液相シリル化、またはクロロシランを用いた気相シリル化等で行うことができる。
気相シリル化の温度はシリル化剤によって適宜調整することができ、限定されるものではないが、通常20℃以上、好ましくは100℃以上である。また通常500℃以下で好ましくは400℃以下である。前記上限超過ではシリル化剤の分解、ゼオライトの骨格の崩壊等が起こる場合があり、前記下限未満ではシリル化反応が進行しない場合がある。
ゼオライトにスチーミングを行う方法は、特に限定はないが、スチーミング温度は通常400℃以上であり、好ましくは500℃以上である。又、通常700℃以下であり、好ましくは650℃以下である。前記下限未満ではスチーミングの効果が小さく、前記上限超過ではゼオライトの構造崩壊が起こる場合がある。
スチームはヘリウム、窒素等の不活性ガスで希釈して使用することもできる。スチーム濃度は特に限定されないが通常3体積%以上、好ましくは5体積%以上であり、上限はなく100%水蒸気で処理が可能である。
アルカリ土類金属を含む化合物の量はゼオライトに対して0.5重量%から45重量%が好ましい。さらに好ましくは3重量%から40重量%である。
又、スチーミングは、外表面の酸量を脱アルミニウムにより選択的に低減する目的で細孔内部に有機物が存在している状態で行ってもよい。有機物とは、特に限定はないが、ゼオライト合成時に使用する構造規定剤、及び反応によって生成するコークが挙げられる。これらの有機物のうち、構造規定剤は合成された状態でゼオライトの細孔内に存在している。また、コークは炭化水素を200℃以上の温度で触媒に流通させるといった方法で、細孔内部に存在させることができる。
ゼオライトをジカルボン酸で処理する方法としては、本願目的を達成する範囲においては特に限定はされない。ジカルボン酸は、ゼオライトの脱アルミニウムなど骨格中の金属の骨格からの脱離を促進することで、酸量を低減させると考えられるが、分子の大きさがゼオライト細孔に比較して大きいため、細孔に入り込むことが出来ず、外表面の酸量を選択的に低減することができる。
ジカルボン酸としてはシュウ酸、マロン酸、コハク酸、グルタル酸、アジピン酸、マレイン酸、フタル酸、イソフタル酸、フマル酸、酒石酸などが挙げられ、これらを混合して使用してもよい。この中ではシュウ酸が好ましい。
また、ジカルボン酸の処理は、外表面の酸量を脱アルミニウムにより選択的に低減する目的で細孔内部に有機物が存在している状態で行ってもよい。有機物とは、特に限定はないが、ゼオライト合成時に使用する構造規定剤、及び反応によって生成するコークが挙げられる。これらの有機物のうち、構造規定剤は合成された状態でゼオライトの細孔内に存在している。また、コークは炭化水素を200℃以上の温度で触媒に流通させるといった方法で、細孔内部に存在させることができる。
(1)反応方法
<反応原料>
原料となるエチレンは特に限定されるものではない。例えば、石油供給源から接触分解法または蒸気分解法等により製造されるエチレン、石炭のガス化により得られる水素/CO混合ガスを原料としてフィッシャートロプシュ合成を行うことにより得られるエチレン、エタンの脱水素または酸化脱水素で得られたものプロピレンのメタセシス反応およびホモロゲーション反応により得られるエチレン、MTO(Methanol to Olefin)反応によって得られるエチレン、エタノールの脱水反応から得られるエチレン、メタンの酸化カップリングで得られるエチレン等、公知の各種方法により得られるエチレンを任意に用いることができる。このとき各種製造方法に起因するエチレン以外の化合物を任意に混合した状態のものをそのまま用いてもよいし、精製したエチレンを用いてもよいが、好ましくは精製したエチレンである。
リサイクルするオレフィンとしては、通常エチレンだが、その他のオレフィンをリサイクルしても良い。原料となるオレフィンは低級オレフィンが好ましく、分岐鎖オレフィンはその分子の大きさからゼオライト細孔内への進入が困難であるため好ましくない。オレフィンとしては好ましくはエチレン、直鎖ブテンであり、最も好ましくはエチレンである。
本発明のエチレンは、反応器中で触媒と接触させ、プロピレンを製造することが好ましい。用いる反応器の形態に特に制限はないが、通常連続式の固定床反応器や流動床反応器が選ばれる。好ましくは流動床反応器である。
なお、流動床反応器に前述の触媒を充填する際、触媒層の温度分布を小さく抑えるために、石英砂、アルミナ、シリカ、シリカ-アルミナ等の、反応に不活性な粒状物を、触媒と混合して充填しても良い。この場合、石英砂等の反応に不活性な粒状物の使用量は特に制限はない。なお、この粒状物は、触媒との均一混合性の面から、触媒と同程度の粒径であることが好ましい。
反応器内には、エチレンの他に、ヘリウム、アルゴン、窒素、一酸化炭素、二酸化炭素、水素、水、パラフィン類、メタン等の炭化水素類、芳香族化合物類、および、それらの混合物など、反応に不活性な気体を存在させることができるが、この中でも水(水蒸気)が共存しているのが好ましい。
<基質濃度>
反応器に供給する全供給成分中のエチレンの濃度(即ち、基質濃度)に関して特に制限はないが、通常エチレンは全供給成分中、90モル%以下である。好ましくは70モル%以下である。また通常5モル%以上である。基質濃度が前記上限超過では、芳香族化合物やパラフィン類の生成が顕著になり、プロピレンの選択率が低下する傾向がある。基質濃度が前記下限未満では、反応速度が遅くなるため、多量の触媒が必要となり、反応器が大きくなりすぎる傾向がある。
従って、このような基質濃度となるように、必要に応じて以下に記載する希釈剤でエチレンを希釈することが好ましい。
ここで言う空間速度とは、触媒(触媒活性成分)の重量当たりの反応原料であるエチレンの流量(重量/時間)である。ここで触媒の重量とは触媒の造粒・成型に使用する不活性成分やバインダーを含まない触媒活性成分の重量である。
反応温度は、エチレンが触媒と接触してプロピレンが製造されれば特に制限されるものではないが、通常約200℃以上、好ましくは300℃以上であり、通常700℃以下、好ましくは600℃以下である。反応温度が前記下限未満では、反応速度が低く、未反応原料が多く残る傾向となり、さらにプロピレンの収率も低下する傾向がある。一方で反応温度が前記上限超過ではプロピレンの収率が著しく低下する場合がある。
反応圧力は特に制限されるものではないが、通常2MPa(絶対圧、以下同様)以下、好ましくは1MPa以下であり、より好ましくは0.7MPa以下である。また、通常1kPa以上、好ましくは50kPa以上である。反応圧力が前記上限超過ではパラフィン類等の好ましくない副生成物の生成量が増え、プロピレンの選択率が低下する傾向がある。反応圧力が前記下限未満では反応速度が遅くなる傾向がある。
本発明においては、転化率は特に制限されるものではないが、通常エチレンの転化率が20%以上、好ましくは40%以上、より好ましくは50%以上、また通常95%以下、好ましくは90%以下となるような条件で反応を行うことが好ましい。
この転化率が前記下限値未満では、未反応のエチレンが多く、プロピレン収率が低いため好ましくないことがある。一方、前記上限値以上では、パラフィン類等の望ましくない副生成物が増え、プロピレン選択率が低下するため好ましくないことがある。
流動床反応器で反応を行う場合には、触媒の反応器内の滞留時間と再生器内での滞留時間を調整することにより、好ましい転化率で運転することができる。
なお、転化率は次の式により算出される値である。
エチレン転化率(%)=〔[反応器入口エチレン(mol)-反応器出口エチレン(mol)]/反応器入口エチレン(mol)〕×100
本明細における選択率とは、以下の各式により算出される値である。下記の各式において、プロピレン、ブテン、C5+、パラフィンまたは芳香族化合物由来カーボン(mol)とは、各成分を構成する炭素原子のモル数を意味する。尚、パラフィンは炭素数1から3のパラフィンの合計、芳香族化合物はベンゼン、トルエン、キシレンの合計、C5+は前記芳香族化合物を除いたC5以上の炭化水素の合計値である。
プロピレン選択率(%)=〔反応器出口プロピレン由来カーボン(mol)/[反応器出口総カーボン(mol)-反応器出口エチレン由来カーボン(mol)]〕×100
ブテン選択率(%)=〔反応器出口ブテン由来カーボン(mol)/[反応器出口総カーボン(mol)-反応器出口エチレン由来カーボン(mol)]〕×100
C5+選択率(%)=〔反応器出口C5+由来カーボン(mol)/[反応器出口総カーボン(mol)-反応器出口エチレン由来カーボン(mol)]〕×100
パラフィン選択率(%)=〔反応器出口パラフィン由来カーボン(mol)/[反応器出口総カーボン(mol)-反応器出口エチレン由来カーボン(mol)]〕×100
芳香族化合物選択率(%)=〔反応器出口芳香族化合物由来カーボン(mol)/[反応器出口総カーボン(mol)-反応器出口エチレン由来カーボン(mol)]〕×100
なお本明細における収率とは、前記エチレン転化率と、生成した各成分の選択率との積により求められ、例えば具体的にプロピレン収率は、次の式で表される値である。
プロピレン収率(%)=(エチレン転化率(%)×プロピレン選択率(%))/100
反応器出口ガス(反応器流出物)としては、反応生成物であるプロピレン、未反応のエチレン、副生成物および希釈剤を含む混合ガスが得られる。該混合ガス中のプロピレン濃度は通常1重量%以上、好ましくは2重量%以上であり、通常95重量%以下、好ましくは80重量%以下である。
この混合ガス中には通常エチレンが含まれるが、この混合ガス中のエチレンはその少なくとも一部を反応器にリサイクルして反応原料として再利用することが好ましい。
なお、副生成物としては炭素数が4以上のオレフィン類およびパラフィン類が挙げられる。
(調製例1)
CHA構造を有するプロトン型のアルミノシリケート(SiO2/Al2O3=37(モル比)、細孔径0.38nm)に対してテトラエトキシシランでシリル化を行った。アルミノシリケート1gに対して、溶媒のヘキサメチルジシロキサン10ml、シリル化剤のテトラエトキシシラン5mlを加えて100℃で撹拌条件下、6時間のリフラックス処理を行った。処理後、濾過によって固液を分離し、得られたアルミノシリケートを100℃で2時間乾燥した。
CHA構造を有するプロトン型のアルミノシリケート(SiO2/Al2O3=37(モル比)、細孔径0.38nm)に対してジメトキシジメチルシランでシリル化を行った。アルミノシリケート1gに対して、溶媒のヘキサメチルジシロキサン10ml、シリル化剤のジメトキシジメチルシラン5mlを加えて100℃で撹拌条件下、6時間のリフラックス処理を行った。処理後、濾過によって固液を分離し、得られたアルミノシリケートを100℃で2時間乾燥した。
CHA構造を有するプロトン型のアルミノシリケート(SiO2/Al2O3=37(モル比)、細孔径0.38nm)に対してスチーミングを行った。アルミノシリケートに対して600℃で30体積%のスチーム及び70体積%の窒素の組成のガスを6時間流通させた。
CHA構造を有するプロトン型のアルミノシリケート(SiO2/Al2O3=37(モル比)、細孔径0.38nm)と炭酸カルシウムを物理混合してスチーミングを行った。炭酸カルシウムはゼオライトに対して36重量%の比率で混合した。アルミノシリケートと炭酸カルシウムの物理混合物に600℃で30体積%のスチーム及び70体積%の窒素の組成のガスを6時間流通させた。
調製例1~4との比較として、未処理の触媒CHA構造を有するプロトン型のアルミノシリケート(SiO2/Al2O3=37(モル比)、細孔径0.38nm)を用意した。
<酸量測定>
調製例1~5のアルミノシリケートについて、全体酸量、外表面酸量をそれぞれ、NH3-TPD、Pyridine-TPDにて測定した。測定には日本ベル社製 自動昇温脱離分析装置TP5500を用い、以下の通りに行った。
(全体酸量)
試料のアルミノシリケート30~50mgを、ヘリウム雰囲気下500℃で1時間放置乾燥して有機物、水などの吸着物を脱離させた。その後、100℃にて5体積%アンモニア/ヘリウム下で15分間保持し、試料にアンモニアを吸着させた。引き続き100℃で水蒸気に接触させて余剰アンモニアを除き、アンモニアを吸着させたアルミノシリケートを得た。次いでアンモニアを吸着させたアルミノシリケートを、ヘリウム雰囲気下、10℃/分で昇温して、100~800℃で脱離したアンモニア量を質量分析法によって検出した。単位重量当たりのアンモニア脱離量をアルミノシリケート試料の全体酸量として表1に示した。
(外表面酸量)
試料のアルミノシリケート30mgを、真空下500℃で1時間放置乾燥して有機物、水などの吸着物を脱離させた。その後、150℃にて100%ピリジン蒸気下で15分間保持し、試料にピリジンを吸着させた。引き続き、減圧排気及びヘリウムフローで(ゼオライトの酸点に吸着させたピリジンが脱離しない程度の減圧条件下で排気しながら、かつヘリウムを流通しながら)余剰ピリジンを除き、ピリジンを吸着させたアルミノシリケートを得た。次いでピリジンを吸着させたアルミノシリケートを、ヘリウム雰囲気下、10℃/分で昇温して、150~800℃で脱離したピリジンの量を質量分析法によって検出した。単位重量当たりのピリジン脱離量をアルミノシリケート試料の外表面酸量として表1に示した。また、全体酸量に対する、外表面酸量の割合を表1に示した。
(実施例1~4、比較例1)
反応には、常圧固定床流通反応装置を用い、内径6mmの石英製反応管に、調製例1から5のアルミノシリケート100mgと石英砂400mgの混合物を充填した。エチレン30体積%、窒素70体積%の混合ガスをエチレンの重量空間速度が0.73Hr-1なるように反応器に供給し、400℃、0.1MPaで反応を行った。反応開始後、未修飾触媒(比較例1)は2.75時間後、修飾触媒(実施例1~4)は1.92時間後にガスクロマトグラフィーで生成物の分析を行った。結果を表1に示した。
反応には、常圧固定床流通反応装置を用い、内径6mmの石英製反応管に、調製例1のアルミノシリケート100mgと石英砂400mgの混合物を充填した。エチレン30体積%、窒素70体積%の混合ガスをエチレンの重量空間速度が0.36Hr-1なるように反応器に供給し、350℃、0.1MPaで反応を行った。反応開始後、1.92時間後および3.17時間後にガスクロマトグラフィーで生成物の分析を行った。結果を表1に示した。
また、表1の結果より、実施例5及び6の触媒は、50%以上の高いエチレン転化率にも関わらず、80%以上の高いプロピレン選択率が得られることが分かる。
Claims (18)
- エチレンと触媒とを接触させる工程を含み、
前記触媒の活性成分としてゼオライトを含み、
前記ゼオライトの外表面の酸量が、ゼオライト全体の酸量に対して5%以下であることを特徴とするプロピレンの製造方法。 - 前記ゼオライトの外表面の酸量が、下記(I)により定義されるピリジン脱離量で表されることを特徴とする請求項1に記載のプロピレンの製造方法。
(I)前処理としてゼオライトを真空下500℃で1時間乾燥させた後、前処理したゼオライトを150℃でピリジン蒸気と接触させてゼオライトにピリジンを吸着させ、150℃で減圧排気及びヘリウムフローにより該ゼオライトから余剰ピリジンを除いて得られた、ピリジンを吸着したゼオライトの、昇温速度10℃/分の昇温脱離法による150~800℃におけるゼオライト単位重量当たりのピリジンの脱離量。 - 前記ゼオライトの全体の酸量が、下記(II)により定義されるアンモニア脱離量で表されることを特徴とする請求項1又は2に記載のプロピレンの製造方法。
(II)前処理としてゼオライトをヘリウムフロー下500℃で1時間乾燥させた後、前処理したゼオライトを100℃で5体積%アンモニア/ヘリウムと接触させてゼオライトにアンモニアを吸着させ、得られたゼオライトを100℃で水蒸気と接触させ該ゼオライトから余剰アンモニアを除いて得られた、アンモニアを吸着したゼオライトの、昇温速度10℃/分の昇温脱離法による100~800℃におけるゼオライト単位重量当たりのアンモニアの脱離量。 - 前記ゼオライトが、0.5nm未満の細孔径を有することを特徴とする請求項1から3のいずれか1項に記載のプロピレンの製造方法。
- 前記ゼオライトが酸素8員環構造または酸素9員環構造を有することを特徴とする請求項1から4のいずれか1項に記載のプロピレンの製造方法。
- 前記ゼオライトの骨格構造がCHA型構造であることを特徴とする請求項1から5のいずれか1項に記載のプロピレンの製造方法。
- 前記ゼオライトの外表面がシリル化されていることを特徴とする請求項1から6のいずれか1項に記載のプロピレンの製造方法。
- 前記ゼオライトが水蒸気処理されていることを特徴とする請求項1から6のいずれか1項に記載のプロピレンの製造方法。
- 前記水蒸気処理の温度が400~700℃であることを特徴とする請求項8に記載のプロピレンの製造方法。
- 前記ゼオライトがアルカリ土類金属を含む化合物と混合後に水蒸気処理されていることを特徴とする請求項8又は9に記載のプロピレンの製造方法。
- 請求項1から10のいずれか1項に記載の製造方法により得られたプロピレンを重合する工程を含むことを特徴とするポリプロピレンの製造方法。
- 0.5nm未満の細孔径を有し、外表面の酸量が、全体の酸量に対して5%以下であることを特徴とするゼオライト。
- アルミノシリケートである請求項12に記載のゼオライト。
- 酸素8員環構造または酸素9員環構造を有する請求項12または13に記載のゼオライト。
- CHA型構造の骨格構造を有する請求項12から14のいずれか1項に記載のゼオライト。
- シリル化された外表面を有する請求項12から15のいずれか1項に記載のゼオライト。
- 請求項12から16のいずれか1項に記載のゼオライトを含む触媒。
- 請求項12から16のいずれか1項に記載のゼオライトを含むオレフィン製造用触媒。
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BRPI1015393-4A BRPI1015393B1 (pt) | 2009-05-08 | 2010-04-28 | Processo de produção de propileno, zeólita e catalisador |
JP2011512347A JP5614401B2 (ja) | 2009-05-08 | 2010-04-28 | プロピレンの製造方法 |
CN201080020934.1A CN102421727B (zh) | 2009-05-08 | 2010-04-28 | 丙烯制造方法 |
US13/291,290 US8759598B2 (en) | 2009-05-08 | 2011-11-08 | Production process of propylene |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2009-113596 | 2009-05-08 | ||
JP2009113596 | 2009-05-08 |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US13/291,290 Continuation US8759598B2 (en) | 2009-05-08 | 2011-11-08 | Production process of propylene |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2010128644A1 true WO2010128644A1 (ja) | 2010-11-11 |
Family
ID=43050145
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2010/057632 WO2010128644A1 (ja) | 2009-05-08 | 2010-04-28 | プロピレンの製造方法 |
Country Status (5)
Country | Link |
---|---|
US (1) | US8759598B2 (ja) |
JP (1) | JP5614401B2 (ja) |
CN (1) | CN102421727B (ja) |
BR (1) | BRPI1015393B1 (ja) |
WO (1) | WO2010128644A1 (ja) |
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2013063865A (ja) * | 2011-09-15 | 2013-04-11 | Mitsubishi Chemicals Corp | シリル化されたcha型構造を有するh型ゼオライトの製造方法 |
JP2013075276A (ja) * | 2011-09-30 | 2013-04-25 | Mitsubishi Chemicals Corp | プロピレン製造用触媒の製造方法及びプロピレンの製造方法 |
JP2014047175A (ja) * | 2012-08-31 | 2014-03-17 | Mitsubishi Chemicals Corp | プロピレンの製造方法 |
WO2015005407A1 (ja) | 2013-07-09 | 2015-01-15 | 三菱化学株式会社 | ゼオライトの製造方法 |
JP2015187064A (ja) * | 2014-03-13 | 2015-10-29 | 三菱化学株式会社 | ゼオライト成形体 |
JP2015193599A (ja) * | 2014-03-20 | 2015-11-05 | 三菱化学株式会社 | プロピレン及び直鎖ブテンの製造方法 |
JP2015535800A (ja) * | 2012-09-28 | 2015-12-17 | パシフィック インダストリアル デベロップメント コーポレイション | 選択触媒還元反応における触媒として使用するためのstt型ゼオライトの調製方法 |
JP2018145085A (ja) * | 2017-03-03 | 2018-09-20 | 東ソー株式会社 | ゼオライトおよびその製造方法 |
Families Citing this family (30)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
MX2012013521A (es) | 2010-05-24 | 2013-04-08 | Siluria Technologies Inc | Catalizadores de nanoalambre, su preparacion y uso de los mismos. |
BR112013030226A2 (pt) | 2011-05-24 | 2022-05-10 | Siluria Technologies Inc | Catalisadores para acoplamento oxidativo de metano |
EA029490B1 (ru) | 2011-11-29 | 2018-04-30 | Силурия Текнолоджиз, Инк. | Катализаторы из нанопроволоки и способы их применения и получения |
US9133079B2 (en) | 2012-01-13 | 2015-09-15 | Siluria Technologies, Inc. | Process for separating hydrocarbon compounds |
US9446397B2 (en) | 2012-02-03 | 2016-09-20 | Siluria Technologies, Inc. | Method for isolation of nanomaterials |
AU2013266250B2 (en) | 2012-05-24 | 2017-07-06 | Lummus Technology Llc | Oxidative coupling of methane systems and methods |
US20140121433A1 (en) | 2012-05-24 | 2014-05-01 | Siluria Technologies, Inc. | Catalytic forms and formulations |
US9670113B2 (en) | 2012-07-09 | 2017-06-06 | Siluria Technologies, Inc. | Natural gas processing and systems |
WO2014089479A1 (en) | 2012-12-07 | 2014-06-12 | Siluria Technologies, Inc. | Integrated processes and systems for conversion of methane to multiple higher hydrocarbon products |
US20140274671A1 (en) | 2013-03-15 | 2014-09-18 | Siluria Technologies, Inc. | Catalysts for petrochemical catalysis |
WO2015081122A2 (en) | 2013-11-27 | 2015-06-04 | Siluria Technologies, Inc. | Reactors and systems for oxidative coupling of methane |
CA2935937A1 (en) | 2014-01-08 | 2015-07-16 | Siluria Technologies, Inc. | Ethylene-to-liquids systems and methods |
CA3148421C (en) | 2014-01-09 | 2024-02-13 | Lummus Technology Llc | Oxidative coupling of methane implementations for olefin production |
US10377682B2 (en) | 2014-01-09 | 2019-08-13 | Siluria Technologies, Inc. | Reactors and systems for oxidative coupling of methane |
WO2015168601A2 (en) | 2014-05-02 | 2015-11-05 | Siluria Technologies, Inc. | Heterogeneous catalysts |
HUE054014T2 (hu) | 2014-09-17 | 2021-08-30 | Lummus Technology Inc | Katalizátorok metán oxidatív csatolására és etán oxidatív dehidrogenálására |
US10472300B2 (en) * | 2014-12-31 | 2019-11-12 | Total Research & Technology Feluy | Process for preparing olefins by dehydrating alcohols with less side effects comprising addition of sulfur containing compounds |
US9334204B1 (en) | 2015-03-17 | 2016-05-10 | Siluria Technologies, Inc. | Efficient oxidative coupling of methane processes and systems |
US10793490B2 (en) | 2015-03-17 | 2020-10-06 | Lummus Technology Llc | Oxidative coupling of methane methods and systems |
US20160289143A1 (en) | 2015-04-01 | 2016-10-06 | Siluria Technologies, Inc. | Advanced oxidative coupling of methane |
US9328297B1 (en) | 2015-06-16 | 2016-05-03 | Siluria Technologies, Inc. | Ethylene-to-liquids systems and methods |
WO2017065947A1 (en) | 2015-10-16 | 2017-04-20 | Siluria Technologies, Inc. | Separation methods and systems for oxidative coupling of methane |
EP4071131A1 (en) | 2016-04-13 | 2022-10-12 | Lummus Technology LLC | Apparatus and method for exchanging heat |
US10544068B2 (en) | 2016-08-16 | 2020-01-28 | Iran Polymer And Petrochemical Institute | Catalytic process for producing olefins |
WO2018118105A1 (en) | 2016-12-19 | 2018-06-28 | Siluria Technologies, Inc. | Methods and systems for performing chemical separations |
HUE064375T2 (hu) | 2017-05-23 | 2024-03-28 | Lummus Technology Inc | Metán oxidatív csatolási folyamatainak integrálása |
WO2019010498A1 (en) | 2017-07-07 | 2019-01-10 | Siluria Technologies, Inc. | SYSTEMS AND METHODS FOR OXIDIZING METHANE COUPLING |
KR102375335B1 (ko) | 2020-04-10 | 2022-03-16 | 한국화학연구원 | 에틸렌으로부터 프로필렌 제조용 촉매 및 그 제조방법 |
FR3137311A1 (fr) | 2022-06-29 | 2024-01-05 | IFP Energies Nouvelles | Procédé de traitement d’un catalyseur comprenant une zéolithe |
FR3137312A1 (fr) | 2022-06-29 | 2024-01-05 | IFP Energies Nouvelles | Procédé de traitement d’un catalyseur comprenant une zéolithe |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH10151351A (ja) * | 1996-11-12 | 1998-06-09 | Phillips Petroleum Co | 炭化水素の転換用触媒組成物 |
JP2007509933A (ja) * | 2003-10-31 | 2007-04-19 | エクソンモービル リサーチ アンド エンジニアリング カンパニー | 8員環ゼオライトを用いる軽質炭化水素の分離 |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN1009100B (zh) * | 1983-10-25 | 1990-08-08 | 国际壳牌研究有限公司 | 丙烯连续聚合的方法 |
CN1004878B (zh) * | 1987-08-08 | 1989-07-26 | 中国石油化工总公司 | 制取低碳烯烃的烃类催化转化方法 |
DE69100534T3 (de) * | 1990-12-13 | 2003-04-24 | Tosoh Corp | Reinigungsmethode von organische Ketonlösungsmittel enthaltenden Abgasen |
US6429348B1 (en) * | 1998-05-05 | 2002-08-06 | Exxonmobil Chemical Patents, Inc. | Method for selectively producing propylene by catalytically cracking an olefinic hydrocarbon feedstock |
EP1061116A1 (en) * | 1999-06-16 | 2000-12-20 | Fina Research S.A. | Production of olefins |
CA2497309A1 (en) * | 2002-08-29 | 2004-03-11 | Albemarle Netherlands B.V. | Catalyst for the production of light olefins |
CN100494129C (zh) * | 2003-12-12 | 2009-06-03 | 三菱化学株式会社 | 制备丙烯的方法 |
JP5135839B2 (ja) | 2006-03-30 | 2013-02-06 | 三菱化学株式会社 | プロピレンの製造方法 |
-
2010
- 2010-04-28 BR BRPI1015393-4A patent/BRPI1015393B1/pt active IP Right Grant
- 2010-04-28 JP JP2011512347A patent/JP5614401B2/ja active Active
- 2010-04-28 WO PCT/JP2010/057632 patent/WO2010128644A1/ja active Application Filing
- 2010-04-28 CN CN201080020934.1A patent/CN102421727B/zh active Active
-
2011
- 2011-11-08 US US13/291,290 patent/US8759598B2/en active Active
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH10151351A (ja) * | 1996-11-12 | 1998-06-09 | Phillips Petroleum Co | 炭化水素の転換用触媒組成物 |
JP2007509933A (ja) * | 2003-10-31 | 2007-04-19 | エクソンモービル リサーチ アンド エンジニアリング カンパニー | 8員環ゼオライトを用いる軽質炭化水素の分離 |
Non-Patent Citations (1)
Title |
---|
TOSHIHIDE BABA ET AL.: "Shin Energy no Kaihatsu Part 2 -Biomass Selective synthesis of propene by the conversion of ethene or ethanol using SAPO-34", GEKKAN FINE CHEMICAL, vol. 37, no. 4, 15 March 2008 (2008-03-15), pages 66 - 74 * |
Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2013063865A (ja) * | 2011-09-15 | 2013-04-11 | Mitsubishi Chemicals Corp | シリル化されたcha型構造を有するh型ゼオライトの製造方法 |
JP2013075276A (ja) * | 2011-09-30 | 2013-04-25 | Mitsubishi Chemicals Corp | プロピレン製造用触媒の製造方法及びプロピレンの製造方法 |
JP2014047175A (ja) * | 2012-08-31 | 2014-03-17 | Mitsubishi Chemicals Corp | プロピレンの製造方法 |
JP2015535800A (ja) * | 2012-09-28 | 2015-12-17 | パシフィック インダストリアル デベロップメント コーポレイション | 選択触媒還元反応における触媒として使用するためのstt型ゼオライトの調製方法 |
WO2015005407A1 (ja) | 2013-07-09 | 2015-01-15 | 三菱化学株式会社 | ゼオライトの製造方法 |
JP2015187064A (ja) * | 2014-03-13 | 2015-10-29 | 三菱化学株式会社 | ゼオライト成形体 |
JP2015193599A (ja) * | 2014-03-20 | 2015-11-05 | 三菱化学株式会社 | プロピレン及び直鎖ブテンの製造方法 |
JP2018145085A (ja) * | 2017-03-03 | 2018-09-20 | 東ソー株式会社 | ゼオライトおよびその製造方法 |
JP7119397B2 (ja) | 2017-03-03 | 2022-08-17 | 東ソー株式会社 | ゼオライトおよびその製造方法 |
Also Published As
Publication number | Publication date |
---|---|
CN102421727A (zh) | 2012-04-18 |
US8759598B2 (en) | 2014-06-24 |
BRPI1015393B1 (pt) | 2018-08-14 |
BRPI1015393A2 (pt) | 2016-04-19 |
CN102421727B (zh) | 2014-10-15 |
US20120059139A1 (en) | 2012-03-08 |
JP5614401B2 (ja) | 2014-10-29 |
JPWO2010128644A1 (ja) | 2012-11-01 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
JP5614401B2 (ja) | プロピレンの製造方法 | |
JP5545114B2 (ja) | 触媒の再生方法 | |
JP6693095B2 (ja) | Aei型ゼオライト、その製造方法、及びそれを用いた低級オレフィンの製造方法 | |
US10201806B2 (en) | Catalyst and process for the conversion of oxygenates to olefins | |
US6841510B2 (en) | Treatment of molecular sieves with silicon containing compounds | |
JP6699336B2 (ja) | Aei型アルミノケイ酸塩の製造方法、該aei型アルミノケイ酸塩を用いたプロピレン及び直鎖ブテンの製造方法 | |
JP5978887B2 (ja) | プロピレン及び直鎖ブテンの製造方法 | |
JP7087636B2 (ja) | ゼオライト触媒の処理方法及び低級オレフィンの製造方法 | |
JP2011079815A (ja) | p−キシレンの製造方法 | |
JP5811750B2 (ja) | プロピレン製造用触媒の製造方法及びプロピレンの製造方法 | |
JP2021165226A (ja) | プロピレン及び直鎖ブテンの製造方法 | |
JP2011079818A (ja) | プロピレンの製造方法 | |
JP5685870B2 (ja) | プロピレンの製造方法 | |
JP5499918B2 (ja) | 触媒の再生方法 | |
JP6641705B2 (ja) | プロピレン及び直鎖ブテンの製造方法 | |
JP6977251B2 (ja) | Aei型メタロケイ酸塩、その製造方法、及びそれを用いたプロピレン及び直鎖ブテンの製造方法 | |
JP2018145085A (ja) | ゼオライトおよびその製造方法 | |
WO2019124519A1 (ja) | エチレンの製造方法 | |
JP5720508B2 (ja) | シリル化されたcha型構造を有するh型ゼオライトの製造方法 | |
JP5023639B2 (ja) | プロピレンの製造方法 | |
JP7218553B2 (ja) | 銀イオン担持ゼオライト触媒の再生方法 | |
JP2015131778A (ja) | プロピレンの製造方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 201080020934.1 Country of ref document: CN |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 10772163 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 2011512347 Country of ref document: JP Kind code of ref document: A |
|
WWE | Wipo information: entry into national phase |
Ref document number: 8037/CHENP/2011 Country of ref document: IN |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 10772163 Country of ref document: EP Kind code of ref document: A1 |
|
REG | Reference to national code |
Ref country code: BR Ref legal event code: B01A Ref document number: PI1015393 Country of ref document: BR |
|
ENP | Entry into the national phase |
Ref document number: PI1015393 Country of ref document: BR Kind code of ref document: A2 Effective date: 20111103 |