WO1997003751A1 - Catalyseur conçu pour la preparation d'esters carboxyliques - Google Patents
Catalyseur conçu pour la preparation d'esters carboxyliques Download PDFInfo
- Publication number
- WO1997003751A1 WO1997003751A1 PCT/JP1996/002008 JP9602008W WO9703751A1 WO 1997003751 A1 WO1997003751 A1 WO 1997003751A1 JP 9602008 W JP9602008 W JP 9602008W WO 9703751 A1 WO9703751 A1 WO 9703751A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- catalyst
- lead
- palladium
- reaction
- reactor
- Prior art date
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 649
- 150000001733 carboxylic acid esters Chemical class 0.000 title claims abstract description 63
- 238000002360 preparation method Methods 0.000 title description 13
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims abstract description 507
- 239000011133 lead Substances 0.000 claims abstract description 417
- 238000000034 method Methods 0.000 claims abstract description 199
- 229910052763 palladium Inorganic materials 0.000 claims abstract description 186
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 158
- -1 alkali metal salts Chemical class 0.000 claims abstract description 137
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 100
- WABPQHHGFIMREM-UHFFFAOYSA-N lead(0) Chemical compound [Pb] WABPQHHGFIMREM-UHFFFAOYSA-N 0.000 claims abstract description 88
- 238000002441 X-ray diffraction Methods 0.000 claims abstract description 86
- 150000001299 aldehydes Chemical class 0.000 claims abstract description 83
- 238000000634 powder X-ray diffraction Methods 0.000 claims abstract description 69
- 150000002611 lead compounds Chemical class 0.000 claims abstract description 48
- 229910001882 dioxygen Inorganic materials 0.000 claims abstract description 45
- 150000002941 palladium compounds Chemical class 0.000 claims abstract description 43
- 150000002500 ions Chemical class 0.000 claims abstract description 41
- 229910052783 alkali metal Inorganic materials 0.000 claims abstract description 37
- 229910000765 intermetallic Inorganic materials 0.000 claims abstract description 36
- 239000012018 catalyst precursor Substances 0.000 claims abstract description 35
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims abstract description 33
- 238000006243 chemical reaction Methods 0.000 claims description 359
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 306
- 238000011282 treatment Methods 0.000 claims description 144
- 239000000203 mixture Substances 0.000 claims description 127
- 229910052751 metal Inorganic materials 0.000 claims description 122
- 239000002184 metal Substances 0.000 claims description 122
- 239000001301 oxygen Substances 0.000 claims description 118
- 229910052760 oxygen Inorganic materials 0.000 claims description 118
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 109
- 235000014113 dietary fatty acids Nutrition 0.000 claims description 87
- 229930195729 fatty acid Natural products 0.000 claims description 87
- 239000000194 fatty acid Substances 0.000 claims description 87
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 84
- 238000004519 manufacturing process Methods 0.000 claims description 76
- 150000004665 fatty acids Chemical class 0.000 claims description 75
- 229910052782 aluminium Inorganic materials 0.000 claims description 69
- 238000000026 X-ray photoelectron spectrum Methods 0.000 claims description 63
- 230000036961 partial effect Effects 0.000 claims description 63
- 230000009467 reduction Effects 0.000 claims description 56
- 239000000126 substance Substances 0.000 claims description 47
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 45
- STNJBCKSHOAVAJ-UHFFFAOYSA-N Methacrolein Chemical group CC(=C)C=O STNJBCKSHOAVAJ-UHFFFAOYSA-N 0.000 claims description 45
- OAKJQQAXSVQMHS-UHFFFAOYSA-N Hydrazine Chemical compound NN OAKJQQAXSVQMHS-UHFFFAOYSA-N 0.000 claims description 44
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 claims description 44
- 150000003839 salts Chemical class 0.000 claims description 44
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 38
- 239000007789 gas Substances 0.000 claims description 37
- 239000000377 silicon dioxide Substances 0.000 claims description 35
- 239000002904 solvent Substances 0.000 claims description 32
- HGINCPLSRVDWNT-UHFFFAOYSA-N Acrolein Chemical compound C=CC=O HGINCPLSRVDWNT-UHFFFAOYSA-N 0.000 claims description 30
- 239000003638 chemical reducing agent Substances 0.000 claims description 28
- 150000001875 compounds Chemical class 0.000 claims description 28
- 239000011777 magnesium Substances 0.000 claims description 28
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 27
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 claims description 22
- 235000019253 formic acid Nutrition 0.000 claims description 22
- 229910052749 magnesium Inorganic materials 0.000 claims description 21
- 150000001298 alcohols Chemical class 0.000 claims description 20
- 238000007254 oxidation reaction Methods 0.000 claims description 20
- 230000003647 oxidation Effects 0.000 claims description 19
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 17
- RVPVRDXYQKGNMQ-UHFFFAOYSA-N lead(2+) Chemical compound [Pb+2] RVPVRDXYQKGNMQ-UHFFFAOYSA-N 0.000 claims description 15
- 229910052710 silicon Inorganic materials 0.000 claims description 15
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 14
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 12
- 239000010703 silicon Substances 0.000 claims description 12
- 150000001768 cations Chemical class 0.000 claims description 11
- 239000007800 oxidant agent Substances 0.000 claims description 9
- 239000000395 magnesium oxide Substances 0.000 claims description 8
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 claims description 4
- 241000255925 Diptera Species 0.000 claims description 3
- 230000033116 oxidation-reduction process Effects 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims 5
- 150000007524 organic acids Chemical class 0.000 claims 2
- 239000006227 byproduct Substances 0.000 abstract description 51
- 230000008569 process Effects 0.000 abstract description 12
- 125000001931 aliphatic group Chemical group 0.000 abstract description 9
- 230000003213 activating effect Effects 0.000 abstract description 8
- 239000000543 intermediate Substances 0.000 description 178
- VVQNEPGJFQJSBK-UHFFFAOYSA-N Methyl methacrylate Chemical compound COC(=O)C(C)=C VVQNEPGJFQJSBK-UHFFFAOYSA-N 0.000 description 145
- 238000001994 activation Methods 0.000 description 129
- TZIHFWKZFHZASV-UHFFFAOYSA-N methyl formate Chemical compound COC=O TZIHFWKZFHZASV-UHFFFAOYSA-N 0.000 description 126
- 230000004913 activation Effects 0.000 description 123
- 239000000243 solution Substances 0.000 description 114
- 235000002639 sodium chloride Nutrition 0.000 description 105
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 82
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 81
- 239000007795 chemical reaction product Substances 0.000 description 76
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 63
- 238000006722 reduction reaction Methods 0.000 description 52
- BAPJBEWLBFYGME-UHFFFAOYSA-N Methyl acrylate Chemical compound COC(=O)C=C BAPJBEWLBFYGME-UHFFFAOYSA-N 0.000 description 50
- 239000007864 aqueous solution Substances 0.000 description 40
- 239000007791 liquid phase Substances 0.000 description 39
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 39
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 39
- 229940046892 lead acetate Drugs 0.000 description 37
- 230000000052 comparative effect Effects 0.000 description 36
- 238000005755 formation reaction Methods 0.000 description 36
- 229910002027 silica gel Inorganic materials 0.000 description 36
- 239000000741 silica gel Substances 0.000 description 36
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 29
- 235000011121 sodium hydroxide Nutrition 0.000 description 27
- 239000012535 impurity Substances 0.000 description 25
- 150000002681 magnesium compounds Chemical class 0.000 description 25
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 24
- RLJMLMKIBZAXJO-UHFFFAOYSA-N lead nitrate Chemical compound [O-][N+](=O)O[Pb]O[N+]([O-])=O RLJMLMKIBZAXJO-UHFFFAOYSA-N 0.000 description 23
- PIBWKRNGBLPSSY-UHFFFAOYSA-L palladium(II) chloride Chemical compound Cl[Pd]Cl PIBWKRNGBLPSSY-UHFFFAOYSA-L 0.000 description 22
- 230000007547 defect Effects 0.000 description 21
- 238000011068 loading method Methods 0.000 description 20
- 230000003197 catalytic effect Effects 0.000 description 19
- 229910001220 stainless steel Inorganic materials 0.000 description 19
- 239000010935 stainless steel Substances 0.000 description 19
- 239000002253 acid Substances 0.000 description 18
- 230000000694 effects Effects 0.000 description 18
- 239000002245 particle Substances 0.000 description 17
- 238000003756 stirring Methods 0.000 description 17
- 239000013078 crystal Substances 0.000 description 16
- 239000007788 liquid Substances 0.000 description 16
- 230000015572 biosynthetic process Effects 0.000 description 15
- 239000001257 hydrogen Substances 0.000 description 15
- 229910052739 hydrogen Inorganic materials 0.000 description 15
- 239000002994 raw material Substances 0.000 description 14
- LIVNPJMFVYWSIS-UHFFFAOYSA-N silicon monoxide Inorganic materials [Si-]#[O+] LIVNPJMFVYWSIS-UHFFFAOYSA-N 0.000 description 14
- 229910052757 nitrogen Inorganic materials 0.000 description 13
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 12
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 12
- 230000001276 controlling effect Effects 0.000 description 12
- YIXJRHPUWRPCBB-UHFFFAOYSA-N magnesium nitrate Chemical compound [Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O YIXJRHPUWRPCBB-UHFFFAOYSA-N 0.000 description 12
- 230000008901 benefit Effects 0.000 description 11
- 229910052571 earthenware Inorganic materials 0.000 description 11
- 238000005259 measurement Methods 0.000 description 11
- 241000894007 species Species 0.000 description 11
- 150000001340 alkali metals Chemical class 0.000 description 10
- 238000010304 firing Methods 0.000 description 10
- 150000004679 hydroxides Chemical class 0.000 description 10
- CERQOIWHTDAKMF-UHFFFAOYSA-N Methacrylic acid Chemical compound CC(=C)C(O)=O CERQOIWHTDAKMF-UHFFFAOYSA-N 0.000 description 9
- 238000000354 decomposition reaction Methods 0.000 description 9
- 230000007423 decrease Effects 0.000 description 9
- 238000004090 dissolution Methods 0.000 description 9
- 238000011156 evaluation Methods 0.000 description 9
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- 230000006641 stabilisation Effects 0.000 description 9
- 238000011105 stabilization Methods 0.000 description 9
- 239000007858 starting material Substances 0.000 description 9
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 8
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 8
- 150000001341 alkaline earth metal compounds Chemical class 0.000 description 8
- 230000000875 corresponding effect Effects 0.000 description 8
- 239000000499 gel Substances 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 8
- 235000017281 sodium acetate Nutrition 0.000 description 8
- BDAGIHXWWSANSR-UHFFFAOYSA-M Formate Chemical compound [O-]C=O BDAGIHXWWSANSR-UHFFFAOYSA-M 0.000 description 7
- KQNKJJBFUFKYFX-UHFFFAOYSA-N acetic acid;trihydrate Chemical compound O.O.O.CC(O)=O KQNKJJBFUFKYFX-UHFFFAOYSA-N 0.000 description 7
- 150000001732 carboxylic acid derivatives Chemical class 0.000 description 7
- 239000000969 carrier Substances 0.000 description 7
- 230000006866 deterioration Effects 0.000 description 7
- 230000007062 hydrolysis Effects 0.000 description 7
- 238000006460 hydrolysis reaction Methods 0.000 description 7
- 229910000464 lead oxide Inorganic materials 0.000 description 7
- 229910052744 lithium Inorganic materials 0.000 description 7
- UEGPKNKPLBYCNK-UHFFFAOYSA-L magnesium acetate Chemical compound [Mg+2].CC([O-])=O.CC([O-])=O UEGPKNKPLBYCNK-UHFFFAOYSA-L 0.000 description 7
- 239000011654 magnesium acetate Substances 0.000 description 7
- 229940069446 magnesium acetate Drugs 0.000 description 7
- 235000011285 magnesium acetate Nutrition 0.000 description 7
- 239000011734 sodium Substances 0.000 description 7
- 239000007921 spray Substances 0.000 description 7
- BNGXYYYYKUGPPF-UHFFFAOYSA-M (3-methylphenyl)methyl-triphenylphosphanium;chloride Chemical compound [Cl-].CC1=CC=CC(C[P+](C=2C=CC=CC=2)(C=2C=CC=CC=2)C=2C=CC=CC=2)=C1 BNGXYYYYKUGPPF-UHFFFAOYSA-M 0.000 description 6
- WVDDGKGOMKODPV-UHFFFAOYSA-N Benzyl alcohol Chemical compound OCC1=CC=CC=C1 WVDDGKGOMKODPV-UHFFFAOYSA-N 0.000 description 6
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 6
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 6
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 6
- 150000001342 alkaline earth metals Chemical class 0.000 description 6
- 238000004458 analytical method Methods 0.000 description 6
- HUMNYLRZRPPJDN-UHFFFAOYSA-N benzaldehyde Chemical compound O=CC1=CC=CC=C1 HUMNYLRZRPPJDN-UHFFFAOYSA-N 0.000 description 6
- 239000001569 carbon dioxide Substances 0.000 description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 description 6
- 150000007942 carboxylates Chemical class 0.000 description 6
- 230000015556 catabolic process Effects 0.000 description 6
- 230000008859 change Effects 0.000 description 6
- 238000010924 continuous production Methods 0.000 description 6
- 230000007797 corrosion Effects 0.000 description 6
- 238000005260 corrosion Methods 0.000 description 6
- 238000006731 degradation reaction Methods 0.000 description 6
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 6
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 6
- 239000006185 dispersion Substances 0.000 description 6
- 229910052914 metal silicate Inorganic materials 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- YEXPOXQUZXUXJW-UHFFFAOYSA-N oxolead Chemical compound [Pb]=O YEXPOXQUZXUXJW-UHFFFAOYSA-N 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 239000002002 slurry Substances 0.000 description 6
- 239000001632 sodium acetate Substances 0.000 description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 5
- 239000005977 Ethylene Substances 0.000 description 5
- 229910002651 NO3 Inorganic materials 0.000 description 5
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 5
- 229910003849 O-Si Inorganic materials 0.000 description 5
- 229910003872 O—Si Inorganic materials 0.000 description 5
- 229910021128 PdPb Inorganic materials 0.000 description 5
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- 238000012545 processing Methods 0.000 description 5
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 5
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
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- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
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- VZSRBBMJRBPUNF-UHFFFAOYSA-N 2-(2,3-dihydro-1H-inden-2-ylamino)-N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]pyrimidine-5-carboxamide Chemical compound C1C(CC2=CC=CC=C12)NC1=NC=C(C=N1)C(=O)NCCC(N1CC2=C(CC1)NN=N2)=O VZSRBBMJRBPUNF-UHFFFAOYSA-N 0.000 description 3
- WZFUQSJFWNHZHM-UHFFFAOYSA-N 2-[4-[2-(2,3-dihydro-1H-inden-2-ylamino)pyrimidin-5-yl]piperazin-1-yl]-1-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)ethanone Chemical compound C1C(CC2=CC=CC=C12)NC1=NC=C(C=N1)N1CCN(CC1)CC(=O)N1CC2=C(CC1)NN=N2 WZFUQSJFWNHZHM-UHFFFAOYSA-N 0.000 description 3
- XNDZQQSKSQTQQD-UHFFFAOYSA-N 3-methylcyclohex-2-en-1-ol Chemical compound CC1=CC(O)CCC1 XNDZQQSKSQTQQD-UHFFFAOYSA-N 0.000 description 3
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 3
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- 241000287463 Phalacrocorax Species 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 3
- DHKHKXVYLBGOIT-UHFFFAOYSA-N acetaldehyde Diethyl Acetal Natural products CCOC(C)OCC DHKHKXVYLBGOIT-UHFFFAOYSA-N 0.000 description 3
- 125000002777 acetyl group Chemical class [H]C([H])([H])C(*)=O 0.000 description 3
- 239000003513 alkali Substances 0.000 description 3
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 3
- 229910000323 aluminium silicate Inorganic materials 0.000 description 3
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 3
- 229910052785 arsenic Inorganic materials 0.000 description 3
- JFDZBHWFFUWGJE-UHFFFAOYSA-N benzonitrile Chemical compound N#CC1=CC=CC=C1 JFDZBHWFFUWGJE-UHFFFAOYSA-N 0.000 description 3
- 229910052797 bismuth Inorganic materials 0.000 description 3
- JCXGWMGPZLAOME-UHFFFAOYSA-N bismuth atom Chemical compound [Bi] JCXGWMGPZLAOME-UHFFFAOYSA-N 0.000 description 3
- 238000007664 blowing Methods 0.000 description 3
- 229910052796 boron Inorganic materials 0.000 description 3
- 238000001354 calcination Methods 0.000 description 3
- 229910052804 chromium Inorganic materials 0.000 description 3
- 239000011651 chromium Substances 0.000 description 3
- 239000000470 constituent Substances 0.000 description 3
- 239000010949 copper Substances 0.000 description 3
- 238000007865 diluting Methods 0.000 description 3
- 239000012527 feed solution Substances 0.000 description 3
- 238000000227 grinding Methods 0.000 description 3
- 150000003840 hydrochlorides Chemical class 0.000 description 3
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- HQQUTGFAWJNQIP-UHFFFAOYSA-K aluminum;diacetate;hydroxide Chemical compound CC(=O)O[Al](O)OC(C)=O HQQUTGFAWJNQIP-UHFFFAOYSA-K 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 229910052787 antimony Inorganic materials 0.000 description 1
- WATWJIUSRGPENY-UHFFFAOYSA-N antimony atom Chemical compound [Sb] WATWJIUSRGPENY-UHFFFAOYSA-N 0.000 description 1
- 229960001716 benzalkonium Drugs 0.000 description 1
- CYDRXTMLKJDRQH-UHFFFAOYSA-N benzododecinium Chemical compound CCCCCCCCCCCC[N+](C)(C)CC1=CC=CC=C1 CYDRXTMLKJDRQH-UHFFFAOYSA-N 0.000 description 1
- ZTQSAGDEMFDKMZ-UHFFFAOYSA-N butyric aldehyde Natural products CCCC=O ZTQSAGDEMFDKMZ-UHFFFAOYSA-N 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 1
- 150000001735 carboxylic acids Chemical class 0.000 description 1
- 238000006757 chemical reactions by type Methods 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000012650 click reaction Methods 0.000 description 1
- 230000002596 correlated effect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 150000004683 dihydrates Chemical class 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 238000004993 emission spectroscopy Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000012013 faujasite Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000010436 fluorite Substances 0.000 description 1
- WBJINCZRORDGAQ-UHFFFAOYSA-N formic acid ethyl ester Natural products CCOC=O WBJINCZRORDGAQ-UHFFFAOYSA-N 0.000 description 1
- 229910052733 gallium Inorganic materials 0.000 description 1
- 238000010574 gas phase reaction Methods 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 150000004820 halides Chemical class 0.000 description 1
- 239000011964 heteropoly acid Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000000017 hydrogel Substances 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- RXPAJWPEYBDXOG-UHFFFAOYSA-N hydron;methyl 4-methoxypyridine-2-carboxylate;chloride Chemical compound Cl.COC(=O)C1=CC(OC)=CC=N1 RXPAJWPEYBDXOG-UHFFFAOYSA-N 0.000 description 1
- 238000011221 initial treatment Methods 0.000 description 1
- 150000002484 inorganic compounds Chemical class 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 230000002262 irrigation Effects 0.000 description 1
- 238000003973 irrigation Methods 0.000 description 1
- 229910052746 lanthanum Inorganic materials 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 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
- 239000000463 material Substances 0.000 description 1
- 239000002207 metabolite Substances 0.000 description 1
- 239000002923 metal particle Substances 0.000 description 1
- 229940095102 methyl benzoate Drugs 0.000 description 1
- LCGLNKUTAGEVQW-UHFFFAOYSA-N methyl monoether Natural products COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 1
- 238000003801 milling Methods 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 150000007522 mineralic acids Chemical class 0.000 description 1
- 239000012046 mixed solvent Substances 0.000 description 1
- 229910052680 mordenite Inorganic materials 0.000 description 1
- 239000004570 mortar (masonry) Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 125000002524 organometallic group Chemical group 0.000 description 1
- 235000020636 oyster Nutrition 0.000 description 1
- QNGNSVIICDLXHT-UHFFFAOYSA-N para-ethylbenzaldehyde Natural products CCC1=CC=C(C=O)C=C1 QNGNSVIICDLXHT-UHFFFAOYSA-N 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000002186 photoelectron spectrum Methods 0.000 description 1
- 238000001637 plasma atomic emission spectroscopy Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 235000011056 potassium acetate Nutrition 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 150000003242 quaternary ammonium salts Chemical class 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 229910052702 rhenium Inorganic materials 0.000 description 1
- WUAPFZMCVAUBPE-UHFFFAOYSA-N rhenium atom Chemical compound [Re] WUAPFZMCVAUBPE-UHFFFAOYSA-N 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- ZNCPFRVNHGOPAG-UHFFFAOYSA-L sodium oxalate Chemical compound [Na+].[Na+].[O-]C(=O)C([O-])=O ZNCPFRVNHGOPAG-UHFFFAOYSA-L 0.000 description 1
- 229940039790 sodium oxalate Drugs 0.000 description 1
- DGPIGKCOQYBCJH-UHFFFAOYSA-M sodium;acetic acid;hydroxide Chemical compound O.[Na+].CC([O-])=O DGPIGKCOQYBCJH-UHFFFAOYSA-M 0.000 description 1
- GRONZTPUWOOUFQ-UHFFFAOYSA-M sodium;methanol;hydroxide Chemical compound [OH-].[Na+].OC GRONZTPUWOOUFQ-UHFFFAOYSA-M 0.000 description 1
- 238000010671 solid-state reaction Methods 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 150000003459 sulfonic acid esters Chemical class 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
- 229910052714 tellurium Inorganic materials 0.000 description 1
- PORWMNRCUJJQNO-UHFFFAOYSA-N tellurium atom Chemical compound [Te] PORWMNRCUJJQNO-UHFFFAOYSA-N 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- OSBSFAARYOCBHB-UHFFFAOYSA-N tetrapropylammonium Chemical compound CCC[N+](CCC)(CCC)CCC OSBSFAARYOCBHB-UHFFFAOYSA-N 0.000 description 1
- 230000036962 time dependent Effects 0.000 description 1
- VZCYOOQTPOCHFL-UHFFFAOYSA-N trans-butenedioic acid Natural products OC(=O)C=CC(O)=O VZCYOOQTPOCHFL-UHFFFAOYSA-N 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 150000003672 ureas Chemical class 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- JLQFVGYYVXALAG-CFEVTAHFSA-N yasmin 28 Chemical compound OC1=CC=C2[C@H]3CC[C@](C)([C@](CC4)(O)C#C)[C@@H]4[C@@H]3CCC2=C1.C([C@]12[C@H]3C[C@H]3[C@H]3[C@H]4[C@@H]([C@]5(CCC(=O)C=C5[C@@H]5C[C@@H]54)C)CC[C@@]31C)CC(=O)O2 JLQFVGYYVXALAG-CFEVTAHFSA-N 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/39—Preparation of carboxylic acid esters by oxidation of groups which are precursors for the acid moiety of the ester
-
- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
- B01J23/622—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead
- B01J23/628—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead with lead
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
- B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
- B01J29/44—Noble metals
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
- B01J29/48—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing arsenic, antimony, bismuth, vanadium, niobium tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
-
- 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
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/08—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C69/00—Esters of carboxylic acids; Esters of carbonic or haloformic acids
- C07C69/52—Esters of acyclic unsaturated carboxylic acids having the esterified carboxyl group bound to an acyclic carbon atom
- C07C69/533—Monocarboxylic acid esters having only one carbon-to-carbon double bond
- C07C69/54—Acrylic acid esters; Methacrylic acid esters
-
- 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
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/14—Silica and magnesia
-
- 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
- B01J37/0027—Powdering
- B01J37/0045—Drying a slurry, e.g. spray drying
Definitions
- the present invention relates to a catalyst used for producing a carboxylic acid ester from an aldehyde, an alcohol and molecular oxygen, a method for producing the catalyst, and a method for producing a carboxylic acid ester using the catalyst. More specifically, the present invention provides a method in which palladium and lead are supported on a carrier in a specific ratio, and has a maximum intensity peak in a specific range of diffraction angles (20) in a powder X-ray diffraction pattern.
- a novel catalyst which provides good carboxylic acid ester selectivity even under high temperature and high aldehyde reaction conditions, and has excellent mechanical strength and corrosion resistance, and production of the catalyst.
- the present invention also relates to a method and a method for continuously and efficiently producing a carboxylic acid ester from an aldehyde, an alcohol and a molecular oxygen with a high yield for a long time using the catalyst.
- methyl methacrylate or methyl acrylate for example, in the case of methyl methacrylate, methacryloline is oxidized with oxygen.
- a method for producing methyl methacrylate by reacting methacrylic acid with methanol to produce methyl methacrylate has already been industrialized.
- the yield of the process of oxidizing methacrylic acid lane to methacrylic acid has been improved to the low 80% range by years of catalyst improvement.
- the heteropolyacid catalyst used has some drawbacks in terms of thermal stability, and decomposition proceeds gradually under reaction temperature conditions.
- catalyst improvement to improve heat resistance has been reported, it is said that the catalyst life of industrial catalysts is still insufficient.
- methacrolein or acrolein are reacted with methanol and molecular oxygen at a stroke.
- New methods of producing methyl methacrylate or methyl acrylate have recently attracted attention. I'm afraid. This method is performed by reacting (meth) acryloline with molecular oxygen in methanol, and the presence of a catalyst containing palladium is essential.
- Japanese Patent Publication No. 62-0 / 07 902 proposes a catalyst containing an intermetallic compound in which palladium and lead are combined in a simple integer ratio.
- the catalyst was shown to be a catalyst system in which the decomposition reaction of the catalyst was almost completely inhibited, and the catalytic activity was not lost for a long time.
- the new production method using these new catalyst systems also has the advantage that the process is shorter than the method using (meta) acrylic acid, which has the effect of improving yield and catalyst life, as mentioned above. Industrialization is awaited as a new method for producing industrially useful raw materials for polymers.
- MMA methyl methacrylate
- the reaction conditions are economically advantageous on the premise of industrial implementation.
- this reaction is carried out at a high temperature of 60 ° C or higher and a high concentration of methacrolein in the reaction system of 20% or more, the catalyst system decreases the selectivity of MMA and formic acid due to oxidation of alcohol itself. A sudden increase in methyl by-products occurs.
- 5-0 69813 discloses the reaction system.
- An example of a reaction at a tacrolein concentration of 20% and a reaction temperature of 80 ° C is shown.
- high MMA selectivity based on high metalloin exceeding 90% has not been obtained.
- methyl formate doubles to 0.0923 mol / mol MMA.
- the concentration of the metal mouth lane to 30%, if the conditions are severe, the MMA selectivity based on the metal mouth lane, which is liable to cause the decomposition reaction of the metal mouth lane, is further increased. Worsen You.
- palladium which is a kind of noble metal
- a catalyst component it is often used by dispersing it on a carrier, and in that case, the choice of the carrier is extremely important.
- a method for producing a carboxylic acid ester by reacting an aldehyde, an alcohol, and oxygen with a catalyst containing palladium is disclosed in Japanese Patent Application Laid-open Nos. 57-35856, 57-73587, 5 7- 3 5 8 5 8, 5 7 — 3 5 8 5 9, 5 7-3 5 8 6 9, activated carbon.
- Silica, alumina, calcium carbonate, etc. are exemplified as catalyst carriers.
- the silica gel production method should be studied, and that the silica gel should be modified by high-temperature firing.
- quartz which is one of the silica-based substances, is hard and has high mechanical strength and hydrolysis resistance.
- the quartz support has very good mechanical strength and hydrolysis resistance, but has a small specific surface area (lm 2 Zg or less) and cannot support the metal catalyst in the form of fine particles in a highly dispersed state.
- the catalyst obtained When used as a carrier, the catalyst obtained has a very low reaction activity per unit weight, and cannot be used as a catalyst carrier.
- the material used for the carrier while presuming its use as a catalyst carrier, maintains a high specific surface area to some extent, and at the same time, has mechanical strength and corrosion resistance to liquid substances inherent to this reaction. There has been no need to satisfy a catalyst support that meets these requirements.
- High temperature, high altitude to improve economy Produces the desired carboxylic acid ester (eg, MMA) with a high selectivity of over 90% under the concentration of dehydration, and produces few by-products (eg, methyl formate). It was desired to develop a catalyst with high corrosion resistance as long as its mechanical strength was high.
- the present inventors have found that even under reaction conditions in which the reaction temperature is high and the aldehyde concentration of the reaction system is high, the selectivity of the target carboxylate is high, and furthermore, for example, methyl formate
- intensive research was conducted on a catalyst system containing palladium and lead. That is, among the intermetallic compound species in which palladium and lead are combined at a simple integer ratio, the atomic ratio of which was previously proposed by the present inventors in Japanese Patent Publication No. 62-0 / 790, the atomic ratio was 3/1. Pd 3 Pb!
- a main object of the present invention is to produce a carboxylate by reacting aldehyde with alcohol and molecular oxygen in the presence of a catalyst containing palladium and lead. Even under the reaction conditions where the aldehyde concentration and reaction temperature of the reaction system are high, which are advantageous for improving the reactivity, the selectivity of the carboxylic acid ester is high, and the amount of by-products derived from alcohol such as methyl formate is small.
- An object of the present invention is to provide a catalyst that enables a method for producing a carboxylic acid ester.
- Another object of the present invention is to provide a method for producing the above catalyst.
- Still another object of the present invention is to provide a method for producing a carbonate ester using the above-mentioned catalyst, particularly a continuous production method with less catalyst deterioration.
- Figure 1 shows the X attributed to the Pd (3d) electron of metallic palladium.
- Fig. 2 is a spectrum diagram showing an example of X-ray photoelectron spectrum;
- FIG. 9 is a spectrum diagram showing an example of a processing result.
- a catalyst for producing a carboxylic acid ester from an aldehyde, an alcohol and molecular oxygen comprising palladium and lead in an atomic ratio (PdZPb) 3.
- PdZPb atomic ratio
- the maximum value attributed to the diffraction of the (111) plane of the palladium-lead intermetallic compound cannot be obtained.
- a catalyst for the production of carboxylic acid esters from aldehydes, alcohols and molecular oxygen comprising palladium and lead in (PdZPb) atomic ratio (S) power of 7 ⁇ S ⁇ 3 / 1.3.
- PdZPb palladium and lead in
- S atomic ratio
- the Pd of metallic lead is the sum of the intensities of the two peaks belonging to the Pd 3d (3/2) electron and the Pd 3 d (5/2) electron of metallic palladium, respectively.
- M represents at least one kind of cation having n valence
- R represents a group IB, ⁇ ⁇ , ⁇ , IV ⁇ , WA, IVB
- n is 1 or 2
- w is an integer of 1 to 4
- x 0.3 ⁇ 0.1, 0.5 ⁇ y ⁇ 500.
- a reducible palladium compound, or a catalyst precursor comprising a reducible palladium compound and a reducible lead compound supported on a carrier is mixed with a C i _C 5 fatty acid in the presence of lead ion and 2.
- the reducible palladium compound is at least one salt selected from an organic acid salt and an inorganic acid salt of palladium
- the reducible lead compound is selected from an organic acid salt and an inorganic acid salt of lead. 7.
- the salt is at least one kind of salt.
- a series of oxidation treatments consisting of oxidation treatment with a gaseous oxidizing agent and subsequent reduction treatment with a gaseous reducing agent on the catalyst intermediate supported on the carrier within the range of 7 ⁇ S ⁇ 3 / 1.3. 2.
- gaseous reducing agent according to the preceding item, characterized in that the gaseous reducing agent includes at least one selected from methanol gas, molecular hydrogen and C 2 -C 4 olefin gas. Or the method according to 16.
- gaseous reducing agent is methanol gas, molecular hydrogen or
- a catalyst intermediate in which (S) is supported on a carrier in the range of 3 Z 0 ⁇ S ⁇ 3/10 is used in a reactor and the oxygen partial pressure at the reactor outlet side in the presence of lead ions.
- the reactor was loaded with a catalyst intermediate consisting of palladium or palladium and lead supported on a carrier with a Pd / Pb atomic ratio (S) in the range of 3/0 ⁇ S ⁇ 3/10. used, the presence of lead ions, under the conditions of the reactor oxygen partial pressure 0-0 the outlet side. 4 kg Z cm 2, and characterized that you are reacted with a mixture of alcohol, or alcohol and aldehyde 3.
- S Pd / Pb atomic ratio
- the catalyst described in 1 above was used in a reactor under the condition of oxygen partial pressure of 0 to 0.8 kg / cm 2 in the presence of lead ion and oxygen Or the reaction with a mixture of alcohol and an alcohol aldehyde.
- catalyst precursor refers to a reducible palladium compound or a composition comprising a reducible palladium compound and a reducible lead compound supported on a carrier. In one embodiment of the method for producing a catalyst of the present invention, it is used as a starting material.
- catalyst intermediate refers to a catalyst composition comprising palladium or a mixture of palladium and lead supported on a carrier at an atomic ratio (S) of 3/0 to 3/10. Means a catalyst composition that does not satisfy all or a part of the essential requirements of the catalyst of the present invention.
- the catalyst composition is activated to produce the catalyst of the present invention.
- Used for Examples of the catalyst intermediate include a conventional catalyst prepared by a known method and a catalyst of the present invention which is deteriorated as a result of using the catalyst of the present invention in a reaction for producing a carboxylic acid ester. Spent catalysts that did not satisfy part or all can be mentioned.
- activation means that the above-mentioned “catalyst intermediate” is reformed or modified in various ways to obtain a catalyst which satisfies all the essential requirements of the catalyst of the present invention.
- high-grade means that the contained palladium-lead intermetallic compound (Pd 3 Pbi) has very few lattice defects and forms a virtually ideal crystal lattice of the lead intermetallic compound.
- low quality means that there are many lattice defects as described above. I do.
- high purity refers to a palladium-lead / intermetallic compound contained in the catalyst (lead oxides other than the lead constituents of PdsPbJ and lead impurity components such as metallic lead alone are extremely small, and the catalyst is supported on the carrier. It means that the metal component consists essentially of only the constituent metals of the intermetallic compound, and the term “low purity” means that the above-mentioned lead impurity component is large.
- catalytic performance such as selectivity of a target carboxylic acid ester such as MMA is significantly reduced as compared with the catalyst of the present invention.
- the present inventors have further studied and made an attempt to prepare a catalyst by reducing the amount of lead to 3/1 as much as possible in a Pd / Pb atomic ratio in order to reduce lead impurities.
- the conventional manufacturing method simply be prepared earthenware pots by P d / P b atomic ratio of 3/1, more lattice defects, low quality P d 3 P b, Only a supported catalyst was obtained, and it was found that the selectivity of the target carboxylic acid ester was further reduced as compared with the catalyst described in Japanese Patent Publication No. 62-0 / 79092. .
- an ideal catalyst containing no lead as a catalytically active species and containing few lead impurities has not been realized.
- the present inventors have conducted research on a method for forming high-quality Pd 3 Pb, an intermetallic compound on a carrier with a stoichiometric composition without using excessive lead. As a result, the palladium compound was reduced. I learned that the underlying process was important. That is, as will be described in detail later, a reducible palladium compound or a catalyst precursor carrying a reducible palladium compound and a reducible lead compound is converted to a lead ion, a lower fatty acid, Under conditions where ions and Z or alkaline earth metal ions coexist, reduction is performed with a reducing agent such as formalin, formic acid, hydrazine, methanol, or molecular hydrogen.
- a reducing agent such as formalin, formic acid, hydrazine, methanol, or molecular hydrogen.
- a catalyst precursor supporting a reducible palladium compound or a reducible palladium compound and a reducible lead compound contains a lead ion. and, and C, - C 5 fatty acids, and this reduced with water and or alcohol solution containing one compound also reduced selected Li by alkali metal salts and Al force Li earth metal salts Yotsutsu High quality Pd3Pb with few defects in the crystal lattice!
- a catalyst containing an intermetallic compound with high purity can be obtained.
- the obtained catalyst shows a high selectivity to the target carboxylic acid ester even under severe reaction conditions such as the above-mentioned high aldehyde concentration and high reaction temperature.
- the catalyst precursor refers to a composition in which a metal salt constituting a catalytic active site is supported on a carrier thereof, and a composition which becomes a metal catalyst when reduced.
- the catalyst of the present invention palladium and lead, palladium / / Pb atomic ratio carrier 3 / 0.7 to 3 1.3 with been carried Is necessary.
- the PdZPb atomic ratio is preferably from 30.9 to 3 / 1.1. If the amount of lead exceeds 1.3 at the above atomic ratio, the production of carboxylate by reaction of aldehyde with alcohol and molecular oxygen in the presence of this catalyst will cause an adverse reaction of methyl formate and the like. If the production of the product is remarkable ⁇ 0.7, the selectivity of the target carboxylic acid ester such as MMA due to decomposition of the aldehyde is greatly reduced. More preferably, the above atomic ratio is as close to 3Z1 as possible.
- the powder X-ray diffraction pattern shows the maximum intensity peak attributed to the diffraction of the (111) plane of the palladium-lead intermetallic compound at the X-ray diffraction angle (20) 38. It is necessary to indicate in the range of 55 to 38.70 degrees. Below 38.55 degrees, by-products such as methyl formate are remarkably formed. When the temperature exceeds 38.70 degrees, the decomposition of aldehyde as a starting material becomes remarkable, and the selectivity of the target carboxylic acid ester such as MMA decreases.
- the catalyst of the present invention that satisfies these two requirements exhibits a high selectivity of more than 90% with respect to a carboxylic acid ester such as MMA. This effect is particularly important when producing carboxylic esters under industrially advantageous reaction conditions such as high temperature and high aldehyde concentration.
- the catalyst whose surface structure and surface composition are precisely controlled as shown in Fig. 7 can generate by-products such as methyl formate even under severe reaction conditions such as high aldehyde concentration and high reaction temperature. It was found that not only the amount was low, but also the selectivity of the target carboxylic acid ester was high and the conversion of aldehyde was high.
- X-ray photoelectron analysis is performed on the surface of the catalyst (approximately 1 OA for Pd and Pb), and the ratio of metal palladium to metal lead present on the catalyst surface is the intensity ratio (area ratio) of each peak. Is calculated based on When the peak intensity ratio is within the above range, the above-described extremely excellent catalytic performance is exhibited. That is, by controlling the surface structure and surface composition of the catalyst containing Pd 3 Pb, as a catalyst species, the selectivity of the target carboxylic acid ester is improved both in the aldehyde standard and the alcohol standard. The result was quite unexpected.
- the catalytic species is ⁇ d3Pb, and in the X-ray photoelectron spectrum, the Pd3d (3/2) and Pd3d (5/2) electrons of metallic palladium are Of the sum of the intensities of the two peaks Peak intensity attributable to Pb 4 f (7/2) electrons of metallic lead XI to the ratio of 75 [Pd 3 d (3/2) + Pd 3 d (5/2)] / [Pb 4 High aldehyde concentration and high temperature can be obtained by precisely controlling the surface structure and composition of the catalyst so that f (7/2) XI.75] is 10.2 or more: LZO.7. Even under such harsh reaction conditions, by-products such as methyl formate were less generated, and it was possible to enhance the selectivity of the target carboxylic acid ester.
- the carrier in the catalyst of the present invention is not particularly limited, but an aluminum-containing silica composition system, a silica-alumina-magnesium composition system or a crystalline aluminosilicate carrier is preferably used as the mechanical support. It is particularly preferably used from the viewpoint of target strength.
- Magnesium (divalent) compensates and neutralizes the difference in charge caused by the difference in valence between A1 and A1 (trivalent), and neutralizes it to promote charge stabilization. Furthermore, it is inferred that (3) the stability of the structure can be further improved because a three-component system can be balanced in charge. Therefore, the silica-alumina-magnesium carrier used in the catalyst of the present invention is almost neutral, whereas the silica-alumina carrier is acidic, which means that It is presumed that this leads to the suppression of the production of acetal which is remarkable.
- Still another preferred carrier used in the catalyst of the present invention is a crystalline metal silicate having a composition represented by the following formula (1) expressed in a molar ratio in an anhydrous state. is there.
- M represents at least one kind of cation having n valence
- R represents IB, ⁇ ⁇ , MA, ⁇ ⁇ , or IV of the short-periodic periodic table
- It represents at least one kind of w-valent metal selected from metals of group A, IVB, VA, VB, IB, WB, and VI, where n is 1 or 2 and w is 1 to 2.
- An integer of 4, x 0.3 ⁇ 0.1,
- the crystalline metal silicate having a regular bonded chain structure for example, if it is assumed that A 1 is used as the R component, the crystalline structure has a regular bonded chain. It is considered that the resistance to hydrolytic degradation is significantly improved due to the formation of Si—O—Al—O—Si bonds and reduction of uncrosslinked sites.
- the formation of the S i —O—A 1 —O—S i crosslinked structure greatly improves the mechanical strength as compared to silica gel alone. That is, it is presumed that the mechanical strength and water resistance are improved by the formation amount of the Si-O-Al-O-Si structure and the formation of the crystal structure by regular bonding.
- the cation M is based on the difference in valence between Si (tetravalent) and A 1 (trivalent) due to the formation of the Si — O— Al — O— Si bridge structure. Neutralizes compensation and promotes charge stabilization. Furthermore, it is assumed that the stability of the crystal structure is improved because the charge can be balanced by the ternary system.
- silica-alumina is a substance exhibiting a strong acid property.
- silica-alumina is a carboxylic acid of the present invention because of its strong acid property.
- Acetal is produced from aldehyde and alcohol, which are the raw materials for the reaction of the acid ester production method. Since it is easily presumed that the catalyst is easily produced, it is considered unsuitable as a catalyst carrier in the ester production method of the present invention, and the catalyst can be added to the ester production method of the present invention without being deeply studied. The research used as a supporter was greatly delayed.
- Three preferred supports effective in significantly improving the life of the catalysts of the present invention are aluminum-containing silica-based compositions, silica-alumina-magnesia compositions, and crystalline metallosilicates. The following is a description of the operation.
- the amount of the aluminum is preferably in the range of 1 to 30 mol% based on the total molar amount of silicon and aluminum.
- the ratio of A 1 / (A 1 + S i) is :! It is preferably about 30 mol%.
- the preferred properly in the range of 5-3 0 mole 0/0.
- the aluminum content is less than 1 mol%, the effect of improving mechanical strength and water resistance is improved. Fruit is small.
- it exceeds 30 mol% the acid resistance and the mechanical strength decrease significantly. This is presumed to be due to the fact that the amount of A 1 atoms incorporated into the S i —O chain exceeded the limit, and A 1 began to separate and precipitate.
- the carrier contains a composition containing 75 to 90 mole% of silicon, 5.5 to 15 mole 0 of aluminum, and 4 to 10 mole% of magnesium. Used. Outside this range, the effect of improving mechanical strength and water resistance is small. This is presumed to be due to the fact that magnesium, aluminum, and silica form specific stable bonding structures within this range.
- crystalline metal silicate those having an anhydrous state and a composition expressed by a molar ratio represented by the above formula (1) are preferred. This is because a metallo ligate having a crystal composition in the range of the above formula (1) is excellent from the viewpoints of carrier strength and catalyst preparation.
- Aluminium-containing silica-based alumina compositions which are typical examples, can be obtained by the following method. (1) Select from commercially available silica-alumina compositions that correspond to the composition of the present invention.
- the obtained aluminum-containing silica composition can be calcined and used under the conditions described below.
- silica sol As a silica source, silica sol, water glass, or silica gel can be used.
- the silica gel only needs to have an uncrossed S i site that reacts with A 1, and the length of the S i —O chain is not particularly limited.
- Aluminum compounds include sodium aluminate, aluminum chloride hexahydrate, aluminum perchlorate hexahydrate, aluminum sulfate, aluminum nitrate nonahydrate, and dihydrate.
- Water-soluble compounds such as aluminum acetate are preferred, but water-insoluble compounds such as aluminum hydroxide and aluminum oxide also react with uncrosslinked Si in silica sol and silica gel.
- Compound Any object can be used.
- the silica sol and the aluminum compound are mixed to obtain a mixed sol containing the silica sol and the aluminum compound, and the resulting mixture has a viscosity of 20 to 10%.
- the above mixed sol is pulverized using a spray dryer, and the mixed sol is dried to form a gel to obtain an aluminum-containing silica carrier having a desired particle size. Is also possible.
- the silica sol is allowed to react with the water-insoluble aluminum compound. It can also be ground.
- the silica sol and the water-insoluble aluminum compound are mixed and reacted, dried, and fired under the conditions described later.
- the fired silica-alumina compound may be ground to a predetermined particle size.
- silica gel is used as a starting material (5).
- the silica gel and the aluminum compound may be pulverized to a predetermined particle size in advance, or may be preliminarily coarsely pulverized.
- the pulverization may be performed by each substance alone, or both may be mixed and pulverized.
- the firing is performed under the following temperature, time, and atmosphere conditions. It is also possible to pulverize silica gel and aluminum compound to a desired particle size after the reaction without using pre-grinding, and use it.
- silica raw material silica sol, water glass, or silica gel can be used.
- the silica gel only needs to have an uncrosslinked Si site that reacts with A 1, and there is no particular limitation on the length of the Si—O chain.
- Aluminum compounds include sodium aluminate, aluminum chloride hexahydrate, aluminum perchlorate hexahydrate, aluminum sulfate, and aluminum nitrate nonahydrate.
- Water-soluble compounds such as aluminum diacetate
- water-insoluble compounds such as aluminum hydroxide and aluminum oxide are preferred as long as they are compounds that react with uncrosslinked Si in silica sol and silica gel. Is possible.
- magnesium oxide, magnesium hydroxide, magnesium acetate, magnesium nitrate, magnesium chloride, magnesium sulfate and the like can be used as a raw material of magnesium.
- the method of (1) using silica-alumina gel as a raw material is to add sulfuric acid to water glass in advance and add silica of pH 8 to 10.5. Li tell a human Dorogeru, this A 1 2 (SO 4) 3 solution was added (
- magnesia performs added pressure to 5 0 ⁇ 9 0 e C, 1 ⁇ 5 hour hydrothermal reaction, it is possible to obtain a carrier was fired under the conditions described below after drying.
- a mixture containing silica sol, aluminum compound and magnesium compound by mixing the silica sol with an aluminum compound and a magnesium compound is used.
- C A hydrothermal reaction is performed for 1 to 48 hours, dried to obtain a gel, and calcined under the conditions described below.
- an aqueous alkaline solution is added to a mixture sol containing the above-mentioned silica sol, aluminum compound and magnesium compound to coprecipitate the silica force, the aluminum compound and the magnesium compound, and dried to obtain a gel.
- the carrier is obtained by firing under the following conditions.
- the above mixture sol is pulverized using a spray dryer as it is, or the mixture is dried and granulated into a gel to form a silica-alumina-magnesia carrier having a desired particle diameter. It is also possible.
- the silica sol is reacted with a water-insoluble anoreminium compound and a water-insoluble magnesium compound.
- the aluminum compound and the magnesium compound are reacted.
- the compound may be ground beforehand to a predetermined particle size or preliminarily coarsely ground.
- silica-alumina-magnesia may be milled to a predetermined particle size.
- the method (4) using silica gel as a starting material involves reacting an aqueous solution of a water-soluble aluminum compound and a water-soluble magnesium compound with the silica gel. It may be crushed to a diameter or preliminary crushed. The silica gel is mixed and reacted with an aqueous solution of a water-soluble aluminum compound and a water-soluble magnesium compound at 20 to 100 ° C. for 1 to 48 hours, dried, and fired under the conditions described later. Without preliminary crushing of silica dim, silica mosquitoes after firing - alumina one magnesia may be ground until a predetermined grain size c
- the method of (5) using silica gel as a starting material is a method in which silica gel is prepared by a solid-phase reaction of an aluminum compound and a magnesium compound. Al and Mg are reacted with uncrosslinked Si in the solid state.
- the silica gel, aluminum compound and magnesium compound may be pulverized to a predetermined particle size in advance, or may be preliminarily coarsely pulverized. Good.
- the pulverization may be performed for each substance alone, or may be performed by mixing and pulverizing the three substances. It is also possible to pulverize silica gel, aluminum compounds and magnesium compounds to a desired particle size after the reaction without using pre-grinding.
- M is a monovalent or divalent cation in the crystalline metallosilicate, and , A proton, or a metal cation belonging to the group ⁇ , ⁇ A, HB, ⁇ , ⁇ , IVA, IVB, VB, VIB, VHB, or ⁇ on the periodic table.
- R is at least one member selected from the group consisting of IB, HB, ⁇ , ⁇ ⁇ , IVA, IVB, VA, VB, VIB, WB, and VIII of the short-periodic table.
- these metals include aluminum, boron, gallium, titanium, chromium, iron, and the like.
- a crystalline aluminosilicate having at least one metal containing aluminum is used, and more preferably, a crystalline aluminosilicate is used.
- the silica R 2 / w O molar ratio of the above crystalline metallosilicate is represented by y in equation (1), and this value is 0.5 or more and 500 or less. It is preferably from 0.5 to 200, more preferably from 0.5 to 100. Outside this range, the effect of improving mechanical strength and water resistance is small. This is presumed to be due to the formation of a stable crystalline meta- mouth silicate structure only within this range.
- X in the formula is the above silica and R 2 / w
- the amount of thione that neutralizes the negative charge generated by the bonding of O The amount of thione expressed as the ratio of ⁇ 2 / ⁇ to R2 / wO, which is independent of the value of y and y Thus, the range is 0.3 ⁇ 0.1.
- crystalline metallosilicates are diverse and structurally.
- structurally nalcime group, faujasite group, shabazite group, soda fluorite (natr 01) ite) group, phi11 ipsite group, mordenite group, ZSM-5, ZSM-5 similar zeolite ZSM-11 zeolite.
- ZSM-5 similar zeolites include ZSM-8 (see German Patent Specification No. 2049755) and ZETA-1 (see German Patent Specification No. 248,697) and ZETA— 3 (see British Patent 1,553,209), UN-14 (see German Patent 3,266,503), UN-5 (German Patent 3,169,066) TZ-011 (see US Pat. No.
- the synthesis of the crystalline metallosilicate used in the present invention is generally performed.
- the usual 20 to 100. C performed by hydrothermal synthesis for 1-48 hours.
- the silica source used at this time is not particularly limited, and water glass, silica sol, silica gel, or the like can be used.
- the metal source various inorganic compounds and organic metal compounds such as sulfates and nitrates of various metals, halides such as chloride and bromide, oxides and the like can be used.
- an organic template may be allowed to coexist as necessary.
- preferred are urea compounds such as dimethyl urea, quaternary ammonium salts such as tetrapropylammonium, diamins such as hexamethylene diamine, and alcohols.
- urea compounds such as dimethyl urea
- quaternary ammonium salts such as tetrapropylammonium
- diamins such as hexamethylene diamine
- alcohols urea compounds
- baking in air at a temperature of 400 to 800 ° C for 1 to 48 hours, or a liquid phase oxidation method using an oxidizing agent such as hydrogen peroxide is used as a method for removing organic substances.
- the above-mentioned various compositions which are preferably used as a carrier in the catalyst of the present invention are used after being calcined at a suitable temperature so as to have the above specific surface area.
- the firing temperature is generally selected from the range of 200 to 800. If it is fired at 800 ° C. or higher, the specific surface area is significantly unfavorably reduced.
- the firing atmosphere is not particularly limited, but firing is generally performed in air or nitrogen.
- the firing time can be determined according to the specific surface area after firing, but is generally 1 to 48 hours.
- reducible palladium compound or a reducible palladium compound and the catalyst precursor carrying reducible lead compounds, containing lead ions, further d-c 5 fatty acids, alkali metal Shokushio and Al force
- a method for producing a catalyst containing at least one compound selected from the group consisting of earth metal salts and reducing in a solution of water, alcohol or a mixture thereof will be described.
- a catalyst precursor in which a reducible palladium compound (hereinafter, often simply referred to as a “palladium compound”) is supported on a carrier can be prepared by a known method.
- the carrier is added to an aqueous solution containing a soluble palladium salt such as palladium chloride, heated at 20 to 100 ° C, and impregnated with the aqueous palladium solution for 1 to 24 hours, and the palladium salt is added to the carrier.
- a soluble palladium salt such as palladium chloride
- the carrier can be prepared by a known method such as loading.
- the catalyst precursor (hereinafter often referred to simply as a “lead compound”) is also added to the carrier with an aqueous solution containing a soluble palladium salt such as palladium chloride and a soluble lead compound such as lead acetate. It is obtained by impregnating for 1 to 24 hours at a temperature.
- the lead compound may be supported before the palladium compound is supported, and the palladium compound and the lead compound may be used as described above. May be simultaneously carried. Alternatively, the lead compound may be supported after the palladium compound is supported.
- the catalytic metal species contained in the catalyst precursor palladium or palladium and lead, and as a different element, for example, mercury, thallium, bismuth, tenorel, nickel, chromium, cobalt , Indium, tantalum, copper, zinc, zirconium, hafnium, tungsten, manganese, silver, rhenium, antimony, tin, rhodium, ruthenium, iridium, platinum, gold, titanium, aluminum, boron, It may contain silicon or the like.
- the content of these different elements is usually not more than 5% by weight, preferably not more than 1% by weight, based on the amount of all the catalytic species after reduction.
- alkali metal and alkaline earth metal are usually 0.01 to 30% by weight, preferably 0.01 to 5% by weight, based on the total amount of the catalyst species after reduction. /. Etc. c
- These different element or Al force Li metal and Al force Li earth metal selected from the range of may be substituted with some small amount, invading Li or crystal lattice metal, between the crystal lattice.
- these heteroelement compounds, alkali metal compounds, and / or earth metal compounds may be added to a solution containing a palladium compound or a lead compound at the time of preparing the catalyst, and may be adsorbed or adhered to a carrier. And prepare a catalyst using a carrier that supports these in advance. You can. It can also be added to the reaction system when performing a reduction reaction for preparing a catalyst.
- the palladium compound or lead compound used for preparing the catalyst precursor includes, for example, an organic acid salt such as formate and acetate, an inorganic acid salt such as sulfate, hydrochloride, and nitrate, an amine complex, and a metal salt. It is appropriately selected from organometallic complexes such as zononitrile complex, oxides and hydroxides, and the palladium compound is palladium chloride, palladium acetate, etc., and the lead compound is lead nitrate. And lead acetate are preferred.
- the alkali metal compound, organic acid salts also alkaline earth metal compound, an inorganic acid salt, but selected from such as water oxides, d-C 5 fatty acid salt is used properly preferred.
- the carrier can be widely selected from silica, alumina, silica-alumina, zeolite, magnesia, magnesium hydroxide, titania, calcium carbonate, activated carbon, and the like. It is preferable to use a carrier.
- the amount of palladium supported on the support in the final catalyst of the present invention is not particularly limited, but is usually 0.1 to 20% by weight, preferably 1 to 10% by weight based on the weight of the support. Normal 0 with respect to the support weight not supported amount particularly limited lead. 1-2 0% by weight, preferred although properly 1 to 1 0 weight 0, palladium, palladium rather Ri by the supported amount of lead.
- the atomic ratio of Z lead is important. Therefore, the palladium salt of the catalyst precursor used in the production method for the catalyst of the present invention is lead.
- the salt loading ratio is selected from the range of 3 to 31.3 in terms of the atomic ratio of PdZPb. It is preferable to select from the range of 3Z0 to 3Z0.7.
- the catalyst of the present invention is obtained by converting these catalyst precursors into an amount of lead ion necessary to obtain the palladium / lead supported catalyst of the present invention having a palladium / lead atomic ratio of 30.7 to 3Zl.3.
- a solution of water, alcohol (eg, methanol), or a mixture of them with a reducing agent such as formalin, formic acid, hydrazine, methanol or molecular hydrogen. And finally has a palladium-to-lead atomic ratio of 30.7 to 3 ⁇ 1.3.
- the above-mentioned catalyst precursor is dispersed in a solvent consisting of water or an alcohol such as methanol or a mixture thereof, and the dispersion is added at 20 to 200 ° C., preferably 40 to 160 ° C., and palladium is dispersed.
- aqueous solution or an alcohol for example, methanum
- the amount of lead required to obtain the palladium lead supported catalyst of the present invention having a supported composition ratio of 0.7 to 3/3.
- Reduction with formalin, formic acid, hydrazine or molecular hydrogen in a solution or alcohol / water solution Reduction with formalin, formic acid, hydrazine or molecular hydrogen in a solution or alcohol / water solution.
- An inert solvent other than alcohols such as water and methanol can be selected as long as the solvent is stable under the above conditions. In practice, it is preferable to select water or methanol.
- the amount of formalin, formic acid, hydrazine, methanol, or molecular hydrogen used is generally 0.1 to 100 times the molar amount of the palladium compound carried on the catalyst precursor. Practically, 0.5 to 10 times mol is used. There is no particular problem if this amount is exceeded. If an alkali such as caustic soda is added together with the reducing agent, the reduction proceeds more easily. Usually, the amount of alkali is about 110 to equimolar to the reducing agent.
- lead ions coexist.
- a lead-containing substance to water or methanol in which a catalyst precursor is dispersed.
- a lead-containing substance there is no particular limitation as long as it dissolves as lead ions.
- organic acid salts such as formate and acetate, sulfates and salts
- Inorganic acid salts such as acid salts and nitrates, oxides, hydroxides, etc., are preferred, but lead nitrate and lead acetate with high solubility are preferred.
- only those eluted from the catalyst precursor into the solution may be used.
- the amount of the lead compound to be added differs depending on the target catalyst precursor, the amount of the lead compound required to obtain the catalyst of the present invention having a supported composition ratio of 30.7 to 31.3 in PdZPb atomic ratio is obtained.
- the required amount of the lead compound is selected from the range of 3Z0 to 3 / 1.3 in the atomic ratio of (Pd in the palladium compound supported on the catalyst precursor) / (Pb to be added).
- the catalyst is dispersed in an aqueous solution in which the corresponding lead compound is dissolved or in an alcohol solution such as methanol to perform reduction.
- the above-mentioned lead compound may be added before starting the reduction operation, or may be added continuously or intermittently during the reduction operation.
- the PdPb ratio of the catalyst precursor is already 3 to 0.7.
- the required amount of lead compound can be added and reduced as described above even when the Pd / Pb atomic ratio does not exceed 3/13.
- it can be reduced without adding a lead compound.
- the Pb ion eluted from the catalyst precursor supporting the Pd salt and Pb salt acts as the lead ion required for this method.
- the catalyst of the present invention comprises a catalyst precursor in the presence of lead ion and Lower (d-C 5) fatty acids, in the presence of alkali metal salts and the Hare Chi least one compound also of alkaline earth metal salts, obtained by the child reduction in the above - reducing agent.
- Lower (d-C 5) is a fatty acid, acetic acid, butyric acid, and Ma lay down acid.
- the amount of the lower fatty acid to be added is about 0.1 to 30 times mol based on the supported palladium. Preferably, it is selected from the range of 1 to 15 moles. In practice, it is preferable to select acetic acid which is easily available.
- These lower fatty acids may be added simultaneously with the reducing agent, but it is more effective to add them before adding the reducing agent. The addition of these lower fatty acids is particularly effective when applied to a catalyst precursor in which both a palladium compound and a lead compound are supported.
- the alkali metal salt or alkaline earth metal salt of a lower fatty acid is added in an amount of about 0.1 to 30 moles based on the supported palladium compound (as palladium) of the catalyst precursor.
- I prefer 1 Choose from a range of ⁇ 15 times mol.
- Alkali metal salts of lower fatty acids As alkaline earth metal salts, sodium acetate and magnesium acetate are preferred.
- the reduction treatment can be carried out at a temperature of from room temperature to 200 ° C. (the pressure required to maintain the liquid phase is applied. Preferably, the pressure is from 40 to 160 ° C., from normal pressure). It is difficult to determine the reduction treatment time because it depends on the type of catalyst and treatment conditions, but it is a few minutes to 100 hours Set the conditions so that the treatment is completed within a few hours The completion of the treatment can be easily determined by measuring the X-ray diffraction angle of the (111) plane of the palladium Z-lead intermetallic compound of the obtained catalyst.
- the reactor used for the reduction is not particularly limited, and can be a usual stirred tank reactor.
- palladium and lead can be supported on the carrier at an atomic ratio (PdZPb) of 3 / 0.7 to 3 / 1.3, and In the X-ray diffraction pattern, the maximum intensity peak attributed to the diffraction of the (111) plane of the palladium-lead intermetallic compound is represented by the X-ray diffraction angle (20) 38.
- PdZPb atomic ratio
- the maximum intensity peak attributed to the diffraction of the (111) plane of the palladium-lead intermetallic compound is represented by the X-ray diffraction angle (20) 38.
- a high-purity supported catalyst comprising a compound can be obtained.
- the alcohol-based The yield is remarkably reduced, for example, when the production of methyl formate is increased, and when it exceeds 38.70 °, the decomposition of aldehyde becomes remarkable, and the yield based on aldehyde is reduced.
- the amount of supported lead exceeds 1.3 in terms of atomic ratio, formation of methyl formate becomes remarkable, and when it is less than 0.7, the selectivity of the target carboxylic acid ester such as MMA due to decomposition of aldehyde decreases. Is big.
- the catalyst obtained by the production method of the present invention has improved yields based on aldehyde and alcohol.
- the supported palladium Z lead atomic ratio is brought close to 3 ⁇ 0.7 to 3Z 1.3 and 3Z1, and does not contain excess lead. P without lattice defects d 3 P b! It is now possible to obtain a catalyst containing an intermetallic compound with high purity. Hence, it is possible to obtain a catalyst in which the amount of lead carried on the catalyst is as close as possible to the palladium lead atomic ratio of 31.
- the selectivity of the carboxylic acid ester such as MMA was low even with the catalyst prepared with the composition in which the lithium atomic ratio of lead was close to 31 as described above.
- catalyst precursor palladium compound is supported, palladium compound and catalyst precursor of lead compounds ing is carried, there is a lead ion, yet lower (C, one C 5) fatty acids, lower (Ci-Cs) Formalin, formic acid, hydrazine, methanol, or molecular hydrogen under the condition that an alkali metal salt or an alkaline earth metal salt of a fatty acid coexists.
- the supported palladium-Z lead-containing catalyst obtained by the above-described catalyst production method of the present invention can be suitably used for a reaction for producing a carboxylic acid ester by reacting an aldehyde with an alcohol and molecular oxygen.
- the amount of the catalyst used can be largely changed depending on the type of the reaction raw materials, the composition and preparation method of the catalyst, the reaction conditions, the reaction type and the like, and is not particularly limited. When the reaction is carried out by using, it is preferable to use 0.04 to 0.5 kg per liter of the reaction solution.
- activation means that the catalyst intermediate is reformed or modified by various methods to obtain a catalyst that satisfies all of the essential requirements of the catalyst of the present invention.
- Means Examples of catalyst intermediates include conventional catalysts prepared by known methods, and catalysts of the present invention which are deteriorated by the use of Spent catalysts that did not satisfy the conditions can be mentioned.
- a typical known method for preparing a catalyst intermediate to be activated includes, for example, an aqueous solution containing a soluble palladium compound such as palladium chloride and a soluble lead compound such as z or lead acetate. Add the carrier, heat at 20 to 100 ° C, impregnate the carrier with the aqueous solution for 1 to 24 hours, and then reduce with formalin, formic acid, hydrazine, methanol, hydrogen gas, etc. .
- a lead compound may be supported before the palladium compound is supported, or the palladium compound may be supported as described above. And a lead compound at the same time.
- various production methods are possible, such as supporting a palladium compound and coexisting a lead compound in the reduction step.
- the catalytic metal species in addition to palladium and lead, different elements.
- mercury, thallium, bismuth, tellurium, nickel, chromium, cobalt, indium, tantalum, copper, zinc, zirconium, hafnium, tungsten, manganese, silver, rhenium antimony, tin, rhodium It may contain ruthenium, iridium, platinum, gold, titanium, aluminum, boron, silicon, and the like.
- These different elements can usually be contained in an amount not exceeding 5% by weight, preferably not exceeding 1% by weight, based on the amount of all the catalytic species after reduction.
- At least one kind selected from an alkali metal compound and an alkaline earth metal compound is used at the time of preparing the catalyst intermediate, and the alkaline metal and the alkaline earth metal are supported on the carrier.
- the alkali metal or alkaline earth metal is usually selected from the range of 0.01 to 30% by weight, preferably 0.01 to 5% by weight, based on the total amount of the catalytic species after reduction. .
- These foreign elements, Al metal and Al earth metal may be substituted by a small amount of metal penetrating between crystal lattices or a part of the crystal lattice metal.
- the alkali metal compound and the alkaline or alkaline earth metal compound may be added to a solution containing a palladium compound or a lead compound at the time of preparing the catalyst intermediate, and may be adsorbed or adhered to the carrier, or may be preliminarily supported.
- a catalyst intermediate can also be prepared using the carrier thus obtained. Further, it can be added to the reaction system when performing the reduction reaction.
- a lead compound is an organic metal salt such as an organic acid salt such as formate and acetate, an inorganic acid salt such as sulfate, hydrochloride and nitrate, an amine complex, and a benzonitrile complex. , Oxides and hydroxides.
- Palladium chloride and palladium acetate are suitable as the palladium compound, and lead nitrate and lead acetate are preferable as the lead compound.
- Alkali metal compounds and alkaline earth metal compounds are also selected from organic acid salts, inorganic acid salts, hydroxides and the like.
- the carrier is widely selected from silica, alumina, silica-alumina, crystalline metal silicate, magnesia, silica-alumina-magnesium, magnesium hydroxide, titania, calcium carbonate, activated carbon, etc.
- silica-alumina, silica-alumina-magnesia, crystalline metal silicate, or silica that satisfies the above conditions is preferred. It is preferred to choose from alumina, silica-alumina-magnesia, and crystalline metal silicate.
- the amount of palladium supported on the carrier is not particularly limited, but is usually 0.1 to 20% by weight, and preferably 1 to 10% by weight, based on the weight of the carrier.
- the amount of lead carried is not particularly limited either, but is usually 0 to 20% by weight, preferably 1 to 10% by weight, based on the weight of the carrier. / 0 .
- the atomic ratio of the supported palladium / lead is more important than the supported amounts of palladium and lead. That is, palladium, or palladium and lead, to be activated in the present invention is
- the PdPb atomic ratio (S) of the catalyst intermediate supported on the carrier is as wide as 3 Z 0 ⁇ S ⁇ 3 Z 10, and practically 3 0 0.1 ⁇ S ⁇ 3/3
- the preferred Pd / Pb atomic ratio depends on whether one of the following first to fourth activation methods is selected.
- activation refers to a step of obtaining the catalyst of the present invention by using palladium or a catalyst intermediate in which palladium and lead are already supported as a metal, as described above. The method is disclosed.
- the above catalyst intermediate is prepared in water, an alcohol such as methanol, or a mixed solvent thereof for 20 to 10 times.
- An activation method includes reduction in the presence of lead ion while heating to 0 ° C.
- an inert solvent other than alcohols such as water and methanol can be selected, but water is preferred for practical use.
- Formalin, formic acid, hydrazine, methanol, or molecular hydrogen can be used as a reducing agent used as an activator for the catalyst intermediate supporting palladium and lead. .
- Formalin In the case of hydrazine and formic acid, it is only necessary to add a solution of formalin, hydrazine, formic acid, water and Z or methanol to the catalyst intermediate dispersion. Further, when methanol is used as the activator, it is only necessary to disperse the catalyst intermediate in methanol, which is convenient.
- a hydrogen-containing gas having a hydrogen concentration of 0.1% by volume or more diluted with pure hydrogen gas or an inert gas such as nitrogen or methane is preferably subjected to atmospheric pressure or several tens of atmospheres. It is preferably carried out by blowing into the aqueous solution of the catalyst intermediate dispersion under normal pressure or several atmospheric pressures.
- the amount of formalin, formic acid, hydrazine, methanol or molecular hydrogen used is generally from 0.1 to the molar amount of the supported palladium: 0.1 to 10 times the molar amount of L, practically 0.1 to 1 mol. 5- to 10-fold molar is used. There is no particular problem if this amount is exceeded. If an alkali such as caustic soda is added at the same time as the activator, the activation proceeds easily. Usually, about 110 to equimolar amount is added to the activator.
- lead ions coexist during activation.
- a lead-containing substance there is no particular limitation as long as it dissolves as lead ions. Examples include organic acid salts such as formate and acetate, inorganic salts such as sulfates, hydrochlorides and nitrates, oxides and hydroxides, with high solubility of lead nitrate and lead acetate. And the like are preferred.
- these lead compounds are added to a dispersion obtained by dispersing a catalyst intermediate in a solvent composed of water, methanol, or a mixture thereof to perform an activation treatment operation.
- the amount of the lead compound to be added differs depending on the catalyst intermediate to be activated, but is generally Pd / Pb based on the amount of palladium supported on the catalyst intermediate to be activated.
- the required minimum amount was selected from the range of 3 / 0.01 to 32 in atomic ratio, and the lead compound corresponding to this amount was dissolved in water, methanol, or a solvent such as a mixture thereof.
- the catalyst intermediate is dispersed in the solution and an activation treatment operation is performed.
- the catalyst intermediate preferably has a PdZPb atomic ratio (S) power of S3 / 0 ⁇ S ⁇ 3 / 1.3.
- the Pd and Pb-supported catalyst obtained by the above activation treatment should have a PdPb atomic ratio of 3 / 0.7 to 3 / 1.3, and as close as possible to 3/1.
- the amount of lead added in the activation step is 30.03 to Pd / Pb atomic ratio based on the amount of supported palladium. A range of 3 / 0.6 is preferred.
- the lead compound may be added to the solvent before starting the activation treatment, or may be added continuously or intermittently during the activation treatment.
- C - C 5 is favored arbitrary keep adding fatty acid to the system. If the amount of the lower fatty acid to be added is too large, the amount of lead eluted is too large and the adverse effect on the final catalyst becomes remarkable. Preferably, it is selected from the range of 1 to 15 moles. Practically, it is preferable to select acetic acid which is easily available.
- lower fatty acids may be added at the same time as the reducing agent used as the activator, but if they are added before the reducing agent, the required amount of lead is obtained from the catalyst intermediate to be activated. Sufficiently elute It is more effective because it can be done. In addition, even when a lead compound is added, the addition of these lower fatty acids is preferable because it has the advantage that the amount of lead to be added can be reduced.
- an alkali metal salt or an alkaline earth metal salt of a lower fatty acid sodium acetate, magnesium acetate and the like are preferable.
- an alkali metal salt and / or an alkaline earth metal salt can be used in place of the above-mentioned lower fatty acid that elutes lead ion from the catalyst intermediate.
- the above activation treatment operation can be performed at a temperature of room temperature to 200 ° C. Apply the necessary pressure to maintain the liquid phase. Preferably, it is carried out at 40 to 160 ° C and normal pressure to several atmospheres.
- the activation treatment time varies depending on the type of catalyst and treatment conditions, but is generally several minutes to 100 hours. It is convenient to set conditions so that the process is completed within a few hours. The completion of the treatment can be easily determined by measuring the X-ray diffraction angle of the (111) plane of the palladium Z lead intermetallic compound of the obtained catalyst.
- the reactor used for the activation treatment is not particularly limited, and can be an ordinary stirred tank reactor.
- This second activation method involves subjecting the catalyst intermediate to an oxidation treatment and a reduction treatment as follows.
- the reduction treatment with methanol gas is usually carried out under the flow of a methanol-containing gas with a methanol concentration of 0.1% by volume or more, diluted with pure methanol gas or an inert gas such as nitrogen or methane. This is usually carried out by heating the catalyst intermediate to 300 to 500 ° C. under a pressure of several to several atmospheres for 1 to 10 hours. If the treatment temperature is lower than 300 ° C., sufficient catalytic performance cannot be obtained, and if it is higher than 50 ° C., it is not preferable because the activity is presumed to be caused by semi-molten metal particles.
- the catalyst intermediate In the reduction treatment with molecular hydrogen (hydrogen gas), the catalyst intermediate is heated to 200 to 500 ° C. for 1 to 10 hours under a normal pressure or several tens of atmospheres in a hydrogen gas stream. This is done.
- hydrogen reduction as well as in the case of methanol reduction, if the heating temperature is too high, the activity of the catalyst is reduced, and if it is too low, sufficient catalytic performance cannot be obtained.
- the reduction treatment can be performed with methanol gas, molecular hydrogen or (C 2 -C 4 ) refin gas as described above. Rather than performing a reduction treatment with a nor gas or a (C 2 -C 4 ) gas and terminating the activation treatment, it is more preferable to perform a reduction treatment with molecular hydrogen last.
- the oxidation treatment with molecular oxygen and the reduction treatment with methanol gas, molecular hydrogen or (C 2 -C 4 ) gas are carried out under the same conditions as those described above. Will be The number of repetitions is not particularly limited, and varies depending on the type of the catalyst intermediate used.
- the atomic ratio (S) of P, Z, and P is 3 Z 0.7 ⁇ S ⁇ 3 / 1.3
- the maximum intensity peak attributed to the diffraction of the (111) plane of the palladium-lead intermetallic compound is represented by the X-ray diffraction angle (20) 38 It may be carried out until the catalyst of the present invention shown in the range of 55 to 38.70 degrees is obtained, but generally it is carried out 2 to 10 times.
- the palladium-Z lead atomic ratio (S) is 3 Z 0.7 ⁇ S ⁇ 3 / 1.3
- the X-ray diffraction characteristics satisfy the conditions of the catalyst of the present invention. It is effective to use a catalyst intermediate that is not used.
- the oxidation-reduction treatment is repeated. Many impurities including lead remain after the activation treatment.
- the formic acid, acetic acid to process a lower (C i- c 5) fatty acids such as propionic acid, butyric acid, Ma Lei phosphate, meta click Li Le acid
- a high-purity catalyst having a palladium / lead atomic ratio (S) of 30.7 ⁇ S ⁇ 3 / 1.3 is obtained.
- the treated catalyst intermediate is converted to a lower (C! -Cs) fatty acid in water, alcohol such as methanol, or a mixture thereof.
- Alcohol such as methanol, or a mixture thereof.
- Solvents other than alcohols, such as water and methanol, can be selected as long as they are inert and stable to the treated catalyst intermediate.However, water is preferred in practice.
- the concentration of the lower fatty acid in the reaction solution is selected from the range of from 0.1 to 20% by weight.
- the processing temperature is from room temperature to 200 ° C., preferably from 40 to 160 ° C.
- Oxidation treatment and reduction treatment were performed according to the second activation method described above, but as an alternative method of obtaining a high-purity catalyst from a low-purity catalyst, the second activation method of the present invention was used.
- carboxylic acid such as methacrylic acid by-produced during the carboxylic acid ester production reaction is used to remove lead-containing impurities during the desired carboxylic acid ester production reaction. This can eliminate the need for the treatment with the lower fatty acids described above.
- a lower (C i one C 5) arbitrarily favored and the this the addition of alkali metal salts and Z or alkaline earth metal salts of fatty acids.
- the alkali metal salt and the alkaline metal salt are added in an amount of about 0.1 to 30 moles based on the supported palladium. Preferably, it is selected from the range of 1 to 15 moles. Lower (C, one C 5) selected alkali metal salts of fatty acids, the concentration of the reaction solution of the alkaline earth metal salt from 0.1 to 2 0 wt% Devour. As an alkali metal salt or an alkaline earth metal salt of a lower fatty acid, sodium acetate, magnesium acetate or the like is preferable.
- alkali metal salts can also be used in place of the lower fatty acids described above.
- the alkali metal or the alkaline earth metal is converted to an oxide, hydroxide or carbonate. Can also be added.
- These alkali metal and alkaline earth metal compounds can be used alone or in combination of two or more.
- a third activation method according to the present invention will be described.
- the catalyst intermediate used in the third activation method preferably has a palladium-Z-lead atomic ratio (S) of 32.5 ⁇ S ⁇ 3/10, which is prepared by a known method. In other words, 3 / 2.5 ⁇ S ⁇ 3/5.
- S palladium-Z-lead atomic ratio
- the third activation method uses a palladium-zinc atomic ratio (S) of 32.
- S palladium-zinc atomic ratio
- This is a simple method of treating a catalyst intermediate with a large amount of lead carrying 5 ⁇ S ⁇ 3/10 with a lower (d-C 5 ) fatty acid.
- the catalyst intermediate is dispersed in an aqueous solution containing 0.1 to 20% by weight of acetic acid as illustrated in Example 35 described later, and the mixture is heated while stirring.
- the third lower (d-C 5) used in the activation method fatty acids are formic acid, propionic acid, butyric acid, Ma Lei phosphate, select menu Tak Li Le acid or al.
- Acetic acid is industrially preferred and readily available.
- These lower fatty acids are preferably used as a solvent having a concentration of 0.1 to 20% by weight using a solvent such as water, an alcohol such as methanol or a mixture thereof. More preferably, it is 1 to 15% by weight.
- a solvent other than alcohol such as water or methanol can be selected, but it is convenient to use as an aqueous solution.
- the catalyst When the catalyst is activated using an inorganic acid such as a mineral acid or sulfuric acid or an acid such as p-toluenesulfonic acid, good catalytic performance cannot be obtained, and the above lower fatty acid does not exceed 20% by weight. It is important to use at a concentration.
- an inorganic acid such as a mineral acid or sulfuric acid or an acid such as p-toluenesulfonic acid
- the activation treatment may be performed while continuously supplying the lower fatty acid to the reactor, or the lower fatty acid may be charged and treated together with the catalyst intermediate.
- the amount of the lower fatty acid to be used varies depending on the activation treatment method.
- the lower fatty acid can be used in the range of 10 to 1,000 times the molar amount of the supported palladium.
- a lower (d-C 5) ⁇ Luke Li metal salts of fatty acids, and Roh or alkaline earth metal salt additives child and further preferred arbitrariness a.
- the alkali metal salt and the Z or alkaline earth metal salt are added in an amount of about 0.1 to 30 times mol based on the supported palladium.
- the concentration of the lower fatty acid alkali metal salt or alkaline earth metal salt in the reaction solution is selected from 0.1 to 20% by weight.
- an alkali metal salt or an alkaline earth metal salt of a lower fatty acid sodium acetate, magnesium acetate and the like are preferable. (These metal salts of lower fatty acids and / or earth metal salts of lower fatty acids can be used in place of the above-mentioned lower fatty acids.)
- Alkaline earth metals can also be added as oxides, hydroxides and carbonates. These alkali metal and alkaline earth metal compounds can be used alone or in combination of two or more.
- the activation temperature is from room temperature to 200 t :, preferably from 40 to 160 ° C.
- the activation treatment time varies depending on the treatment type, the treatment temperature, and the type of the catalyst intermediate, but if the treatment time is too long, the catalyst performance may be reduced. Usually, it is selected from the range of 0.1 hour to 100 hours, preferably 0.5 to 20 hours.
- the third activation process is a stirred tank reactor, bubble column reactor, etc.
- the catalyst can be used by dispersing the catalyst intermediate in a slurry state in the solvent described above.
- the concentration of the catalyst intermediate in the slurry is usually 0.44 to 0.5 kg per liter.
- the catalyst intermediate can be filled in a fixed bed and a solution containing lower fatty acids can be passed through.
- a fourth activation method according to the present invention will be described.
- a palladium and lead-supported catalyst prepared by a known method (hereinafter, also referred to as a “catalyst intermediate” in the same manner as in the first to third activation methods)
- the desired activation can be achieved by a simple method of reacting the aldehyde with an aldehyde and an alcohol or with an alcohol at a specific oxygen partial pressure in the presence of lead ions.
- aldehyde to be used in the activation of the catalyst of the present invention, for example, formaldehyde; ⁇ Seto aldehydes, pro pin On'arudehi de, Lee Sobuchiruarudehi de, Dali Okisaru of any one C 1 0 aliphatic saturated aldehyde ; ⁇ click b lay down, meta click b Tray down, click collected by filtration N'arudehi C, such as de 3 -.
- Examples of anore call include, for example, , Isopropanol, octanol, etc. 0 fat aliphatic saturated alcohols, ethylene glycol, C 2, such as pigs Njioru - C i 0 diol; ⁇ Lil alcohols, C 3- C i, such as meta Rirua alcohol. Aliphatic unsaturated alcohols; C 6 -C 2 Q aromatic alcohols such as benzyl alcohol; These alcohols can be used alone or as a mixture of two or more kinds.
- the ratio of the amount of aldehyde to the amount of alcohol used is not particular limitation; for example, it can be used in a wide range such as the molar ratio of aldehyde Z alcohol of 1100 to 10/1, Specifically, it can be used in a molar ratio of 1/2 to 1/50. It can also be carried out with alcohol alone.
- the amount of the catalyst intermediate used in the fourth activation method can be largely changed depending on the type of the aldehyde and the alcohol, the type of the catalyst intermediate, and other activation conditions. Although not particularly limited, when the catalyst is activated in a slurry state, it is preferable to use 0.04 to 0.5 kg in one slurry.
- organic acid salts such as formate and acetate
- inorganic acid salts such as sulfate, hydrochloride and nitrate, oxides and hydroxides, and lead nitrate and lead acetate having high solubility. And the like are preferred.
- the amount of the lead-containing substance to be added varies depending on the type of the catalyst intermediate, but based on the amount of the supported palladium, the lead content corresponding to the palladium-Z lead atomic ratio of 3 / 0.01 to 3/2. Dissolve or disperse the substance in the above aldehydes and alcohols or alcohols.
- the above-mentioned lead-containing substance may be added before starting the activation treatment operation, or may be added continuously or intermittently during the activation treatment operation. For this reason, the aldehyde and alcohol, or the lead concentration in the alcohol cannot be unambiguously determined, but it is usually 0.1 to 2, OOOppm, and often 1 to 200 ppm. To shorten the time required for activation, it is advisable to increase the lead concentration.
- the palladium / lead atomic ratio (S) of the catalyst intermediate obtained by the activation treatment according to the fourth method is 30.7 ⁇ S ⁇ 3 / 1.3, and more preferably as close to 31 as possible.
- the activation treatment The amount of the lead-containing substance added in this step is preferably such that the atomic ratio of palladium to lead is in the range of 3 / 0.03 to 3 / 0.6, based on the amount of supported palladium.
- a lead-containing substance In order to make a lead-containing substance present, it is common to add a lead-containing substance as described above, but the purity of the catalyst intermediate is low, for example, a palladium-lead atomic ratio of 3 / 1.3 to 3
- these lead components which are impurity components, are dissolved from the catalyst intermediate. It can also be present as lead ions and used for activation purposes. In this case. Good results can be obtained by adding lower (C-Cs) fatty acids such as propionic acid, acetic acid, butyric acid, maleic acid, and methacrylic acid to the system to help dissolve the lead component.
- acetic acid For lower fatty acids, it is preferable to select acetic acid which is easily available.
- the lower fatty acid is added in an amount of about 0.1 to 30 times the molar amount of the supported catalyst for the catalyst intermediate. More preferred :! Choose from a range of ⁇ 15 times mol.
- the concentration of the lower fatty acid in the reaction solution is selected from the range of 0.1 to 20% by weight.
- These lower fatty acids may be added simultaneously with the activation treatment, If added before the activation treatment is started, the amount of lead required for the activation can be sufficiently dissolved from the catalyst intermediate, which is effective. In addition, even when a lead compound is added, the addition of these lower fatty acids is preferable because it has the advantage that the amount of lead to be added can be reduced.
- the oxygen partial pressure at the outlet of the reactor is set to 0.8 kg / cm 2 or less.
- the oxygen partial pressure 0. 8 kg Roh cm 2 hereinafter, preferably 0. 4 kg Z cm 2 Dearuko and is important ⁇ Li. O kg Roh cm 2 even Yo Rere.
- the oxygen used can be molecular oxygen, i.e. oxygen gas itself, or a mixed gas of oxygen gas diluted with a diluent inert to this activation method, e.g. nitrogen, carbon dioxide, etc. .
- Air can be used, and in any case, it is important to control the oxygen supply to keep the outlet oxygen partial pressure at 0.8 kg Z cm 2 or less. If the oxygen partial pressure is set low, the amount of lead present during activation can be reduced. As the amount of lead supplied to the reactor increases, the cost of detoxifying lead in wastewater increases, so that the amount of lead practically ranges from 1 to 200 PPm to the minimum required.
- the oxygen partial pressure at the outlet of the reactor is preferably set to 0.4 kgcm 2 or less.
- Preferred catalyst intermediates for applying this fourth method are those whose PdZPb atomic ratio (S) power S3 0 0 ⁇ S ⁇ 3/10.
- the purity of the catalyst intermediate is low, such as palladium Catalyst intermediates with a Z lead atomic ratio (S) of 31.3 ⁇ S ⁇ 3/10, and actually 3 / 1.3 ⁇ S ⁇ 33, contain a lot of lead impurities.
- the oxygen partial pressure is set to be higher. Therefore, it is necessary to change the oxygen partial pressure and the amount of lead to be present within the range described above for the catalyst intermediate to be activated.
- the reaction pressure in the activation treatment may as in child in any wide pressure range under pressure from reduced pressure, usually at a total pressure comprising an inert gas or solvent vapor pressure 0. 5 ⁇ 2 0 kg Z cm 2 It is carried out at a pressure of The total pressure should be set so that the oxygen concentration of the reactor effluent gas does not exceed the explosive limit (8%).
- This fourth activation operation can be performed at a temperature from room temperature to 200 ° C. Apply the necessary pressure to maintain the liquid phase. Preferably, it is carried out at 40 to 160 ° C and normal pressure to several atmospheres.
- the activation treatment time varies depending on the type of the catalyst and the treatment conditions, but conditions are generally set so that the treatment is completed within 100 hours, which is several hours to 500 hours. It is convenient to set.
- the reactor used for activation is not particularly limited, and can be a normal stirred tank type reactor.
- the palladium-Z lead atomic ratio (S) power S 3 0.7 ⁇ 0.7 S ⁇ 3 / 1.3, and the X-ray diffraction angle (2 ⁇ ) of the (111) plane of the palladium-lead intermetallic compound should be set to 38.55 to 38.70. bets can be, Ru is possible to get high purity of the onset Ming catalyst comprising fewer lattice defects high quality P d 3 P bi compound.
- a palladium / lead intermetallic compound-supported catalyst with a controlled surface structure refers to the Pd 3d (3/2) electron and Pd 3d (5/2) of metallic palladium in the X-ray photoelectron spectrum.
- Catalysts with such controlled surface structures are subject to the following conditions:
- the catalyst may be obtained by performing the activation treatment of any of the above-described first to fourth methods on a catalyst intermediate.
- a method for reliably obtaining a surface-controlled catalyst is as follows:
- the catalyst used for controlling the surface structure of the present invention is not particularly limited as long as it is a catalyst intermediate in the method 1), but the palladium-lead atomic ratio (S) is 30.7 in the method 2).
- an aldehyde and an alcohol or an alcohol are used as in the above-described fourth activation method, and the aldehyde and the alcohol to be used are used.
- the quantitative ratio is the same as in the fourth activation method.
- lead ions are present. It is common to add lead-containing substances for this It is. When adding a lead-containing substance, there is no particular limitation as long as it dissolves as lead ions. Examples include organic acid salts such as formate and acetate, inorganic salts such as sulfates, hydrochlorides and nitrates, oxides and hydroxides, but lead nitrate, which has high solubility, Lead acetate and the like are preferred.
- the amount of lead added depends on the catalyst whose surface structure is to be controlled.However, based on the amount of palladium supported, the palladium / lead atomic ratio is between 3 / 0.01 and 3/2.
- a lead-containing substance corresponding to the above is dissolved or dispersed in the above-mentioned aldehyde and alcohol or an alcohol solvent to perform a surface structure control treatment.
- the above-mentioned lead compound may be added before starting the surface structure control treatment operation, or may be added continuously or intermittently during the surface structure control treatment operation. Therefore, the concentration of lead in the aldehyde and the alcohol or in the alcohol varies, but is usually 0.1 to 2, OOOppm, preferably:! ⁇ 200ppm. To shorten the time required for controlling the surface structure, it is advisable to increase the lead concentration.
- the surface structure In order to make the palladium-lead atomic ratio (S) of the catalyst obtained by the surface structure control treatment 30.7 ⁇ S ⁇ 3 / 1.3, and as close as possible to 3/1, the surface structure
- the amount of lead added in the control treatment process should be within the range of palladium-lead atomic ratio (S) force; 3 ⁇ 0 ⁇ 03 ⁇ S ⁇ 3 / 0.6, based on the amount of supported palladium. Is preferred.
- S palladium-lead atomic ratio
- the purity of the catalyst is low, for example, a palladium-lead atomic ratio ( If S) is a catalyst such as 3Z1.3S ⁇ 3/3, lead such as lead oxide and simple metal lead contains a lot of impurities. These lead components, which are impurity components, can be dissolved from the resulting catalyst and used for the purpose of controlling the surface structure.
- Bro acid To aid dissolution of the lead component acetic acid, butyric acid, Ma Lei phosphate, lower, such as meta click Li Le acid (CL- c s) fatty correct preferred is a this added to the system ⁇ For lower fatty acids, it is preferable to select acetic acid which is easily available.
- Lower aliphatic acid is c Yo Li favored properly adding 0.1 to 3 0-fold moles based on supported palladium selected from the range of 1 to 5 moles.
- concentration of the lower fatty acid in the aldehyde or the alcohol or in the alcohol is 0.1 to 20% by weight. It is preferable to select from the range.
- lower fatty acids such as methacrylic acid are by-produced from aldehydes and alcohols during the surface structure control treatment, the amount of lower fatty acids to be added should be reduced or made unnecessary. You can do it.
- These lower fatty acids may be added at the same time as the surface structure control treatment, but by adding them before the surface structure control treatment is started, it is necessary to control the surface structure from the target catalyst for the surface structure control. An effective amount of lead can be sufficiently dissolved. In addition, even when a lead compound is added, the addition of these lower fatty acids is advantageous because it can reduce the amount of lead to be added.
- an alkali metal salt and / or an alkaline earth metal salt of a lower (Ci-Cs) fatty acid is added in an amount of about 0.1 to 30 moles based on the supported palladium.
- concentration of the reaction solution in is selected from 0.1 to 2 0 wt. / 0.
- Alkali metal and alkaline earth metal can also be added as oxides, hydroxides and carbonates. These alkali metal and / or earth metal compounds can be used alone or in combination of two or more.
- the palladium / lead used there is no particular limitation on the supported catalyst (so-called catalyst intermediate), but the oxygen partial pressure at the outlet of the reactor must be 0 to 0.4 kg / cm 2 . Preferably, the oxygen partial pressure is between 0 and 0. S kg Z cm 2 .
- the oxygen used can be in the form of molecular oxygen, that is, oxygen gas itself or a mixed gas obtained by diluting oxygen gas with an inert diluent, for example, nitrogen or carbon dioxide, according to the surface structure control method.
- Air can also be used, and in any case, it is important to control the oxygen supply to keep the outlet oxygen partial pressure to 0.4 kg Z cm 2 or less.
- the oxygen partial pressure is set low, the amount of lead present in the above method 1) can be reduced.
- a catalyst having a low purity for example, having a palladium / lead atomic ratio (S) of 3 Z 1. Contains a large amount of lead impurities. Therefore, when controlling the surface structure of such a low-purity catalyst, It is preferable to effectively use these lead components, which are impurity components. In this case, the oxygen partial pressure is set to be higher. Therefore, it is necessary to change the oxygen partial pressure and the amount of lead present within the above-mentioned range depending on the type of the catalyst to be subjected to the surface structure control treatment.
- the catalyst used as the object of the surface structure control is the specific catalyst described above, and the oxygen partial pressure at the outlet of the reactor is 0 to 0.8 kg.
- Z cm 2 preferably 0 0. a 4 kg Z cm 2.
- the oxygen used may be molecular oxygen, that is, oxygen gas itself, or a mixed gas obtained by diluting oxygen gas with an inert diluent, such as nitrogen or carbon dioxide, according to the surface structure control method.
- Air can also be used, and in any case, it is important to control the oxygen supply to keep the outlet oxygen partial pressure to 0.8 kg Z cm 2 or less. If the oxygen partial pressure is set low, the amount of lead present during the surface structure control treatment can be reduced.
- the reaction pressure can and benzalkonium be implemented in any wide pressure range under pressure from reduced pressure, usually carried out at 0. Pressure of SSO kg Z cm 2.
- the total pressure should be set so that the oxygen concentration in the reactor effluent gas does not exceed the explosion limit (8%).
- the surface structure control treatment operation can be performed at a temperature from room temperature to 200 ° C. Apply the necessary pressure to maintain the liquid phase.
- the reaction is carried out at 40 to 160 at atmospheric pressure to several atmospheres.
- the surface structure control treatment time varies from several hours to 500 hours, depending on the type of catalyst and the treatment conditions. It is convenient to set conditions so that processing is completed within 100 hours.
- the reactor used for controlling the surface structure is not particularly limited, and can be an ordinary stirred tank reactor.
- the atomic ratio (Pd / Pb) of palladium and lead is 3 / 0.7 to 3: 1.
- the maximum intensity peak attributed to the diffraction of the (111) plane of the palladium-lead intermetallic compound is represented by the X-ray diffraction angle (20) 38.5.5- It is shown in the range of 38.70 degrees, and in the X-ray photoelectron spectrum, the Pd 3d (3Z2) electron and Pd 3d (5/2) electron of the metal
- the catalyst of the present invention can be suitably used for a reaction for producing a carboxylic acid ester by reacting an aldehyde with an alcohol and molecular oxygen.
- the amount of catalyst used can vary widely depending on the type of reaction raw materials, the composition and preparation method of the catalyst, the reaction conditions, the type of reaction, etc., and is not particularly limited, but when the catalyst is reacted in a slurry state. For this purpose, it is preferable to use 0.04 to 0.5 kg per liter of the reaction system.
- the alcohol may be, for example, a C, —C, 0 aliphatic saturated alcohol such as methanol, ethanol, isopropanol, or octanol. alcohol; Echirenda recall, C 2, such as pigs Njioru - C t 0 diol; ⁇ Li Honoré Al co Lumpur, meta Li Norea Honoré calls etc. C 3 —C 1Q aliphatic unsaturated alcohols; C 6 —C 20 aromatic alcohols such as benzyl alcohol; These alcohols can be used alone or as a mixture of two or more kinds.
- the amount ratio of the aldehyde to the alcohol is not particularly limited.
- the molar ratio of aldehyde hydroxyl is 10 to: LZl, 000. Although it can be carried out in such a wide range, it is generally carried out in a molar ratio in the range of 12 to 1/50.
- the method for producing a carboxylic acid ester according to the present invention can be carried out by any conventionally known method such as a gas phase reaction, a liquid phase reaction, and a liquid reaction.
- a gas phase reaction a liquid phase reaction
- a liquid reaction a liquid reaction
- any reactor type such as a bubble column reactor, a draft tube reactor, and a stirred tank reactor can be used.
- the oxygen used in the carboxylic acid ester production reaction of the present invention is molecular oxygen, that is, oxygen gas itself or a mixed gas obtained by diluting oxygen gas with a diluent inert to the reaction, such as nitrogen or carbon dioxide gas. And air can be used.
- the reaction pressure is Ru can and this you implemented in any wide pressure range under pressure from reduced pressure, but usually is carried out at a pressure of 0. SSO kg Z cm 2.
- the total pressure should be set so that the oxygen concentration in the reactor effluent does not exceed the explosion limit (8%).
- an alkali metal or alkaline earth metal compound eg, oxide, hydroxide, carbonate, carboxylate, etc.
- an alkali metal or alkaline earth metal compound eg, oxide, hydroxide, carbonate, carboxylate, etc.
- setting the pH to 6 or more has the effect of preventing dissolution of the lead component in the catalyst.
- alkali metal or alkaline earth metal compounds can be used alone or in combination of two or more.
- the reaction can be carried out at a high temperature of 100 ° C. or more, but preferably 30 to 100 ° C.
- the temperature is preferably 60 to 90 ° C.
- the reaction time is not particularly limited and cannot be uniquely determined because it differs depending on the set conditions, but is usually 1 to 20 hours.
- the catalyst of the present invention is used together with the catalyst stabilization method first enabled by using the catalyst of the present invention.
- the present inventors have found that the desired carboxylic acid ester can be continuously and efficiently produced from aldehyde, alcohol and molecular oxygen.
- the inventors of the present invention have developed a catalyst using a catalyst in which palladium and lead are supported on a carrier, and from aldehydes, alcohols and molecular oxygen.
- the catalyst that caused the deterioration was analyzed and examined.
- the deteriorated catalyst had a reduced lead content, and correspondingly, about 0.1 to several ppm of lead was dissolved in the reaction solution.
- Example 10 of Japanese Patent Publication No. 62-7902 as an example of the reaction using the irrigation type reactor, there was no change in the reaction results even after 2,000 hours.
- the lead concentration in the reaction system is not particularly limited, but is usually 1 to 200 ppm. However, it is preferable that the lead concentration in the reaction system is low, and as described below, it is possible to control the oxygen concentration to 200 ppm or less, and preferably 100 ppm or less, by controlling the oxygen concentration. .
- a method for continuously producing a carboxylic acid ester from aldehyde, alcohol and molecular oxygen in the presence of a catalyst comprising palladium and lead supported on a carrier in the above, by performing the reaction while adding the lead-containing substance to the reactor, the deterioration of the catalyst is suppressed, and the carboxylic acid ester can be stably produced continuously. Furthermore, if the oxygen partial pressure at the reactor outlet is controlled to 0.1 kg / cm 2 or less, catalyst degradation can be suppressed even if the lead concentration in the raw material liquid supplied to the reactor is further reduced. Can be.
- the above-mentioned prevention of catalyst deterioration during the reaction can be achieved by (1) when performing the reaction while supplying the lead-containing substance to the reaction raw material liquid, the deterioration of the catalyst performance can be suppressed, and (2) This is based on two findings that maintaining the oxygen concentration in a specific range can reduce the required amount of lead-containing substance supplied to the reaction raw material liquid. less than, The mechanism for suppressing the catalyst deterioration will be described in more detail.
- a very simple method of adding a lead-containing substance to a raw material to be supplied to a reactor can be used without deteriorating the used catalyst and without reducing the intended carboxylic acid. Ester It was first discovered that efficient and continuous production was possible.
- the present inventors consider that the active hydrogen remaining on the palladium catalyst plays an important role. If the oxygen partial pressure at the reactor outlet side is controlled to a specific value or less, the action of active hydrogen on the catalyst can be enhanced, and even if the amount of lead-containing substance supplied to the reactor is small, We found that it was effectively incorporated into the catalyst.
- the amount of lead-containing substance supplied to the reactor can be reduced, and preferably, the amount is 0.8 kg Z cm.
- the concentration is set to 2 or less, the concentration of lead in the raw material liquid supplied to the reactor can be reduced to 1 to 200 ppm or less.
- the lead-containing substance added to the reaction system according to the catalyst stabilization method described above is not particularly limited as long as it is soluble in the reaction system as lead ions.
- Examples include organic acid salts such as formate and acetate, inorganic acid salts such as sulfates, hydrochlorides and nitrates, oxides and hydroxides, but lead nitrate and lead acetate with high solubility Etc. are preferred.
- the amount of the lead-containing substance to be added is large, it is preferable that the treatment cost for detoxifying the lead in the wastewater becomes higher, and the amount of by-product methyl formate is increased. no order, the oxygen partial pressure at the reactor outlet side 0.
- the pressure is set to 0.2 kgcm 2 or less so as to reduce the amount of the supplied lead-containing substance.
- the oxygen required for the reaction is not ensured, the conversion of the raw material aldehyde, which becomes oxygen deficient, will decrease, and undesirable by-products will be produced.
- the Pd / Pb atomic ratio was determined by inductively coupled plasma (ICP) emission spectroscopy using JY-38P2 manufactured by Seiko Electronics Industries, Japan as an ICP emission spectrometer. Were determined.
- ICP inductively coupled plasma
- the X-ray diffraction angle (2 ⁇ ) of the maximum intensity peak attributed to the diffraction of the (111) plane of the palladium-lead intermetallic compound in the powder X-ray diffraction pattern was determined by evacuation of the catalyst under vacuum evacuation. After removing low-molecular-weight adsorbed Z-absorbing components (mainly hydrogen) by treating at 3 ° C for 3 hours, RAD-RA, an X-ray diffractometer manufactured by Rigaku Denki Co., Ltd., Japan, was used. In accordance with the usual powder X-ray diffraction measurement procedure, use Cu Kct 1 line (1.54 It was determined by measuring the diffraction angle 20 of the (111) plane of the lead intermetallic compound.
- the X-ray diffraction angle (20 °) of the maximum intensity peak attributed to the (111) plane diffraction of the palladium-lead intermetallic compound in the powder X-ray diffraction pattern ) Is often simply referred to as “the X-ray diffraction angle (20) of the maximum intensity peak at the powder X-ray diffraction angle” or the like.
- Figures 1 and 2 show examples of palladium (3d) and lead (4f) measurements, respectively.
- the concentration of Sion measured by the following method was used as an index of water resistance.
- a 100 ml stainless steel container weigh 0.2 g of the carrier to be evaluated, add 20 g of water, seal, heat at 180 ° C for 1 hour, hydrolyze and elute into water
- the measured Si ion concentration was measured by ICP (plasma emission spectroscopy) using the ICP emission spectrometer described above.
- the specific surface area of the support was measured by a BET nitrogen adsorption method.
- the carrier was adjusted so that palladium chloride and lead nitrate corresponded to 100 parts by weight of the carrier and palladium and lead, respectively, so that the amounts of palladium and lead were 5 parts by weight and 6.5 parts by weight, respectively.
- the mixture was mixed with an aqueous solution containing 10% by weight of sodium and a 13% by weight aqueous solution of lead nitrate, and stirred at room temperature for 1 hour to completely adsorb palladium chloride and lead nitrate on the carrier.
- a hydrazine aqueous solution three times the molar amount of Pd + Pb is added dropwise while stirring, and the catalyst is reduced by reduction.
- the obtained catalyst is referred to as “catalyst intermediate”).
- the composition ratio of PdPb supported was 3Z1.95 in atomic ratio
- the X-ray diffraction angle of the maximum intensity peak in the powder X-ray diffraction pattern ( 20) was 38.745 degrees
- the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) and lead metal (4f) was 24.
- the NaOH concentration supplied to the reactor was controlled so that the pH of the reaction system was 7.1.
- the reaction product was continuously withdrawn from the reactor outlet at 0.6 liter / hr.
- the above activation process was completed in 50 hours.
- the reaction product withdrawn from the reactor outlet contained on average about 270 ppm lead. This is due to the action of methacrylic acid generated in the reaction system (the average concentration in the extracted reaction product is 1.1% by weight), and lead from the catalyst is converted into ions in the form of ions in the reaction system. It is presumed that the dissolved substance was reduced by active hydrogen generated by the reaction between the methanol mouth lane and methanol.
- the Pd / Pb atomic ratio was 31.24
- the X-ray diffraction angle (2 ⁇ ) of the maximum intensity peak in the powder X-ray diffraction pattern was 3 8.
- the reaction was carried out by charging 240 g of this catalyst, which was equipped with a catalyst separator, to an external circulation stainless steel bubble column reactor having a liquid phase part of 1.2 liters. .
- the reaction product was continuously extracted from the reactor outlet by overflow.
- the conversion of methacrolein was 57.3%, and the selectivity of MMA was 90.7%.
- propylene was produced at a selectivity of 1.7%, and methyl formate was produced at a yield of 0.085 mol mol MMA.
- productivity of MMA was 0.49 [MMA (g) Zg catalyst ⁇ time].
- the catalyst intermediate treatment conditions in the above method for measuring the X-ray diffraction angle in connection with the present invention that is, by treating the catalyst intermediate at 160 under vacuum evacuation for 3 hours, the adsorption of low molecular weight After removing occluded components (mainly hydrogen), the X-ray diffraction angle of the maximum intensity peak in the powder X-ray diffraction pattern of the catalyst intermediate was measured.
- the X-ray diffraction angle (20) was 38. It was 786 degrees.
- MMA formation reaction was performed under exactly the same conditions as in Example 1, and the reaction product was analyzed 10 hours after the start of the reaction.
- the conversion of lone is 55.2%
- the selectivity of MMA is 84.1%
- the selectivity of propylene as a by-product is 7.9%
- the methyl formate is 0%. 242 mol mol MMA was produced.
- Examples 2 to 6 and Comparative Examples 3-1, 3-2, 4-1-1, 4-2, 5 and 6 Using various catalyst intermediates shown in Table 1, MMA formation reaction was carried out as follows. Was done. In Examples 2 to 6, the same catalyst intermediate activation treatment as in Example 1 was performed, whereas in Comparative Examples 3 to 6, the catalyst intermediate activation treatment was not performed.
- Example 2 to 6 and Comparative Examples 3-1 to 4-1, 5 and 6 the MMA formation reaction was carried out under the same conditions as in Example 1.
- Comparative Examples 3-2 and 4-1-2 the same as Comparative Examples 3-1 and 4-1 except that the reaction system was set to 10% of methacrolein and the reaction temperature was set to 50 ° C.
- the reaction was performed as follows. Pd / Pb loading composition ratio (atomic ratio) in Examples 2 to 6 and Comparative Examples 3-1, 3, 2, 41, 42, 5, and 6, the maximum intensity peak in the powder X-ray diffraction pattern Table 1 shows the X-ray diffraction angle (20) and the reaction results of the test.
- the MMA formation reaction was carried out at a methacolein concentration of the reaction system of 10% and a reaction temperature of 50.
- the composition ratio of PdZPb supported was 3Z1.27 in atomic ratio, and the X-ray diffraction angle (2 ⁇ ) of the maximum intensity peak in the powder X-ray diffraction pattern was obtained.
- the force was S 38.691 degrees.
- the Pd / Pb supporting composition ratio was 3Z1.27 in atomic ratio and the powder X-ray diffraction pattern
- the X-ray diffraction angle (20) of the maximum intensity peak was 38.642 degrees.
- Example 1 The catalyst separator used in Example 1 was installed, and two externally circulating stainless steel bubble column reactors with a liquid phase of 1.2 liters were connected in series, and each reactor was activated. Each of the finished catalysts was charged in an amount of 240 g, and an MMA generation reaction was carried out as follows. A 36.7% by weight of metachlorin / metabolite was added to the first-stage reactor. Roh Lumpur solution was continuously fed at 0.5 4 Li Tsu Honoré Zh r,.
- the MA formation reaction was carried out under the same operation and reaction conditions as in Example 7, except that acrolein was reacted in place of methacrolein using the activated catalyst prepared in Example 3. Was done.
- the reaction product was analyzed after 10 hours, the conversion of acrolein was 58.2%, the selectivity of methyl acrylate (MA) was 91.3%, Ethylene was produced at a selectivity of 1.2% as a by-product, and ethyl ethyl formate was produced at a concentration of 0.055 mol MA.
- MA methyl acrylate
- Example 7 Example 7 was repeated except that the activated catalyst prepared in Example 4 was reacted with benzaldehyde in place of methanol and with ethanol in place of methanol. The production reaction of methyl benzoate was performed under the same operation and reaction conditions as in. After 10 hours, the reaction product was analyzed. The selectivity of ethyl benzoate was 93.2% at 2%.
- the reactor exit oxygen concentration 4.0 vol% (the oxygen partial pressure 0. 2 0 kg Z cm 2 equivalent) to change, 3 6 Kyoawase the reactor at the same time.
- Lead acetate was added to a 7 wt% metallochlorin Z methanol solution so that the lead concentration in the reaction system was 20 ppm.
- activation processing time After a lapse of 100 hours in total, the catalyst was withdrawn from the reactor and analyzed by the above-mentioned method.
- the composition ratio of Pd / Pb was 3 to 1.08 in atomic ratio, powder X
- -240 g of the catalyst whose surface structure was treated as described above was charged into an externally circulating stainless steel bubble column reactor equipped with a catalyst separator and having a liquid phase of 1.2 liters.
- the formation reaction was performed as follows. 36.7 wt% of lead acetate dissolved in the reactor so that the lead concentration in the feedstock solution would be 20 ppm.
- the reaction was carried out for 50 hours in the same manner as in Example 11, and then the catalyst was extracted from the reactor and analyzed.
- the composition ratio of PdZPb was 3Z in atomic ratio. 1.24, the X-ray diffraction angle (20) of the maximum intensity peak in the powder X-ray diffraction pattern is 38.652 degrees, and the X-ray diffraction angle of Pd (3d) / Pb (4f) The intensity ratio of the linear photoelectron vector was 0.89.
- Example 13 to 19 and Comparative Examples 8 to 10 the same MMA production reaction as in Example 11 was performed using the various catalyst intermediates described in Table 2.
- Example 13 to 19 the same catalyst intermediate activation treatment and surface structure control treatment of the activated catalyst as in Example 11 were performed, while in Comparative Examples 8 to 10, the catalyst intermediate activation treatment and surface structure were performed.
- the catalyst intermediate was used as such without any control treatment.
- Example 1 3 Pd 5 - ° Pb 3 - 21 / Si0 2 O 3 / 0.99 38.602 ° 1 / 0.21 62.7 89.8 2.13 0.038
- Example 1 4 Pd 5 ° Pb 3 ' 4, Mg 5 - ° / Si0 2 3 / 1.05 38.611 ° 1 / 0.43 63.8 91.1 1.21 0.043
- the data of the PdZPb atomic ratio and the X-ray diffraction angle (20) are the data obtained for the catalyst intermediate.
- An external circulation stainless steel bubble column reactor with a liquid separator of 1.2 liters was connected in series with a catalyst separator, and the catalyst intermediate obtained in Reference Example 1 was connected to each reactor.
- the catalyst was activated in the same manner as in Example 11, and 240 g of the catalyst subjected to the surface structure control treatment was charged to perform an MMA generation reaction.
- lead acetate was dissolved so that the lead concentration in the feedstock liquid was 20 ppm.
- the reaction product containing the catalyst withdrawn from the first-stage reactor by overflow is separated into liquid and solid and the catalyst is returned to the first-stage reactor, and only the obtained reaction product is 0.6 liter Z hr to the second stage reactor with 2 to 4 wt% NaOH nomethanol solution with 0.06 liter / hr, the gas discharged from the first stage reactor to the second stage reactor
- the oxygen concentration at the outlet of the second stage reactor was 2.2 volumes while venting. /. Performing (oxygen partial pressure 0. Llkg / cm 2 equivalent) shortage of the air in the Hare by the added to the second stage reactor the reaction temperature 8 0 ° C, a reaction pressure of 4. 6 kg / cm 2 Was.
- the NaOH concentration supplied to the first-stage reactor and the second-stage reactor was controlled so that the pH of the reaction system was 7.1.
- the reaction product obtained in the second stage reactor was continuously extracted from the second stage reactor outlet by overflow. After 500 hours, the reaction product withdrawn from the second-stage reactor was analyzed.
- the conversion of methacrolein was 81.6%
- the selectivity of MMA was 91.5%
- by-products As a result, propylene was produced at a selectivity of 1.36%
- methyl formate was produced at 0.049 mol MMA.
- the Pd-no-Pb supporting composition ratio of the first-stage reactor catalyst was 3 / atomic ratio. 1.05, X-ray diffraction angle of maximum intensity peak in powder X-ray diffraction pattern
- the catalyst ratio of PdZPb for the second-stage reactor catalyst is 3 / 0.98 in atomic ratio, and the X-ray diffraction angle (20) force of the maximum intensity peak in the powder X-ray diffraction pattern S3 8.6 1 2 degrees.
- the intensity ratio of the X-ray photoelectron spectra of the radiometal (3d) and the lead metal (4f) was 10.45. Further reaction under these conditions
- the lkg of the catalyst intermediate obtained in Reference Example 2 and the Pd / Pb carrying composition ratio (atomic ratio) of this catalyst intermediate were placed in a stirred tank reactor having a liquid phase of 6 liters. 3 liters of lead acetate trihydrate, 20.9 g, dissolved in 0.9 g of lead, which is insufficient to obtain 1.3, was charged at a reaction temperature of 90 ° C and a reaction pressure of 5 kg. / cm 2 and the outlet oxygen concentration 2.0 volume. /.
- the catalyst intermediate was activated for 20 hours by supplying air to the reactor while adjusting the amount of air so that the oxygen partial pressure became 0.10 kg / cm 2 .
- Supply and control of catalyst surface structure was.
- the NaOH concentration supplied to the reactor was controlled so that the PH of the reaction system was 7.1.
- the reaction product was continuously withdrawn from the reactor outlet by overflow.
- the composition ratio of PdZPb supported was 31.10 by atomic ratio, and the peak intensity peak in the powder X-ray diffraction pattern was The X-ray diffraction angle (two angles) is 38.611 degrees, and the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) and Z lead metal (4f) is 1 / 0.428. there were.
- a catalyst obtained by subjecting the catalyst intermediate obtained in Reference Example 2 to activation treatment only in the same manner as in Example 21 was analyzed by the above-mentioned method.
- the X-ray diffraction angle (2 ⁇ ⁇ ) of the maximum intensity peak in the powder X-ray diffraction pattern was 38.691 °, and the palladium metal (3d) Z lead metal (4 f ), The intensity ratio of the X-ray photoelectron spectrum was 10.763.
- 200 g of this catalyst was charged into a stirred tank reactor having the same capacity as the bubble column reactor of Example 1, and lead acetate was added to the reactor. 3 6 lead concentration in the feed solution was dissolved in earthenware pots by the 2 0 ppm to.
- the composition ratio of Pd / Pb supported was 3/1-27 in atomic ratio, and the X-ray diffraction angle (20%) of the maximum intensity peak in the powder X-ray diffraction pattern was obtained.
- the intensity ratio of the X-ray photoelectron spectrum of the (3d) lead metal (4f) was 1 Z 0.953.
- Example 11 The MMA production reaction of Example 11 was continued, and the reaction product was analyzed at 500 hours after the start of the reaction. While the conversion of methacrolein, the selectivity of MMA, and the selectivity of propylene were almost the same as those at 100 hours, the amount of methyl formate produced was 0.045 to 0.032. Mol / mol MMA.
- Example 21 The same operation and reaction as in Example 21 were carried out, except that acrolein was reacted with the catalyst of Example 14 in place of metacrolein.
- MA methyl acrylate
- aqueous silica sol As an aqueous silica sol, A1 / (Si + Al) were added to aluminum oxide nitrate magnesium nitrate in Snowtex N—30 (SiO 2 min: 30% by weight) manufactured by Nissan Chemical Co., Japan. after the percentage of) was dissolved was added to the power sale by the percentage of 1 0 mole 0/0, M g / ( S i + M g) is that Do 1 0 mole 0/0, the temperature of 1 3 0 ° C Spray-dried with the set spray dryer to obtain a spherical carrier with an average particle diameter of 60 ⁇ m.Bake in air at 300 ° C for 2 hours and then at 600 ° C for 3 hours.
- the carrier was palladium chloride and lead nitrate, and the carrier was adjusted to 100 parts by weight of palladium and 5.0 parts by weight of lead, and 2.3 parts by weight of palladium chloride as lead.
- 1 5 by weight 0 and Na Application Benefits ⁇ beam 1 0% by weight aqueous solution chloride, mixed with 1 3% by weight aqueous solution of lead nitrate, and stirred for 1 hour at room temperature, completely adsorb chloride Parajiu arm and lead nitrate on the carrier Sa It was.
- Catalyst intermediate A 1 2 0 3 -M g O) was obtained (hereinafter, the resulting catalyst Is referred to as "catalyst intermediate").
- the obtained catalyst intermediate was analyzed by the method described above.
- the composition ratio (atomic ratio) of PdZPb was 3Z0.70, and the X-ray of the maximum intensity peak in the powder X-ray diffraction pattern was obtained.
- the diffraction angle (20) is 39.102 degrees, and the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) / lead metal (4f) is 1 / 0.19. there were.
- the supported composition ratio (atomic ratio) of Pd / Pb was 3 / 1.07, the X-ray diffraction angle of the maximum intensity peak in the powder X-ray diffraction pattern.
- the NaOH aqueous solution was continuously supplied to the reactor at 0.06 liter Zh (the metachlorine concentration of the reaction system consisting of the above two solutions was about 36 wt./ 0), the reaction temperature 8 0 ° C, the reaction pressure 5 kg / cm 2 outlet oxygen concentration is 4.0 volume% (oxygen partial pressure 0. 2 0 kg / cm 2 equivalent) and air amount cormorants'll become Air was supplied to the reactor while adjusting, and the reaction was carried out for 10 hours.
- the NaOH concentration supplied to the reactor was controlled so that the pH of the reaction system was 7.1.
- the reaction product was continuously withdrawn from the reactor outlet by overflow.
- Palladium lead lead nitrate equivalent to 3 / 0.60 atomic ratio based on 2 kg of the catalyst intermediate of Reference Example 3 and palladium supported on the catalyst intermediate.
- the catalyst obtained by subjecting the catalyst intermediate of Reference Example 4 to the same activation procedure as in Example 26 under the activation conditions shown in Table 3 was analyzed by the method described above, and the MMA formation reaction was performed as in Example 26.
- Pillar * 2 Peak ratio of palladium metal (3d) / lead / gold shoulder (4f) in the X-ray photoelectron spectrum.
- the resulting catalyst had a Pd / Pb loading composition ratio of 31.27 in atomic ratio, and the X-ray diffraction angle (2S) of the maximum intensity peak in the powder X-ray diffraction pattern was 38.642 degrees.
- the intensity ratio of the palladium metal (3d) / lead metal (4f) X-ray photoelectron spectrum was 10.753.
- Example 3 5 Using 240 g of this catalyst, the reaction was carried out under exactly the same conditions as in Example 26 under the same reaction conditions, and the reaction product was analyzed. As a result, the conversion of methacrolein was 56.8%. Yes, MMA was formed at a selectivity of 912%, propylene as a by-product was formed at a selectivity of 1.43%, and methyl formate was formed at 0.138 mol / mol MMA. .
- Example 3 5 Example 3 5
- the catalyst intermediate before activation (P dsapb ⁇ ZS i O 2) was prepared in the same manner as in Reference Example 3 except that the amount of supported lead was 4.2 parts by weight. - give the A 1 2 03 -M g O) .
- the resulting catalyst intermediate had a Pd / Pb loading composition ratio (atomic ratio) of 3 / 1.29, and the X-ray diffraction angle (20) of the maximum intensity peak in the powder X-ray diffraction pattern was 38. At 913 degrees, the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) and Z lead metal (4f) was 0.18.
- the catalyst 2 used in Example 26 was connected to two externally circulating stainless steel bubble column reactors having a liquid phase of 1.2 liters in liquid phase and connected in series. 40 g was charged and an MMA generation reaction was performed. 36.7 weight of lead acetate dissolved in the first stage reactor so that the lead concentration in the reaction system becomes 20 ppm.
- the reaction was carried out by supplying air to the reactor while adjusting the amount of air so that The reaction product containing the catalyst withdrawn from the outlet of the first-stage reactor is withdrawn in an overflow manner, separated into a liquid and a solid, and the catalyst is returned to the first-stage reactor.
- the gas is passed through the second-stage reactor, while the second air is supplied with the insufficient air so that the oxygen concentration at the outlet of the second-stage reactor is 2.2% by volume (corresponding to an oxygen partial pressure of 0.1 lkgcm 2 ).
- the reaction was carried out at a reaction temperature of 80 ° C. and a reaction pressure of 4.6 kg / cm 2 .
- the NaOH concentration supplied to the reactors was controlled so that the PH of the reaction system was 7.1 in both the first and second reactors.
- the reaction product obtained in the second-stage reactor was continuously withdrawn from the outlet of the second-stage reactor by overflow. After 10 hours from the start of the reaction, the reaction product extracted from the second-stage reactor was analyzed, and the conversion of methacrylone was 85.9%, and the selectivity of MMA was high. 91.5%, propylene as a by-product was formed at a selectivity of 1.0%, and methyl formate was 0.046 mol / Mol had produced MMA.
- Example 26 Except that 200 g of the activated catalyst was charged into a stirred tank reactor having the same volume as the liquid phase part of the bubble column reactor of Example 6, and the lead concentration supplied to the reactor was 10 ppm. Was reacted for 10 hours under the same operating conditions as in Example 35.
- the reaction product was analyzed, the conversion of methacrolein was 62.1%, the selectivity of MMA was 91.4%, and the selectivity of propylene as a by-product was 11%. And methyl formate was produced at 0.044 mol / mol MMA. °
- Example 3 7 Example 3 7
- AF particle size: 10 to 150 m
- the obtained catalyst intermediate was subjected to the same activation treatment as in Example 26.
- the PdZPb atomic ratio of the obtained catalyst was 3Z1.24, and the X-ray diffraction angle (20) of the maximum intensity peak in the powder X-ray diffraction pattern was 38.611 degrees.
- the intensity ratio of the X-ray photoelectron spectrum of the metal (3d) Z lead metal (4f) was 1 / 0.51.
- Example 3 8 The reaction was carried out in the same apparatus and under the same operating conditions as in Example 36, and the reaction product was analyzed.
- the conversion of methacrolein was 61 and 3%, and the selectivity of MMA was 90%. .8%, propylene as a by-product was formed at a selectivity of 1.3%, and methyl formate was formed at 0.052 mol mol MMA.
- Example 3 8 The conversion of methacrolein was 61 and 3%, and the selectivity of MMA was 90%. .8%, propylene as a by-product was formed at a selectivity of 1.3%, and methyl formate was formed at 0.052 mol mol MMA.
- Example 3 8 The conversion of methacrolein was 61 and 3%, and the selectivity of MMA was 90%. .8%, propylene as a by-product was formed at a selectivity of 1.3%, and methyl formate was formed at 0.052 mol mol MMA.
- Example 37 Using the catalyst activated in the same manner as in Example 37, the reaction was carried out under the same operation and reaction conditions as in Example 36, except that the lactone was reacted instead of the methacrylate.
- the reaction product was analyzed, the conversion of acrolein was 57.8%, the selectivity for methyl acrylate (MA) was 92.1%, and the As a result, ethylene was produced at a selectivity of 1.1%, and methyl formate was produced at 0.039 mol / mol MA.
- Reference example 5 Scan and the aqueous Shi Li Ca sol node on Te click scan N-3 0 (Japan, Nissan Chemical Co., Ltd., S i O 2 minutes: 3 0 wt%) in the aluminum nitrate two ⁇ beam, magnesium nitrate Were added and dissolved such that the ratio of A 1 Z (S i + A l) was 10 mol% and the ratio of Mg / (S i + M g) was 10 mol%. Spray drying was performed with a spray dryer set to a temperature of 0 ° C to obtain a spherical support having an average particle size of 6.
- palladium chloride and lead nitrate are used as carriers, each with 100 parts by weight of palladium and lead.
- the carrier was mixed with an aqueous solution of 15% by weight of palladium chloride and 10% by weight of sodium chloride, and an aqueous solution of 13% by weight of lead nitrate so as to be 5 parts by weight and 4.2 parts by weight. The mixture was stirred at room temperature for 1 hour, and palladium chloride and lead nitrate were completely adsorbed on the carrier.
- the temperature was raised at a rate of 50 ° C / hour, and when it reached 300 ° C, it was held for 5 hours and further reduced.
- the catalyst intermediate was activated by cooling in a nitrogen stream.
- the supported composition ratio (atomic ratio) of PdZPb was 31.2.
- the X-ray diffraction angle (2 () of the maximum intensity peak in the powder X-ray diffraction pattern was 38.62.
- the intensity ratio of the X-ray photoelectron spectrum of palladium (3d) lead (4f) was 1Z 0.354.
- Example 39 Except that the oxidation treatment with oxygen gas was not performed, the same treatment as in Example 39 was carried out, and the loading composition ratio (atomic ratio) of Pd / Pb was 3 / 1.28, and the maximum in the powder X-ray diffraction pattern was Catalyst with an X-ray diffraction angle (20) of the intensity peak of 38.832 degrees and an intensity ratio of the X-ray photoelectron spectrum of palladium (3d) lead (4f) of 10.261 An intermediate was obtained.
- This catalyst intermediate (240 g) was reacted in exactly the same manner as in Example 39.
- the conversion of methacrolein was 59.1%
- the selectivity of MMA was 85.2%
- the by-products were As a result, propylene was produced at a selectivity of 5.7%
- methyl formate was produced at 0.132 mol Z mol MMA.
- Example 39 Activation was performed under the same conditions as in Example 39 except that the catalyst intermediate of Reference Example 5 was subjected to an oxidation treatment with oxygen gas and then a hydrogen reduction treatment, and was not subjected to a reduction treatment with methanol gas.
- the activated catalyst was analyzed, the PdZPb-supported composition ratio (atomic ratio) was 3 to 1.28, and the X-ray diffraction angle of the maximum intensity peak in the powder X-ray diffraction pattern (2 ⁇ ) is 38.66.55 degrees, The intensity ratio of palladium (3d) / lead (4f) X-ray photoelectron total was 1 / 0.378.
- Example 39 The same activation treatment as in Example 39 was performed on the catalyst intermediate of Reference Example 2.
- the resulting catalyst had a PdZPb-supported composition ratio of 3 / 0.98 in atomic ratio, and the X-ray diffraction angle (20) force of the maximum intensity peak in the powder X-ray diffraction pattern S38.697 degrees , And palladium
- the intensity ratio of the (3d) / lead (4f) X-ray photoelectron spectrum was 10.245.
- A12O3-MgO was obtained.
- the Pd / Pb loading composition ratio (atomic ratio) of the obtained catalyst intermediate was 3 / 1.95, and the X-ray diffraction angle (2 °) of the maximum intensity peak in the powder X-ray diffraction pattern was 38. At 745 degrees, the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) and lead metal (4f) was 1 / 1.24.
- This catalyst intermediate was subjected to the same activation treatment as in Example 39, and then 3 liters of an aqueous solution containing 300 g of the catalyst and 10% by weight of acetic acid.
- the reactor is charged to an autoclave having a liquid phase of 30 liters, and water containing 10% by weight of acetic acid is continuously supplied at 1 liter Zhr and stirred at 90 ° C for 10 hours.
- the PdZPb atomic ratio of the obtained catalyst was 31.25, and the X-ray diffraction angle (20) of the maximum intensity peak in the powder X-ray diffraction pattern was 38.611 degrees.
- the intensity ratio of the X-ray photoelectron spectrum of palladium (3d) Z-lead (4f) was 10.212.
- Example 4 4 to 4 7 Using this catalyst, an MMA formation reaction was carried out under exactly the same conditions as in Example 42, and the reaction product was analyzed 10 hours after the start of the reaction. 62.3%, MMA is 90.2% selectivity, propylene as a by-product is formed at 1.3% selectivity, and methyl formate is 0.049 mol / " Example 4 4 to 4 7
- Example 39 The same activation treatment as in Example 39 was performed for each of the catalyst intermediates shown in Table 4, and the reaction was carried out under exactly the same conditions as in Example 42.
- Table 4 shows the intensity ratio of X-ray photoelectron spectra of (20) and palladium metal (3d) lead metal (4f) together with the reaction results.
- Example 44 Pd 5 Pb 2 'B9 Mg 5 - ° / Si0 2 3 / 0.89 38.679 ° 1 / 0.23 62.4 89.4 2.12 0.044
- Example 45 3 / 1.12 38.656 ° 1 / 0.44 69.4 90.3 1.65 0.065
- Example 46 pd 5 ° P '06 TI ° ' VSi0 2 -Ai 2 0 3 * 2 3 / 1.25 38.633 ° 1 / 0.45 63.5 91.2 1.24 0.074 example 47 3 / 1.02 38.655 ° 1 / 0.34 64.3 90.7 1.87 0.061
- A1 Z Si 2 O 3 min .: 30 wt%, Siotex N-30 (Nissan Chemical Co., Ltd., Japan) was added to aluminum nitrate and magnesium nitrate, respectively. + after proportion of a 1) was added and dissolved in earthenware pots by the percentage of 1 0 mole 0/0, M g / ( S i + M g) becomes 1 0 mole 0/0, 1 3 0 ° C
- the carrier was spray-dried with a spray dryer set at a temperature of 3 ° C. to obtain a spherical carrier having an average particle size of 60 ⁇ .
- Catalyst intermediate the resulting catalyst.
- the composition ratio of PdZPb supported was 3Z2.98 in atomic ratio
- the X-ray diffraction angle of the maximum intensity peak in the powder X-ray diffraction pattern ( 2) was 38.865 °
- the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) / lead metal (4f) was 1 / 1.94.
- the intensity ratio of the X-ray photoelectron spectrum of (4f) was 1Z0.234.
- a catalyst separator was provided with 240 g of the activated catalyst, and the reaction was carried out in an externally circulating stainless steel bubble column reactor having a liquid phase of 1.2 liters.
- Lead acetate in the feed liquid in the reactor 3 lead concentration of dissolved in jar by the 5 0 ppm 6. 7% by weight of the main Taku Russia Rei N'nome data Roh Lumpur solution 0.5 4 liters Zh r, 2 ⁇ 4 weight 0 /.
- the activation treatment was performed in exactly the same manner as in Example 49 except that the catalyst intermediate of Reference Example 6 was activated with a 5% by weight aqueous hydrochloric acid solution.
- the Pd / Pb loading composition ratio (atomic ratio) was 3 / 0.74, and the X-ray diffraction angle of the maximum intensity peak in the powder X-ray diffraction pattern. (20) was 3.8743 degrees.
- palladium metal (3d) / lead-gold The intensity ratio of the X-ray photoelectron spectrum of the genus (4f) was 1 Z 0.185.
- Example 50 to 54 the catalyst intermediate of Reference Example 7 was activated in the same manner as in Example 49 except that various fatty acids shown in Table 5 were used instead of acetic acid of Example 49.
- the MMA formation reaction was performed in the same manner as in Example 49.
- Table 5 shows the intensity ratio of the X-ray photoelectron spectrum of (4f) together with the reaction results.
- Example 49 The same activation operation as in Example 49 was performed except that the activation treatment time was set to 30 hours.
- the resulting catalyst had a PdZPb-supported composition ratio (atomic ratio) of 3 / 0.95, and the X-ray diffraction angle (2 °) of the maximum intensity peak in the powder X-ray diffraction pattern was 38.6. 82 degrees.
- the intensity ratio of the X-ray photoelectron spectrum of palladium (3d) lead (4f) was 0.183.
- the Pd / Pb carrying composition ratio (atomic ratio) was 3Z1.09, and the powder X-ray diffraction pattern
- the X-ray diffraction angle (2 °) of the maximum intensity peak was 38.634 degrees.
- the intensity ratio of the X-ray photoelectron spectrum of palladium (3d) lead (4f) was 1Z0.597.
- the MMA generation reaction was performed while adjusting the air volume so that the volume became 0% by volume (equivalent to an oxygen partial pressure of 0.20 kg / cm 2 ).
- the NaOH concentration supplied to the reactor was controlled so that the PH of the reaction system was 7.1.
- the reaction product was continuously withdrawn from the reactor outlet by overflow.
- the conversion of methacrolein was 60.8%
- the selectivity of MMA was 91.2%
- Pyrene was produced at a selectivity of 1.4%
- methyl formate was produced at 0.062 molmol 1 ⁇ ] ⁇ . Comparative Example 1 4
- the reaction pressure in the reactor was 8.3 kg / cm 2
- the outlet oxygen concentration was 6.0 volumes.
- / 0 equivalent to an oxygen partial pressure of 0.5 kg / cm 2
- the air was supplied to the reactor while adjusting the amount of air so that the activation process of Example 1 was performed. went.
- the Pd / Pb carrying composition ratio (atomic ratio) was 31.03
- the X-ray diffraction angle of the maximum intensity peak in the powder X-ray diffraction pattern (2 0) was 38.7339 degrees.
- X-ray photoelectron spectra of palladium metal (3d) and Z lead metal (4f) The intensity ratio was 10.45.
- the lkg of the catalyst intermediate of Reference Example 2 and the PdZPb-supporting composition ratio (atomic ratio) of the catalyst intermediate were set to 3 to 1.3.
- 20.9 g of lead acetate corresponding to the shortage of lead in methanol was added to a methanol solution of 5 ⁇ in 5 ⁇ , and the reaction was performed at a reaction temperature of 90 e C and a reaction pressure of S kg Z cm 2.
- the composition ratio of Pd / Pb supported was 3Z1.27 in atomic ratio, and the X-ray diffraction angle (2 0) was 38.691 degrees.
- the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) and lead metal (4f) was 1 / 0.763.
- Example 57 Stirring having the same volume as the liquid phase part of the bubble column reactor of 7 A tank-type reactor was charged with 200 g of the catalyst after the activation step, and 36.7% by weight of a metachlorin-containing methanol solution was added to the reactor with 0.54 liter Z hr 2. to 4 wt% of N a OH / / meta Nord solution 0.0 6 l Z hr continuously supplied (main Tak port lay down concentrations above SL two solutions by Li made reaction system in about 3 3 wt%), the reaction temperature 8 0 t, at a reaction pressure 5 kg Z cm 2, by exit oxygen concentration becomes 4.0 vol% (the oxygen partial pressure 0.
- the catalyst intermediate (PdSQpi ⁇ ZSioO2) was prepared in the same manner as in Reference Example 1 except that the amount of supported lead was changed to 4.2 parts by weight.
- A12O3MgO was obtained.
- the PdZPb supported composition ratio (atomic ratio) of the obtained catalyst intermediate was 31.29, and the X-ray diffraction angle (20) of the maximum intensity peak in the powder X-ray diffraction pattern was 38. At 913 degrees, the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) and Z lead metal (4f) was 1 / 1.187.
- a methanol solution of acetic acid obtained by dissolving 2.5 kg of acetic acid in 25 kg of methanol was charged into a 30 liter autoclave and stirred at 90 ° C for 1 hour. Analysis of the aqueous solution revealed that 720 ppm of lead ions had been dissolved.
- An external circulation stainless steel bubble column reactor having a catalyst separator of the same type as that used in Example 57 and having a liquid phase of 1.2 liters was connected in series with two reactors. 240 g of the catalyst after the activation treatment was charged, and the reaction was carried out as follows. First stage reactor, the 3 6. 7 weight 0/0 main Taku b lay down / meta Nord solution lead concentration was dissolved in earthenware pots by the 2 0 ppm of lead acetate feed solution 0.54 liter Zhr, 2-4% by weight 1 ⁇ 301 / methanol solution is continuously supplied at 0.06 liter / hr (measurement of the reaction system of the first stage reactor).
- the reactor is adjusted in air volume so that the outlet oxygen concentration is 4.0% by volume (equivalent to an oxygen partial pressure of 0.20 kg cm 2 ).
- the reaction was performed by supplying air to the reactor.
- the reaction product containing the catalyst removed from the first-stage reactor by overflow is separated into liquid and solid and the catalyst is returned to the first-stage reactor, and the obtained reaction product is transferred to the second-stage reactor.
- NaOH / methanol solution was sent with 0.06 liters / hr, while the first stage reaction effluent gas was vented to the second stage reactor while the second stage 2 outlet oxygen concentration stage reactor.
- the reaction temperature is 90 ° C
- the reaction pressure is S kg Z cm 2
- the outlet oxygen concentration is 2.0% by volume (equivalent to oxygen partial pressure of 0.10 kg / cm 2 ).
- Air was supplied to the reactor while adjusting the amount of air.
- the activation treatment was completed in 50 hours, and the catalyst was analyzed.
- the Pd / Pb carrying composition ratio was 31.1, and the X-ray of the maximum intensity peak in the powder X-ray diffraction pattern was found.
- the diffraction angle (20) was 38.632 degrees.
- the intensity ratio of the X-ray photoelectron spelling of palladium metal (3d) / lead metal (4f) was 1 / 0.614.
- the activated catalyst was subjected to an MMA formation reaction under exactly the same conditions as in Example 57, and the reaction product was analyzed 10 hours after the start of the reaction.
- the conversion was 59.8%, the selectivity of MMA was 90.9%, the by-product propylene was formed at a selectivity of 1.4%, and the methyl formate was 0.05%. 3 mol mol MMA was produced.
- the activation treatment was changed as shown in Table 6 and the catalyst in Reference Example 1 was used. The same operation as in Example 60 was performed except that the interstitial activation treatment was performed.
- Example 3 In the same manner as in Example 3 6, to yield a catalyst intermediate (P d 5 '° P b 3' 36 T 1 ° ⁇ 1 J S i 0 2). Using this catalyst intermediate, the same activation treatment as in Example 58 was performed except that the outlet oxygen concentration was 3.0% by volume (oxygen partial pressure 0.15 kg Zcm 2 ).
- the Pd / Pb loading composition ratio (atomic ratio) of the obtained catalyst was 3: 1.20, and the X-ray diffraction angle (2 ⁇ ) of the maximum intensity peak in the powder X-ray diffraction pattern was 38.668. At 2 degrees, the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) / lead metal (4f) is 1.0%.
- Example 57 200 g of the activated catalyst was charged into a stirred tank reactor having the same volume as the liquid phase part of the bubble column reactor of Example 7, and the lead concentration of the reaction system was adjusted to 100 ppm. The reaction was carried out for 10 hours under the same operating conditions as in Example 57 except that the lead acetate was dissolved in the methanol solution of methanol. When the reaction product was analyzed, the conversion of methacrolein was 62.1%, the selectivity was 90.4% for MMA and 1% for propylene as a by-product. .
- Example 64 The same activation treatment as in Example 64 was performed on the same catalyst intermediate prepared in Example 37.
- the resulting catalyst is described above.
- the composition ratio (atomic ratio) supporting PdZPb was 3 / 1.24
- the X-ray diffraction angle (20) of the maximum intensity peak in the powder X-ray diffraction pattern was 3 At 8.67 degrees
- the X-ray photoelectron spectrum intensity ratio of palladium metal (3d) / lead metal (4f) was 1 / 0.595.
- Example 6 The reaction was carried out under the same operating conditions as in Example 64, and the reaction product was analyzed.
- the conversion of methacrolein was 60.4% and the selectivity of MMA was 90.5%.
- propylene was formed in a selectivity of 1.96% and methyl formate 0.075 mol mol 1 ⁇ ] ⁇ .
- Example 64 The reaction was carried out under the same operation and under the same reaction conditions as in Example 64 except that the activated catalyst of Example 62 was used to react the lactone layer instead of metachlorine.
- the reaction product was analyzed, the conversion of acrolein was 59.3% and the selectivity for methyl acrylate (MA) was 90.1%. The selectivity was 1.83% for len and 0.086 mol mol of MA for methyl formate. 5 7
- Example 60 The same activation operation as in Example 60 was performed except that air was not supplied to the reactor, and the PdZPb loading composition ratio was 3128 in atomic ratio, and the maximum intensity peak in the powder X-ray diffraction pattern was obtained.
- X-ray diffraction angle (20) of 38.675 °
- an intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) / lead metal (4f) is 1 Z 0.914.
- silica sol 10 kg of Snowtex N—30 (SiO 2 content: 30% by weight) manufactured by Nissan Chemical Co., Ltd. of Japan was placed in a 40 liter stainless steel container. The mixture was stirred. To this, 2.05 kg of aluminum nitrate nonahydrate was added little by little to dissolve. After complete dissolution, it was spray-dried with a spray dryer set to a temperature of 130 ° C to obtain a solid. Next, the obtained solid was spread in a stainless steel container having an open top with a thickness of about 1 cm, heated in an electric furnace from room temperature to 300 ° C over 2 hours, and held for 3 hours. . The temperature was further raised to 600 ° C over 2 hours, and then held for 3 hours.
- the carrier was gradually cooled to obtain a carrier.
- the molar ratio of A 1 / (A 1 + S i) was 10%.
- a carrier having a specific surface area of 188 m 2 Z g was obtained in the same manner as in Reference Example 8, except that aluminum nitrate was not added.
- the accelerated evaluation of the water resistance of the carrier by the method described above revealed that the concentration of eluted Si ions was 210 ppm. Comparative Reference Example 2
- silica gel (Fuji Silicon Co., Ltd., Carrierat 10) was calcined at 600 ° C. for 3 hours.
- the specific surface area of the obtained silica measured by a nitrogen adsorption method was 300 m 2 g.
- the dissolved Si ion concentration was 244 ppm.
- Reference Example 9 Except that aluminum included in the carrier, the aluminum nitrate Yu arm addition to earthenware pots by the 5 mole 0/0 of the total molar amount of shea Li co down and aluminum, and the sintering temperature was set to 7 5 0 ° C In the same manner as in Reference Example 8, a carrier having a specific surface area of 53 m 2 Z g was obtained. The accelerated evaluation of the water resistance of the carrier by the above method revealed that the eluted Si ion concentration was 90 ppm.
- Ni aluminum and Na door Li Umm is, Let 's made each 3 0 mole 0/0 and 1 molar 0 / o with respect to the total molar amount of Shi Li co-down and the aluminum and Na door Li ⁇ beam, aluminum nitrate A carrier having a specific surface area of 98 m 2 / g was obtained in the same manner as in Reference Example 8, except that sodium and sodium acetate were added. The accelerated evaluation of the water resistance of the carrier by the above-mentioned method revealed that the eluted Si ion concentration was 43 Ppm.
- a commercially available silica-alumina compound [Nikki Chemical Co., Japan: N631HN, molar ratio of A1 / (A1 + Si) 30%] was transferred to a stainless steel container with the top open. spread in a thickness of about 1 cm, electricity in a gas furnace, and held 3 0 0 e C over 2 hours heating after 3 hours at room temperature. The temperature was further raised to 800 ° C. over 2 hours, maintained for 3 hours, and then cooled to obtain a carrier. The specific surface area of the obtained carrier determined by a nitrogen adsorption method was 348 m 2 / g. The accelerated evaluation of the water resistance by the method described above revealed that the concentration of the dissolved S ion was 87 ppm.
- Reference Example 8- Table 4 shows the molar ratio of A 1 Z (A 1 + S i), specific surface area, and eluted S i ion concentration, together with the carrier material and the calcination temperature, for L 4 and Comparative Reference Examples 1 and 2. .
- Example 2 0 - MMA production reaction of (S i O 2 A 1 are use of 2 0 3 M g O carrier-based catalyst) was performed 1 0 0 0 hours.
- the reaction mixtures having a reaction time of 500 hours and 1000 hours were measured by ICP, the reaction mixtures extracted from the reactor outlets of the first and second stages were in each case measured. Pd was not detected (that is, the Pd concentration was below the detection limit), and the concentrations of S i and A 1 were all below 1 ppm.
- the catalyst was extracted from the first and second stage reactors, respectively, and examined with an electron microscope (SEM). As a result, almost no cracks or chips were found in the catalyst. . Comparative Example 15
- This catalyst intermediate was subjected to the same activation treatment as in Example 26.
- the Pd / Pb loading composition (atomic ratio) of the obtained catalyst was 3Z1.20, and the powder X-ray diffraction pattern showed The X-ray diffraction angle (20) of the maximum intensity peak is 38.626 °, and the X-ray photoelectron spectrum intensity ratio of palladium metal (3d) and lead metal (4f) is 1 Z0.46.
- an MMA production reaction was carried out under the same conditions as in Example 42. After 1,000 hours, the conversion of methacrolein was 61.5%, the selectivity of MMA was 90.9%, the selectivity of propylene was 1.16, and the methyl formate was 0.045 mol MMA. When the reaction mixture was measured by ICP, no Pd ion was detected (that is, the Pd concentration was below the detection limit).
- the resulting carrier is silicon, against the total moles of aluminum and magnesium, Shi Li co down, 8 aluminum and magnesium, respectively 3.3 mol%, 8. 4 mol%, 8. 3 mol 0 /. Included.
- the specific surface area by the nitrogen adsorption method was 148 m 2 / g, the average particle size was about 60 ⁇ m from microscopic observation, it was almost spherical, and the crushing property was examined using a mortar. It was hard.
- Reference Example 1 7 Ni Let 's magnesium and aluminum contained in the carrier is respectively 5.6 mole 0/0 and 2 2.3 mole 0/0 of the total moles of silicon co down, magnesium and Aluminum nitrate Magne Shiumu Then, a carrier having a specific surface area of 13.8 m 2 Zg was obtained in the same manner as in Reference Example 15 except that aluminum nitrate was added to the silica sol and the firing temperature was 800 ° C. The accelerated evaluation of the water resistance of the carrier by the method described above revealed that the eluted Si ion concentration was 4 O ppm. Reference Example 1 8
- Silicon contained in the carrier, the total moles of magnesium and aluminum, respectively magnesium is 3 8.1 mole 0/0, Ni Let 's aluminum is 1 5 mole 0/0, magnesium nitrate nitrate aluminum
- a carrier having a specific surface area of 134 mg was obtained in the same manner as in Reference Example 15 except that the firing temperature was set at 65 ° C.
- the accelerated evaluation of the water resistance of the carrier by the method described above revealed that the eluted Si ion concentration was 43 ppm.
- Table 8 shows the composition, specific surface area, sintering temperature, and elution S ion concentration of the carrier obtained in Reference Examples 15 to 21.
- Carrier material Firing temperature Silicon Aluminum Magnesium Specific surface area Accelerated water resistance evaluation:
- the resulting product is filtered, washed with water, dried for 5 hours at 1 2 0 e C, to remove organic matter was calcined for 5 hours in air at 5 0 0 ° C, after which the product 1
- the mixture was subjected to ion exchange in N nitric acid for 8 hours, filtered, washed with water, and dried at 120 ° C for 6 hours to obtain a proton-type crystalline aluminosilicate.
- the obtained product was identified as Zeolite ZSM-5 as a result of X-ray diffraction analysis.
- the composition expressed in the form of the oxide of this anhydride was determined by K-ray X-ray analysis and measurement of the amount of acid obtained by the pyridin adsorption method.
- Solution A was mixed with Solutions B, C, and D while stirring vigorously, and stirring was continued for 1 hour to obtain a gel.
- the obtained gel was crystallized by heating at 150 ° C. for 40 hours while stirring at a stirring peripheral speed of 2 m / sec.
- the obtained product was filtered, washed with water, dried at 120 ° C for 5 hours, and calcined in air at 500 ° C for 5 hours to remove organic substances. Then, the product is ion-exchanged in 1 N nitric acid for 8 hours, filtered, washed with water, dried at 120 ° C for 6 hours, and treated with a boron-type crystalline aluminoporous. Got a silicate.
- the resulting product was identified as a Zeolite ZSM-5 analog by X-ray diffraction analysis. Further, from the amount of acid determined by K-ray X-ray analysis and pyridyl adsorption, the composition of this anhydride in the form of an oxide was as follows.
- ZSM 11 Zeolite ion-exchanged into a rib mouth type by the method described in US Pat. No. 3,709,779.
- Example 11 The same catalyst as obtained in Example 11 [Pd / Pb supported composition (atomic ratio): 3Zl.08, X-ray diffraction angle of maximum intensity peak in powder X-ray diffraction pattern (20% ): 38.6 12 degrees, using the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) Z lead metal (4f): 10.0.49] A continuous reaction was carried out for 1,00 hours by the same operation as in Example 11 except that lead acetate was supplied so that the concentration became 20 ppm. The analysis results of the reaction mixture at reaction time of 200 hours and 1000 hours were compared. When compared, almost no difference was observed between the analysis results at 2000 hours and at 1000 hours.
- Example 71 A continuous reaction was carried out in the same manner as in Example 71 except that no lead acetate was supplied in Example 71. Analysis of the reaction mixture at a reaction time of 2000 hours and a reaction time of 1000 hours showed that at 200 hours, the conversion of methacrolein was 60.3% and the selectivity of MMA was 88.6%. As a by-product, selectivity was 3.15% for propylene and 0.038 mol / mol MMA of methyl formate was produced. 1,
- the concentrations of 1 and A 1 were all less than 1 Ppm. Also, 1, After the reaction for 00 hours, the catalyst was extracted and examined by SEM. As a result, no change was found in the catalyst.
- Example 11 Same as Example 11 except that the catalyst intermediate obtained in Reference Example 1 was used and the lead concentration in the reaction system was changed to 10 ppm as a control condition of the catalyst surface structure after 50 hours. Operated. When a total of 100 hours had passed since the start of the activation treatment, the catalyst was withdrawn from the reactor and analyzed by the above-mentioned method. As a result, the composition ratio (atomic ratio) of PdPb supported was 31.02. The X-ray diffraction angle (2 ⁇ ) of the maximum intensity peak in the powder X-ray diffraction pattern is 38.609 degrees, and the intensity of the X-ray photoelectron spectrum of palladium metal (3d) and lead metal (4f). The ratio was 0.32.
- the obtained catalyst (240 g) was equipped with a catalyst separator, and the liquid phase was charged to a 1.2 liter external circulation stainless steel bubble column reactor to carry out a reaction. 0.56 liters of a 36.7% by weight solution of methacrolein Z methanol in which lead acetate was added so that the lead concentration in the reaction system was 2 O ppm was obtained.
- the carrier used in Reference Example 29 was charged with 100 parts by weight of palladium chloride and lead nitrate, respectively, so that the amount of palladium and lead was 5.0 parts by weight and 4.2 parts by weight, respectively.
- the carrier is mixed with an aqueous solution of 15% by weight of palladium chloride and 10% by weight of sodium chloride, and an aqueous solution of 13% by weight of lead nitrate, and stirred at room temperature for 1 hour to completely remove the palladium chloride and lead nitrate from the carrier. Was adsorbed.
- a catalyst was prepared from the precursor.
- the Pd / Pb loading composition ratio (atomic ratio) was 3Z1.92
- the X-ray diffraction angle of the maximum intensity peak in the powder X-ray diffraction pattern ( 2) was 38.623 degrees
- the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) and lead metal (4 layers) was 1 / 1.23.
- Example 79 Using the obtained catalyst, the same procedures as in Example 79 were carried out.
- the MA formation reaction was performed and the obtained reaction product was analyzed, the conversion of methacrolein was 57.8%, the selectivity was 87.3%, and the selectivity was 87.3%.
- propylene was produced at a selectivity of 1.9%, and methyl formate was produced at 0.213 mol / mol MMA. Comparative Example 20
- a catalyst was prepared from the catalyst precursor of Reference Example 29 in exactly the same manner as in Example 79 except for the absence. When the obtained catalyst was analyzed by the above method, the composition ratio (atomic ratio) of PdZPb supported was 31.5.58, and the X-ray diffraction angle (2 ⁇ ) was 3870 ° C., and the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) / lead metal (4f) was 1 / 0.75.
- Example 8 an MMA formation reaction was carried out in the same manner as in Example 79, and the obtained reaction product was analyzed.
- the conversion of methacrolein was 57.8. %
- MMA selectivity is 85.3%
- propylene is formed as a by-product with a selectivity of 5.1%
- methyl formate is 0.129 mole mol] ⁇ ] ⁇ Was generated.
- the composition ratio (atomic ratio) of PdZPb supported was 31.18
- the X-ray diffraction angle of the maximum intensity peak in the powder X-ray diffraction pattern ( (20) was 38.697 degrees
- the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) / lead metal (4f) was 1 / 0.72. .
- the mixture was impregnated with a force beam while stirring on a boiling water bath, dried to dryness, and fired at 500 ° C. for 3 hours.
- 83 g of palladium chloride and 28 g of NaCl were added to water to make a 500 ml aqueous solution, and 34 g of lead nitrate dissolved in water were mixed.
- the catalyst obtained by reducing the catalyst precursor obtained in Reference Example 30 under the reducing conditions shown in Table 10 was analyzed by the method described above.
- PdZPb loading composition ratio (atomic ratio), X-ray diffraction angle of maximum intensity peak (2 2) in powder X-ray diffraction pattern, X-ray photoelectron of palladium metal (3d) / lead metal (4f)
- Table 10 summarizes the spectral intensity ratios and the reaction results of the MMA formation reaction.
- the MMA formation reaction was performed using the same apparatus and reaction conditions as in Example 79. Table 10 Performing Activation Conditions Activated M Medium ”In.
- the Pd / Pb carrying composition ratio (atomic ratio) of the obtained catalyst was 3Z1.27, and the X-ray diffraction angle (20) of the maximum intensity peak in the powder X-ray diffraction pattern was 38.6. At 10 degrees, the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) Z lead metal (4f) was 1Z0.39.
- Example 79 The above reduction treatment was carried out in a reactor equipped with the catalyst separator used in Example 9 and having two externally circulating stainless steel bubble column reactors having a liquid phase of 1.2 liters connected in series.
- the finished catalyst (240 g) was charged to carry out an MMA generation reaction.
- First stage reactor the lead concentration in the reaction system vinegar lead was added to the power sale by the 2 0 ppm 3 6. 7 weight 0 /. 0 meta click b lay down / METHANOL solution. 5 4 l Z hr,.
- the effluent gas from the first stage reactor was sent to the second stage reactor, while the oxygen at the outlet of the second stage reactor was The concentration is 2.2 volumes. / 0 (oxygen partial pressure 0. llkg Z cm 2 equivalent) and power sale to shortage amount of the air by comprising adding to the second stage reactor the reaction temperature 8 0 ° C, reaction pressure 4. 6 kg / cm 2
- the MMA formation reaction was performed.
- the NaOH concentration supplied to the first and second reactors was controlled so that the PH of the reaction system became 7.1.
- the reaction product obtained in the second-stage reactor was continuously extracted from the second-stage reactor outlet by overflow.
- Example 8 7 In the same manner as in Example 36, 100 parts by weight of a silica gel (Carrier 10) manufactured by Fuji Silicon Co., Ltd., Japan, [Pd
- Example 79 The same as Example 79 except that 200 g of the obtained catalyst was used in a stirred tank reactor having a liquid phase part of the same volume as in Example 79, and the lead concentration of the reaction system was set to 10 ppm.
- the MMA formation reaction was performed under the following reaction conditions. When the reaction products were analyzed, the metachlorine conversion rate was 62.4% and the MMA selectivity was 91.2%, and propylene was selected as a by-product. It was produced at a rate of 1.2%, and methyl formate was produced at 0.042 mol Z mol MMA.
- P b 2 ⁇ 7 B i ° ⁇ 23 M g 2 - 0 / A 1 had a 2 0 3 composition.
- the PdZPb atomic ratio was 3 to 1.24
- the X-ray diffraction angle (20) of the maximum intensity peak in the powder X-ray diffraction pattern was 38.
- the intensity ratio of the X-ray photoelectron spectrum of silver and palladium metal (3d) / lead metal (4f) was 10.52.
- Example 88 Same as Example 88 except that the catalyst obtained in Example 86 was used and acrolein was reacted in place of the methanol mouth lane.
- the methyl acrylate (MA) formation reaction was performed under the same operation and reaction conditions, and the reaction product was analyzed. The reaction rate was 58.4%, and the MA selectivity was 92. At 4%, ethylene was produced as a by-product at a selectivity of 1.0%, and methyl formate was produced at 0.042 mol / mol MA.
- MA methyl acrylate
- the catalyst intermediate in Reference Example 5 was activated in the same manner as in Example 39, except that the methanol gas was replaced with isobutene gas, and the temperature was set at 300 ° C.
- the Pd / Pb loading composition ratio (atomic ratio) was 31.28, and the X-ray diffraction angle (20) of the maximum intensity peak in the powder X-ray diffraction pattern was 3
- Example 9 1 The activation treatment of the catalyst intermediate was performed in the same manner as in Example 43 except that the temperature was changed to 300 ° C. instead of methanol gas and isobutene gas.
- the PdZPb atomic ratio of the obtained catalyst was 3 to 131, and the X-ray diffraction angle (20) of the maximum intensity peak in the powder X-ray diffraction pattern was 38.623 degrees. Further, the intensity ratio of the X-ray photoelectron spectrum of palladium metal (3d) and lead metal (4f) was 10.0.38.
- the MMA formation reaction was carried out in the same manner as in Example 42, and the reaction product after 10 hours was analyzed.
- the conversion of methacrolein was 618%, and the selectivity of MMA was 90%.
- 1%, propylene as a by-product was produced at a selectivity of 1.1%, and methyl formate was produced at 0.051 mol / mol MMA.
- Example 9 2
- a catalyst intermediate supporting 5.0 parts by weight of palladium was obtained in the same manner as in Reference Example 2 except that lead nitrate was not added.
- activation treatment was performed in the same manner as in Example 7, except that 90.5 g of lead acetate trihydrate was used and the activation treatment time was set to 100 hours.
- the obtained catalyst was analyzed by the above-described method.
- the atomic ratio of PdZPb was 3Z0.96, and the X-ray diffraction angle (20) of the maximum intensity peak in the powder X-ray diffraction pattern was 38. 6 8 8 degrees.
- Example 92 The palladium obtained in Example 92 was prepared in the same manner as in Example 1 except that lead acetate was added to the reaction system so that the lead became 200 ppm, and the activation treatment was performed for 200 hours.
- the catalyst intermediate supporting 0 parts by weight was activated.
- the atomic ratio of PdZPb was 30.94
- the X-ray diffraction angle (2 °) of the maximum intensity peak in the powder X-ray diffraction pattern was 38.6. 93 degrees.
- the MMA formation reaction was carried out in the same manner as in Example 7, and after 10 hours, the reaction product was analyzed.
- the conversion of methacrolein was 57.8%, and the selectivity of MMA was 89%.
- palladium and lead are not supported on a carrier with a Pd / Pb atomic ratio (S) of 3 Z 0.7 ⁇ S ⁇ 3 / 1.3.
- S Pd / Pb atomic ratio
- palladium-lead A catalyst exhibiting the maximum intensity peak attributed to the diffraction of the (111) plane of the intermetallic compound in the range of the X-ray diffraction angle (2 ⁇ ) 38.55 to 38.70 degrees has a mechanical strength
- the desired carboxylic acid ester can be produced with high selectivity and with few by-products.
- the catalyst of the present invention can be effectively stabilized at the same time in a continuous process for producing a carboxylic acid ester using the catalyst, and can maintain the long-term catalyst life while maintaining the desired carboxylic acid ester. Acid esters can be produced stably in high yield for a long period of time, and their industrial value is extremely high.
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Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
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EP96924148A EP0857512B1 (en) | 1995-07-18 | 1996-07-18 | catalyst for the preparation of carboxylic esters |
AT96924148T ATE269755T1 (de) | 1995-07-18 | 1996-07-18 | Katalysator zur herstellung von carbonsäureestern |
US10/101,252 USRE38283E1 (en) | 1995-07-18 | 1996-07-18 | Catalyst for use in producing carboxylic esters |
DE69632788T DE69632788T2 (de) | 1995-07-18 | 1996-07-18 | Katalysator zur herstellung von carbonsäureestern |
US08/945,308 US6040472A (en) | 1995-07-18 | 1996-07-18 | Catalyst for use in producing carboxylic esters |
HK98110335A HK1009412A1 (en) | 1995-07-18 | 1998-09-01 | Catalyst for the preparation of carboxylic esters. |
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JP18154795A JP3503776B2 (ja) | 1995-07-18 | 1995-07-18 | カルボン酸エステル製造用パラジウム、鉛含有担持触媒 |
JP7/181547 | 1995-07-18 | ||
JP18272195A JP3503777B2 (ja) | 1995-07-19 | 1995-07-19 | パラジウム及び鉛を含む表面制御担持触媒 |
JP7/182721 | 1995-07-19 |
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PCT/JP1996/002008 WO1997003751A1 (fr) | 1995-07-18 | 1996-07-18 | Catalyseur conçu pour la preparation d'esters carboxyliques |
Country Status (10)
Country | Link |
---|---|
US (2) | US6040472A (ja) |
EP (2) | EP0857512B1 (ja) |
KR (1) | KR100259743B1 (ja) |
CN (1) | CN1086313C (ja) |
AT (2) | ATE280750T1 (ja) |
DE (2) | DE69633753T2 (ja) |
HK (1) | HK1009412A1 (ja) |
MY (1) | MY119415A (ja) |
TW (1) | TW348073B (ja) |
WO (1) | WO1997003751A1 (ja) |
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US5906142A (en) * | 1997-09-11 | 1999-05-25 | Harmonic Drive Systems, Inc. | Wave gear drive |
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JPS5524106A (en) * | 1978-08-09 | 1980-02-21 | Asahi Chem Ind Co Ltd | Preparation of methyl methacrylate |
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-
1996
- 1996-07-18 EP EP96924148A patent/EP0857512B1/en not_active Expired - Lifetime
- 1996-07-18 DE DE69633753T patent/DE69633753T2/de not_active Expired - Lifetime
- 1996-07-18 EP EP20030077037 patent/EP1361206B1/en not_active Expired - Lifetime
- 1996-07-18 WO PCT/JP1996/002008 patent/WO1997003751A1/ja active IP Right Grant
- 1996-07-18 US US08/945,308 patent/US6040472A/en not_active Ceased
- 1996-07-18 TW TW085108875A patent/TW348073B/zh not_active IP Right Cessation
- 1996-07-18 MY MYPI96002963A patent/MY119415A/en unknown
- 1996-07-18 AT AT03077037T patent/ATE280750T1/de not_active IP Right Cessation
- 1996-07-18 AT AT96924148T patent/ATE269755T1/de not_active IP Right Cessation
- 1996-07-18 CN CN96193950A patent/CN1086313C/zh not_active Expired - Lifetime
- 1996-07-18 US US10/101,252 patent/USRE38283E1/en not_active Expired - Lifetime
- 1996-07-18 DE DE69632788T patent/DE69632788T2/de not_active Expired - Lifetime
- 1996-07-18 KR KR1019970708219A patent/KR100259743B1/ko not_active IP Right Cessation
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1998
- 1998-09-01 HK HK98110335A patent/HK1009412A1/xx not_active IP Right Cessation
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JPS5524106A (en) * | 1978-08-09 | 1980-02-21 | Asahi Chem Ind Co Ltd | Preparation of methyl methacrylate |
JPS56150043A (en) * | 1980-04-22 | 1981-11-20 | Asahi Chem Ind Co Ltd | Preparation of unsaturated carboxylic acid ester |
JPS59162947A (ja) * | 1983-02-26 | 1984-09-13 | バスフ アクチエンゲゼルシヤフト | メタクリル酸メチル製造用触媒 |
JPH05148184A (ja) * | 1991-11-28 | 1993-06-15 | Mitsui Toatsu Chem Inc | カルボン酸エステルの製造法 |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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US5906142A (en) * | 1997-09-11 | 1999-05-25 | Harmonic Drive Systems, Inc. | Wave gear drive |
Also Published As
Publication number | Publication date |
---|---|
TW348073B (en) | 1998-12-21 |
ATE280750T1 (de) | 2004-11-15 |
EP1361206A1 (en) | 2003-11-12 |
USRE38283E1 (en) | 2003-10-21 |
MY119415A (en) | 2005-05-31 |
US6040472A (en) | 2000-03-21 |
DE69633753D1 (de) | 2004-12-02 |
KR100259743B1 (ko) | 2000-07-01 |
DE69632788D1 (de) | 2004-07-29 |
CN1086313C (zh) | 2002-06-19 |
HK1009412A1 (en) | 1999-09-10 |
EP1361206B1 (en) | 2004-10-27 |
DE69632788T2 (de) | 2005-07-14 |
CN1184439A (zh) | 1998-06-10 |
DE69633753T2 (de) | 2005-12-22 |
ATE269755T1 (de) | 2004-07-15 |
EP0857512A4 (en) | 2000-01-05 |
EP0857512B1 (en) | 2004-06-23 |
KR19990014874A (ko) | 1999-02-25 |
EP0857512A1 (en) | 1998-08-12 |
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