WO2021214954A1 - 均一型白金担持アルミナ触媒、その製造方法、及びその使用方法 - Google Patents
均一型白金担持アルミナ触媒、その製造方法、及びその使用方法 Download PDFInfo
- Publication number
- WO2021214954A1 WO2021214954A1 PCT/JP2020/017563 JP2020017563W WO2021214954A1 WO 2021214954 A1 WO2021214954 A1 WO 2021214954A1 JP 2020017563 W JP2020017563 W JP 2020017563W WO 2021214954 A1 WO2021214954 A1 WO 2021214954A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- platinum
- catalyst
- supported
- supported alumina
- sulfur
- Prior art date
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 307
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title claims abstract description 198
- 238000000034 method Methods 0.000 title claims description 71
- 238000004519 manufacturing process Methods 0.000 title claims description 18
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims abstract description 119
- 229910052697 platinum Inorganic materials 0.000 claims abstract description 54
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 51
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 51
- 239000011593 sulfur Substances 0.000 claims abstract description 51
- 239000011734 sodium Substances 0.000 claims abstract description 31
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims abstract description 27
- 229910052783 alkali metal Inorganic materials 0.000 claims abstract description 27
- 150000001340 alkali metals Chemical class 0.000 claims abstract description 27
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 27
- 150000003464 sulfur compounds Chemical class 0.000 claims abstract description 17
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910052700 potassium Inorganic materials 0.000 claims abstract description 10
- 239000011591 potassium Substances 0.000 claims abstract description 10
- 239000011575 calcium Substances 0.000 claims abstract description 7
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 6
- 229910052791 calcium Inorganic materials 0.000 claims abstract description 6
- UAEPNZWRGJTJPN-UHFFFAOYSA-N methylcyclohexane Chemical compound CC1CCCCC1 UAEPNZWRGJTJPN-UHFFFAOYSA-N 0.000 claims description 84
- 239000001257 hydrogen Substances 0.000 claims description 76
- 229910052739 hydrogen Inorganic materials 0.000 claims description 76
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 73
- GYNNXHKOJHMOHS-UHFFFAOYSA-N methyl-cycloheptane Natural products CC1CCCCCC1 GYNNXHKOJHMOHS-UHFFFAOYSA-N 0.000 claims description 42
- 239000011148 porous material Substances 0.000 claims description 42
- 150000004678 hydrides Chemical class 0.000 claims description 32
- 102000002322 Egg Proteins Human genes 0.000 claims description 31
- 108010000912 Egg Proteins Proteins 0.000 claims description 31
- 210000003278 egg shell Anatomy 0.000 claims description 31
- 239000007864 aqueous solution Substances 0.000 claims description 19
- 239000000203 mixture Substances 0.000 claims description 15
- 238000010304 firing Methods 0.000 claims description 11
- 150000001875 compounds Chemical class 0.000 claims description 10
- 125000003118 aryl group Chemical group 0.000 claims description 8
- NNBZCPXTIHJBJL-UHFFFAOYSA-N decalin Chemical compound C1CCCC2CCCCC21 NNBZCPXTIHJBJL-UHFFFAOYSA-N 0.000 claims description 8
- -1 dibenzotriol Chemical compound 0.000 claims description 8
- CXWXQJXEFPUFDZ-UHFFFAOYSA-N tetralin Chemical compound C1=CC=C2CCCCC2=C1 CXWXQJXEFPUFDZ-UHFFFAOYSA-N 0.000 claims description 8
- QEGNUYASOUJEHD-UHFFFAOYSA-N 1,1-dimethylcyclohexane Chemical compound CC1(C)CCCCC1 QEGNUYASOUJEHD-UHFFFAOYSA-N 0.000 claims description 6
- NHCREQREVZBOCH-UHFFFAOYSA-N 1-methyl-1,2,3,4,4a,5,6,7,8,8a-decahydronaphthalene Chemical compound C1CCCC2C(C)CCCC21 NHCREQREVZBOCH-UHFFFAOYSA-N 0.000 claims description 6
- ZUOUZKKEUPVFJK-UHFFFAOYSA-N diphenyl Chemical compound C1=CC=CC=C1C1=CC=CC=C1 ZUOUZKKEUPVFJK-UHFFFAOYSA-N 0.000 claims description 6
- 238000001035 drying Methods 0.000 claims description 6
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims description 4
- PXXNTAGJWPJAGM-UHFFFAOYSA-N vertaline Natural products C1C2C=3C=C(OC)C(OC)=CC=3OC(C=C3)=CC=C3CCC(=O)OC1CC1N2CCCC1 PXXNTAGJWPJAGM-UHFFFAOYSA-N 0.000 claims description 4
- GVJFFQYXVOJXFI-UHFFFAOYSA-N 1,2,3,4,4a,5,6,7,8,8a,9,9a,10,10a-tetradecahydroanthracene Chemical compound C1C2CCCCC2CC2C1CCCC2 GVJFFQYXVOJXFI-UHFFFAOYSA-N 0.000 claims description 3
- 150000001339 alkali metal compounds Chemical class 0.000 claims description 3
- 125000002619 bicyclic group Chemical group 0.000 claims description 3
- 239000004305 biphenyl Substances 0.000 claims description 3
- 235000010290 biphenyl Nutrition 0.000 claims description 3
- 125000005982 diphenylmethyl group Chemical group [H]C1=C([H])C([H])=C(C([H])=C1[H])C([H])(*)C1=C([H])C([H])=C([H])C([H])=C1[H] 0.000 claims description 3
- 125000002950 monocyclic group Chemical group 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 description 82
- 230000000052 comparative effect Effects 0.000 description 38
- 239000000126 substance Substances 0.000 description 33
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 21
- 229910052799 carbon Inorganic materials 0.000 description 21
- 238000006356 dehydrogenation reaction Methods 0.000 description 21
- 229910052751 metal Inorganic materials 0.000 description 21
- 239000002184 metal Substances 0.000 description 21
- 238000011161 development Methods 0.000 description 16
- 230000000694 effects Effects 0.000 description 16
- 238000005516 engineering process Methods 0.000 description 16
- 238000003860 storage Methods 0.000 description 16
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 15
- 230000009467 reduction Effects 0.000 description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- 239000000243 solution Substances 0.000 description 13
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 12
- 239000007789 gas Substances 0.000 description 12
- 229910044991 metal oxide Inorganic materials 0.000 description 11
- 150000004706 metal oxides Chemical class 0.000 description 11
- 238000005470 impregnation Methods 0.000 description 10
- 150000003058 platinum compounds Chemical class 0.000 description 10
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 10
- 239000002253 acid Substances 0.000 description 9
- 238000009792 diffusion process Methods 0.000 description 9
- 239000000499 gel Substances 0.000 description 9
- 239000007788 liquid Substances 0.000 description 9
- 229910000000 metal hydroxide Inorganic materials 0.000 description 9
- 150000004692 metal hydroxides Chemical class 0.000 description 9
- 239000002994 raw material Substances 0.000 description 9
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 8
- 238000000354 decomposition reaction Methods 0.000 description 8
- 230000007423 decrease Effects 0.000 description 8
- 239000000446 fuel Substances 0.000 description 8
- 150000002431 hydrogen Chemical class 0.000 description 8
- 230000003197 catalytic effect Effects 0.000 description 7
- 238000006555 catalytic reaction Methods 0.000 description 6
- 230000006866 deterioration Effects 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 6
- 238000002360 preparation method Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 5
- 239000012535 impurity Substances 0.000 description 5
- CLSUSRZJUQMOHH-UHFFFAOYSA-L platinum dichloride Chemical compound Cl[Pt]Cl CLSUSRZJUQMOHH-UHFFFAOYSA-L 0.000 description 5
- 239000002243 precursor Substances 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 239000004317 sodium nitrate Substances 0.000 description 5
- 235000010344 sodium nitrate Nutrition 0.000 description 5
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 4
- 239000003513 alkali Substances 0.000 description 4
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 4
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 4
- 235000011130 ammonium sulphate Nutrition 0.000 description 4
- 239000011324 bead Substances 0.000 description 4
- 238000001354 calcination Methods 0.000 description 4
- 239000000017 hydrogel Substances 0.000 description 4
- 230000006872 improvement Effects 0.000 description 4
- 239000012263 liquid product Substances 0.000 description 4
- 239000008188 pellet Substances 0.000 description 4
- 238000012827 research and development Methods 0.000 description 4
- 239000011780 sodium chloride Substances 0.000 description 4
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 125000005595 acetylacetonate group Chemical group 0.000 description 3
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 3
- 239000002585 base Substances 0.000 description 3
- 238000012824 chemical production Methods 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 150000002736 metal compounds Chemical class 0.000 description 3
- 239000002923 metal particle Substances 0.000 description 3
- 239000003960 organic solvent Substances 0.000 description 3
- NLKNQRATVPKPDG-UHFFFAOYSA-M potassium iodide Chemical compound [K+].[I-] NLKNQRATVPKPDG-UHFFFAOYSA-M 0.000 description 3
- 239000004323 potassium nitrate Substances 0.000 description 3
- 235000010333 potassium nitrate Nutrition 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- FVAUCKIRQBBSSJ-UHFFFAOYSA-M sodium iodide Chemical compound [Na+].[I-] FVAUCKIRQBBSSJ-UHFFFAOYSA-M 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 229910002651 NO3 Inorganic materials 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- VSGNNIFQASZAOI-UHFFFAOYSA-L calcium acetate Chemical compound [Ca+2].CC([O-])=O.CC([O-])=O VSGNNIFQASZAOI-UHFFFAOYSA-L 0.000 description 2
- 239000001639 calcium acetate Substances 0.000 description 2
- 235000011092 calcium acetate Nutrition 0.000 description 2
- 229960005147 calcium acetate Drugs 0.000 description 2
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- PHFQLYPOURZARY-UHFFFAOYSA-N chromium trinitrate Chemical compound [Cr+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O PHFQLYPOURZARY-UHFFFAOYSA-N 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 239000012847 fine chemical Substances 0.000 description 2
- 238000009472 formulation Methods 0.000 description 2
- 238000004817 gas chromatography Methods 0.000 description 2
- 239000002815 homogeneous catalyst Substances 0.000 description 2
- XMBWDFGMSWQBCA-UHFFFAOYSA-N hydrogen iodide Chemical compound I XMBWDFGMSWQBCA-UHFFFAOYSA-N 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 230000000873 masking effect Effects 0.000 description 2
- 230000000704 physical effect Effects 0.000 description 2
- SCVFZCLFOSHCOH-UHFFFAOYSA-M potassium acetate Chemical compound [K+].CC([O-])=O SCVFZCLFOSHCOH-UHFFFAOYSA-M 0.000 description 2
- IOLCXVTUBQKXJR-UHFFFAOYSA-M potassium bromide Chemical compound [K+].[Br-] IOLCXVTUBQKXJR-UHFFFAOYSA-M 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- JHJLBTNAGRQEKS-UHFFFAOYSA-M sodium bromide Chemical compound [Na+].[Br-] JHJLBTNAGRQEKS-UHFFFAOYSA-M 0.000 description 2
- 229910052720 vanadium Inorganic materials 0.000 description 2
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 2
- PKQYSCBUFZOAPE-UHFFFAOYSA-N 1,2-dibenzyl-3-methylbenzene Chemical compound C=1C=CC=CC=1CC=1C(C)=CC=CC=1CC1=CC=CC=C1 PKQYSCBUFZOAPE-UHFFFAOYSA-N 0.000 description 1
- GVHUQXQVSWGYSH-UHFFFAOYSA-N 4-(3-bromophenyl)-2-methyl-1,3-thiazole Chemical compound S1C(C)=NC(C=2C=C(Br)C=CC=2)=C1 GVHUQXQVSWGYSH-UHFFFAOYSA-N 0.000 description 1
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- UNMYWSMUMWPJLR-UHFFFAOYSA-L Calcium iodide Chemical compound [Ca+2].[I-].[I-] UNMYWSMUMWPJLR-UHFFFAOYSA-L 0.000 description 1
- BCZXFFBUYPCTSJ-UHFFFAOYSA-L Calcium propionate Chemical compound [Ca+2].CCC([O-])=O.CCC([O-])=O BCZXFFBUYPCTSJ-UHFFFAOYSA-L 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- 229910021555 Chromium Chloride Inorganic materials 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- YVDLTVYVLJZLLS-UHFFFAOYSA-J O.Cl[Pt](Cl)(Cl)Cl Chemical compound O.Cl[Pt](Cl)(Cl)Cl YVDLTVYVLJZLLS-UHFFFAOYSA-J 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 1
- 229910021550 Vanadium Chloride Inorganic materials 0.000 description 1
- NENZXZYKVSFEOK-UHFFFAOYSA-J [Cl-].[Cl-].[Cl-].[Cl-].[Pt+4].[C]=O Chemical compound [Cl-].[Cl-].[Cl-].[Cl-].[Pt+4].[C]=O NENZXZYKVSFEOK-UHFFFAOYSA-J 0.000 description 1
- CPLPNZFTIJOEIN-UHFFFAOYSA-I [V+5].CC([O-])=O.CC([O-])=O.CC([O-])=O.CC([O-])=O.CC([O-])=O Chemical compound [V+5].CC([O-])=O.CC([O-])=O.CC([O-])=O.CC([O-])=O.CC([O-])=O CPLPNZFTIJOEIN-UHFFFAOYSA-I 0.000 description 1
- AZFUOHYXCLYSQJ-UHFFFAOYSA-N [V+5].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O Chemical compound [V+5].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O AZFUOHYXCLYSQJ-UHFFFAOYSA-N 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- LFVGISIMTYGQHF-UHFFFAOYSA-N ammonium dihydrogen phosphate Chemical compound [NH4+].OP(O)([O-])=O LFVGISIMTYGQHF-UHFFFAOYSA-N 0.000 description 1
- 229910000387 ammonium dihydrogen phosphate Inorganic materials 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 229940045985 antineoplastic platinum compound Drugs 0.000 description 1
- 239000011260 aqueous acid Substances 0.000 description 1
- QSKKXNSTGHZSQB-UHFFFAOYSA-N azane;platinum(2+) Chemical compound N.[Pt+2] QSKKXNSTGHZSQB-UHFFFAOYSA-N 0.000 description 1
- 229910001593 boehmite Inorganic materials 0.000 description 1
- 229910001622 calcium bromide Inorganic materials 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 235000011148 calcium chloride Nutrition 0.000 description 1
- WGEFECGEFUFIQW-UHFFFAOYSA-L calcium dibromide Chemical compound [Ca+2].[Br-].[Br-] WGEFECGEFUFIQW-UHFFFAOYSA-L 0.000 description 1
- 229940046413 calcium iodide Drugs 0.000 description 1
- 229910001640 calcium iodide Inorganic materials 0.000 description 1
- 239000004330 calcium propionate Substances 0.000 description 1
- 235000010331 calcium propionate Nutrition 0.000 description 1
- 235000011132 calcium sulphate Nutrition 0.000 description 1
- 150000001728 carbonyl compounds Chemical class 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- QSWDMMVNRMROPK-UHFFFAOYSA-K chromium(3+) trichloride Chemical compound [Cl-].[Cl-].[Cl-].[Cr+3] QSWDMMVNRMROPK-UHFFFAOYSA-K 0.000 description 1
- PYXSPTLIBJZHQW-UHFFFAOYSA-K chromium(3+);propanoate Chemical compound [Cr+3].CCC([O-])=O.CCC([O-])=O.CCC([O-])=O PYXSPTLIBJZHQW-UHFFFAOYSA-K 0.000 description 1
- WYYQVWLEPYFFLP-UHFFFAOYSA-K chromium(3+);triacetate Chemical compound [Cr+3].CC([O-])=O.CC([O-])=O.CC([O-])=O WYYQVWLEPYFFLP-UHFFFAOYSA-K 0.000 description 1
- PPUZYFWVBLIDMP-UHFFFAOYSA-K chromium(3+);triiodide Chemical compound I[Cr](I)I PPUZYFWVBLIDMP-UHFFFAOYSA-K 0.000 description 1
- GRWVQDDAKZFPFI-UHFFFAOYSA-H chromium(III) sulfate Chemical compound [Cr+3].[Cr+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O GRWVQDDAKZFPFI-UHFFFAOYSA-H 0.000 description 1
- XZQOHYZUWTWZBL-UHFFFAOYSA-L chromium(ii) bromide Chemical compound [Cr+2].[Br-].[Br-] XZQOHYZUWTWZBL-UHFFFAOYSA-L 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 150000001923 cyclic compounds Chemical class 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- FAHBNUUHRFUEAI-UHFFFAOYSA-M hydroxidooxidoaluminium Chemical compound O[Al]=O FAHBNUUHRFUEAI-UHFFFAOYSA-M 0.000 description 1
- 239000004434 industrial solvent Substances 0.000 description 1
- 229910052816 inorganic phosphate Inorganic materials 0.000 description 1
- 150000002605 large molecules Chemical class 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- JTHJBIGZCJVTLP-UHFFFAOYSA-J molybdenum(4+) propanoate Chemical compound C(CC)(=O)[O-].[Mo+4].C(CC)(=O)[O-].C(CC)(=O)[O-].C(CC)(=O)[O-] JTHJBIGZCJVTLP-UHFFFAOYSA-J 0.000 description 1
- WFLYOQCSIHENTM-UHFFFAOYSA-N molybdenum(4+) tetranitrate Chemical compound [N+](=O)([O-])[O-].[Mo+4].[N+](=O)([O-])[O-].[N+](=O)([O-])[O-].[N+](=O)([O-])[O-] WFLYOQCSIHENTM-UHFFFAOYSA-N 0.000 description 1
- ICYJJTNLBFMCOZ-UHFFFAOYSA-J molybdenum(4+);disulfate Chemical compound [Mo+4].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O ICYJJTNLBFMCOZ-UHFFFAOYSA-J 0.000 description 1
- TXCOQXKFOPSCPZ-UHFFFAOYSA-J molybdenum(4+);tetraacetate Chemical compound [Mo+4].CC([O-])=O.CC([O-])=O.CC([O-])=O.CC([O-])=O TXCOQXKFOPSCPZ-UHFFFAOYSA-J 0.000 description 1
- QKKCMWPOASMDQR-UHFFFAOYSA-J molybdenum(4+);tetraiodide Chemical compound I[Mo](I)(I)I QKKCMWPOASMDQR-UHFFFAOYSA-J 0.000 description 1
- PDKHNCYLMVRIFV-UHFFFAOYSA-H molybdenum;hexachloride Chemical compound [Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Mo] PDKHNCYLMVRIFV-UHFFFAOYSA-H 0.000 description 1
- 235000019837 monoammonium phosphate Nutrition 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- RPESBQCJGHJMTK-UHFFFAOYSA-I pentachlorovanadium Chemical compound [Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[V+5] RPESBQCJGHJMTK-UHFFFAOYSA-I 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 239000003348 petrochemical agent Substances 0.000 description 1
- 150000003016 phosphoric acids Chemical class 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- KGRJUMGAEQQVFK-UHFFFAOYSA-L platinum(2+);dibromide Chemical compound Br[Pt]Br KGRJUMGAEQQVFK-UHFFFAOYSA-L 0.000 description 1
- 235000011056 potassium acetate Nutrition 0.000 description 1
- 235000011164 potassium chloride Nutrition 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
- 235000007715 potassium iodide Nutrition 0.000 description 1
- BWILYWWHXDGKQA-UHFFFAOYSA-M potassium propanoate Chemical compound [K+].CCC([O-])=O BWILYWWHXDGKQA-UHFFFAOYSA-M 0.000 description 1
- 239000004331 potassium propionate Substances 0.000 description 1
- 235000010332 potassium propionate Nutrition 0.000 description 1
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 description 1
- 229910052939 potassium sulfate Inorganic materials 0.000 description 1
- 235000011151 potassium sulphates Nutrition 0.000 description 1
- MCXBMLBTPQEQJP-UHFFFAOYSA-N potassium;sodium;dinitrate Chemical compound [Na+].[K+].[O-][N+]([O-])=O.[O-][N+]([O-])=O MCXBMLBTPQEQJP-UHFFFAOYSA-N 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 235000019260 propionic acid Nutrition 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000001632 sodium acetate Substances 0.000 description 1
- 235000017281 sodium acetate Nutrition 0.000 description 1
- 229910001388 sodium aluminate Inorganic materials 0.000 description 1
- 235000009518 sodium iodide Nutrition 0.000 description 1
- JXKPEJDQGNYQSM-UHFFFAOYSA-M sodium propionate Chemical compound [Na+].CCC([O-])=O JXKPEJDQGNYQSM-UHFFFAOYSA-M 0.000 description 1
- 239000004324 sodium propionate Substances 0.000 description 1
- 235000010334 sodium propionate Nutrition 0.000 description 1
- 229960003212 sodium propionate Drugs 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 150000003463 sulfur Chemical class 0.000 description 1
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- YPFBRNLUIFQCQL-UHFFFAOYSA-K tribromomolybdenum Chemical compound Br[Mo](Br)Br YPFBRNLUIFQCQL-UHFFFAOYSA-K 0.000 description 1
- VLOPEOIIELCUML-UHFFFAOYSA-L vanadium(2+);sulfate Chemical compound [V+2].[O-]S([O-])(=O)=O VLOPEOIIELCUML-UHFFFAOYSA-L 0.000 description 1
- ZOYIPGHJSALYPY-UHFFFAOYSA-K vanadium(iii) bromide Chemical compound [V+3].[Br-].[Br-].[Br-] ZOYIPGHJSALYPY-UHFFFAOYSA-K 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
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
- B01J23/58—Platinum group metals with alkali- or alkaline earth 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
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
- B01J27/04—Sulfides
- B01J27/043—Sulfides with iron group metals or platinum group metals
- B01J27/045—Platinum group 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
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
- B01J21/04—Alumina
-
- 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
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
-
- B01J35/397—
-
- B01J35/615—
-
- B01J35/633—
-
- B01J35/647—
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
- B01J37/0205—Impregnation in several steps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0236—Drying, e.g. preparing a suspension, adding a soluble salt and drying
-
- 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
- B01J37/16—Reducing
- B01J37/18—Reducing with gases containing free hydrogen
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
- C01B3/26—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using catalysts
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/367—Formation of an aromatic six-membered ring from an existing six-membered ring, e.g. dehydrogenation of ethylcyclohexane to ethylbenzene
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
- C01B2203/1047—Group VIII metal catalysts
- C01B2203/1064—Platinum group metal catalysts
- C01B2203/107—Platinum catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1252—Cyclic or aromatic hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/02—Boron or aluminium; Oxides or hydroxides thereof
- C07C2521/04—Alumina
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
- C07C2523/42—Platinum
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals combined with metals, oxides or hydroxides provided for in groups C07C2523/02 - C07C2523/36
- C07C2523/56—Platinum group metals
- C07C2523/58—Platinum group metals with alkali- or alkaline earth metals or beryllium
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the present invention relates to a metal catalyst used in a process using a catalyst such as environmental purification such as chemical production, hydrogen production, fine chemical production, and exhaust gas treatment, and the uniform platinum-supported alumina in which platinum is supported on an alumina carrier. It relates to a catalyst, a method for producing the catalyst, and a method for using the catalyst.
- a platinum-supported alumina catalyst in which platinum or the like is supported on an alumina carrier undergoes a dehydrogenation reaction in which hydrogen is dehydrogenated with the corresponding aromatics from hydrogenated aromatics such as methylcyclohexane, cyclohexane, decalin, and dibenzyltoluene.
- a dehydrogenation reaction in which hydrogen is dehydrogenated with the corresponding aromatics from hydrogenated aromatics such as methylcyclohexane, cyclohexane, decalin, and dibenzyltoluene.
- a porous alumina carrier made of a metal oxide of alumina is prepared, and the obtained porous alumina carrier is prepared with an aqueous solution of platinum chloride, an aqueous solution of platinum ammonium chloride, acetylacetonato platinum, or the like.
- a solution of a catalytic metal compound such as a solution of an organic platinum compound
- drying to obtain a dried product carrying a catalytic metal compound, for example, under the conditions of 350 ° C. or higher and 800 ° C. or lower and 0.5 hours or longer and 24 hours or shorter. It is produced by firing, and if necessary, hydrogen-reducing the obtained catalyst metal compound-supported calcined product under the conditions of, for example, 250 ° C. or higher and 800 ° C. or lower and 0.5 hours or longer and 24 hours or lower.
- the platinum atom has a large atomic weight of 195 and a large mass, and the platinum compound is strongly adsorbed on the catalyst carrier of the platinum compound used as a platinum source. Therefore, the platinum compound is inside the alumina carrier. Since it is adsorbed and fixed only on the outer shell of the alumina carrier before it diffuses into the catalyst, when the dispersed state of the platinum metal is observed on the catalyst cross section, the platinum metal is supported only on the outer peripheral portion of the catalyst, and the carrier. It is known that it is a so-called egg shell type platinum-supporting catalyst in which no platinum metal is supported inside.
- the molecules of the raw material diffuse into the catalyst even if the active metal platinum is supported inside the catalyst. It is known that the reaction preferentially occurs around the outer shell of the catalyst particles because the reaction does not proceed sufficiently due to the slow speed. In such a reaction, the egg shell type in which the active metal is present only in the outer shell of the catalyst is more advantageous.
- the density of the active metal particles becomes high, so that the dispersion degree of the active metal particles cannot be sufficiently realized, and due to syntaring and coking. There is a risk that problems such as catalyst deterioration are likely to occur.
- Patent Document 1 discloses an egg-shell type platinum-supported alumina catalyst in which the pore sizes of the platinum-supported alumina catalyst are uniform to the extent that the diffusion resistance does not increase and the platinum dispersion is good. Further, a catalyst in which platinum metal is well dispersed over the entire cross section of the catalyst has been developed so that the surface area of the carrier can be fully utilized in the reaction in which the diffusion resistance does not affect, and Patent Document 2 describes such a catalyst. A uniform platinum-supported alumina catalyst is disclosed.
- Platinum-supported alumina catalysts have long been used in catalytic processes in a wide range of fields, but in recent years they have been used in the organic chemical hydride method, which is one method of hydrogen energy carriers that has been attracting attention as a storage and transportation technology for hydrogen energy. ing. Development of platinum-supported alumina catalysts having higher performance than conventional platinum-supported alumina catalysts has been promoted, and Patent Documents 1 and 2 are required for the use of platinum-supported alumina catalysts in the organic chemical hydride method. It discloses its use in dehydrogenation reactions.
- the organic chemical hydride method is a method of "storing" and “carrying” hydrogen as an organic chemical hydride compound (hydrogenated organic compound) in which hydrogen is incorporated into the molecular structure of a chemical product by a chemical reaction.
- the organic chemical hydride method has been proposed since the 1980s, but it is difficult to carry out industrially because the life of the dehydrogenation catalyst that generates hydrogen from the compound of the organic chemical hydride that has taken in hydrogen is extremely short.
- the key to technological development was the development of a new dehydrogenation catalyst with sufficient performance such as catalyst life that can be used industrially.
- Non-Patent Documents 3 and 4 disclose the background of the development of such an organic chemical hydride method.
- Japan has included a policy to promote the practical application and dissemination of hydrogen energy as a national policy from the 4th basic energy plan after the earthquake, and following the formulation of the hydrogen and fuel cell technology roadmap, the basic hydrogen strategy will be implemented in 2017. It has been decided by the Cabinet.
- the above-mentioned organic chemical hydride method can provide a hydrogen energy carrier that "stores” and "carries” hydrogen energy on a large scale, and its practical application is included in the basic hydrogen strategy, and hydrogen supply by 2030.
- the price target is 30 yen / Nm 3
- the 2050 target is 20 yen / Nm 3 . Therefore, cost reduction by continuous development of improved technology is required, and improvement of catalyst performance, particularly catalyst life, has a great influence on cost reduction.
- the conversion rate, selectivity and the yield which is the product of the conversion rate, have been developed to a relatively high level in the development so far, and the catalyst life of how long the performance can be maintained. Is in the stage of contributing to cost reduction.
- Japanese Patent No. 4652695 Japanese Patent No. 4142733 Yoshimi Okada, Energy / Resources, Vol.33, No. 3,168 (2016) Yoshimi Okada, Tokyo Metropolitan High Pressure Gas Association Bulletin, August 2019, September 2019 Agency for Natural Resources and Energy, Hydrogen Basic Strategy (December 2017)
- the homogeneous platinum-supported alumina catalyst of Patent Document 2 has a relatively long catalyst life and is practically useful, but further improvement is desired. Since the dehydrogenation reaction in the organic chemical hydride method is an endothermic reaction and an equilibrium reaction in which the number of molecules increases due to the reaction, the higher the reaction conditions and the lower the pressure, the more efficient it is. On the other hand, the hydrogen produced is preferably at a high pressure depending on the intended use, so that a catalyst that can be used even at a higher reaction temperature may be required. However, when the reaction conditions are high, side reactions are likely to occur, so it is necessary to improve the selectivity of the catalyst. Further, when the reaction condition becomes high temperature, carbon is likely to be generated on the catalyst, and the catalyst is likely to be deteriorated. Therefore, there is a demand for a catalyst for a long-life dehydrogenation reaction that has high selectivity under high-temperature reaction conditions and produces less carbon.
- an object of the present invention is to provide a platinum-supported alumina catalyst having excellent performance in terms of catalytic activity, selectivity, and catalyst life for a uniform platinum-supported alumina catalyst using sulfur.
- Another object of the present invention is to provide a uniform platinum-supported alumina catalyst having excellent catalytic activity and selectivity, particularly excellent performance in catalyst life, a method for producing the same, and a method for using the same.
- One aspect of the present invention is a uniform platinum-supported alumina catalyst in which an alumina carrier, sulfur or a sulfur compound dispersed over the entire cross section of the alumina carrier, and dispersed over the entire cross section of the alumina carrier. It has a supported platinum and one or more alkali metals selected from the group of sodium, potassium, and calcium. According to this aspect, the catalyst life can be improved as compared with the uniform platinum-supported alumina catalyst disclosed in Patent Document 2.
- the content of the platinum is preferably 0.05 or more and 5.0 wt% or less as the platinum element. Further, the content of the sulfur or the sulfur compound is preferably 0.15 or more and 5.0 wt% or less as the sulfur element.
- the content of the alkali metal is preferably 0.1 wt% or more and 5.0 wt% or less as the alkali metal element.
- Another aspect of the present invention is a method for producing a uniform platinum-supported alumina catalyst, wherein the step of preparing a uniform platinum-supported alumina catalyst and the uniform platinum-supported alumina catalyst are impregnated with an aqueous solution of an alkali metal compound.
- the uniform platinum-supported alumina catalyst is reduced in a hydrogen atmosphere, or the dried uniform platinum-supported alumina catalyst is fired and then reduced in a hydrogen atmosphere. Has steps and.
- Another aspect of the present invention provides a method for dehydrogenating hydrogenated aromatics by using a uniform platinum-supported alumina catalyst to dehydrogenate the hydrogenated aromatics.
- One or two kinds of hydrogenated aromatics selected from the group consisting of hydrides of monocyclic aromatics, hydrides of bicyclic aromatics, and hydrides of compounds having three or more aromatic rings. The above mixture is preferable.
- the hydrogenated aromatics are one or more selected from the group consisting of methylcyclohexane, cyclohexane, dimethylcyclohexane, tetralin, decalin, methyldecalin, biphenyl, diphenylmethyl, dibenzotriol and tetradecahydroanthracene. It should be a mixture.
- the homogeneous catalyst is effective when the diffusion of the raw material into the catalyst is sufficiently performed, and the egg shell type catalyst is effective when the diffusion into the catalyst is restricted and is not sufficiently performed. Therefore, it is preferable to use these two types of catalysts properly according to the state of diffusion in the reaction field. Further, even in the same reaction, the diffusion state of the raw material into the catalyst may differ depending on the position in the reactor, and the concentration of the raw material becomes low near the outlet where the reaction has proceeded, so that the diffusion into the catalyst can be restricted. .. In such a case, it is preferable to use a homogeneous type and an egg shell type catalyst in combination in the reactor.
- the degree of diffusion of the raw material into the catalyst is generally expressed by the catalyst effective coefficient, but the catalyst effective coefficient can be controlled by changing the size and shape of the catalyst pellets. From these, it is possible to produce platinum alumina catalysts having various catalyst effective coefficients by changing the size and shape of the catalyst pellets for both the uniform type and the egg shell type catalysts.
- the alumina carrier in which sulfur or a sulfur compound is present is preferably one in which the pore size is controlled as uniformly as possible.
- the sulfur-containing porous metal oxide has a surface area of 150 m 2 / g or more, a pore volume of 0.4 cm 3 / g or more, an average pore diameter of 40 ⁇ or more and 300 ⁇ or less, and an average pore diameter with respect to the total pore volume.
- a porous metal oxide in which the pores of ⁇ 30 ⁇ occupy 60% or more is preferable.
- the alumina carrier has uniform pore sizes throughout the powder and the compact.
- Patent Document 1 occupies pores having a surface area of 150 m 2 / g or more, a pore volume of 0.55 cm 3 / g or more, an average pore diameter of 90 ⁇ or more and 300 ⁇ or less, and a pore diameter of 90 ⁇ or more and 300 ⁇ or less with respect to the total pore volume.
- a platinum-supported alumina catalyst is disclosed in which platinum is supported on a porous ⁇ -alumina carrier having a ratio of 60% or more. As described above, this catalyst is a general egg-shell type platinum-supported alumina catalyst, and Patent Document 1 also discloses a catalyst to which an alkali metal is added as a means for improving the catalyst life.
- Patent Document 1 describes that in an egg-shell type platinum-supported catalyst, platinum is supported on platinum with a high dispersity to suppress decomposition on platinum, and addition of an alkali causes acid points on alumina. By performing masking, a remarkable effect was found in improving the catalyst life.
- Patent Document 2 discloses a uniform platinum-supported alumina catalyst that improves the catalyst life by suppressing the decomposition reaction while making the dispersed form of the supported platinum uniform by containing sulfur in the alumina carrier. doing.
- an alumina carrier containing sulfur or a sulfur compound it is considered that when an alumina carrier containing sulfur or a sulfur compound is used, the decomposition reaction suppressing effect is equal to or higher than that even if the acid spots are not masked with an alkali metal. Was done.
- the sulfur element forms a composite oxide together with alumina and changes the residual acid point to a different structure in the case of alumina alone.
- the form when the sulfur element forms a composite oxide with alumina is generally considered to be a sulfuric acid root form.
- Sulfate roots are acidic in their own right, and it is possible that the number of acid points, that is, the amount of acid, increases due to their presence, but the decomposition reaction does not proceed at reaction temperatures where these acid points are relatively low. Therefore, it was thought that the addition of alkali metal was not necessary for the uniform platinum-supported alumina catalyst using sulfur.
- the uniform platinum-supported alumina catalyst suppresses the deterioration of activity as compared with the conventional uniform platinum-supported alumina catalyst using sulfur. It was found by the reaction test that the life of the catalyst was extended. Increasing the number of alkali addition steps in catalyst production causes an increase in cost, but the cost reduction effect of extending the life of the catalyst according to the present invention is extremely higher than the cost increase in catalyst production cost, and the catalyst in the reactor Depending on the method of use, the replacement life of the dehydrogenation catalyst can be extended from the conventional 1 to 2 years to 3 to 4 years.
- This catalyst is typically used as a dehydrogenation catalyst, but is used by filling the catalyst reaction tube of a heat exchange type reactor.
- the number of catalytic reaction tubes may be several thousand in a large reactor, similar to a general heat exchanger.
- the platinum-supported alumina catalyst used in such a reactor is extracted to replace it with a new catalyst when the catalyst life is reached, which is when its performance drops to a certain yield. Platinum is recovered from the extracted waste catalyst and recycled for the production of the next replacement catalyst. Since the extraction work requires several days and the filling of the new catalyst requires more work days, it takes about two weeks to replace the catalyst. During that time, production is stopped, so reducing the frequency of replacement greatly contributes to cost reduction.
- the life of the catalyst disclosed in Patent Document 1 and Patent Document 2 is 1 to 2 years, but the life of the alkali-added uniform platinum-supported alumina catalyst according to the present invention is 4 years, and the catalyst replacement frequency is half. It can be reduced to the following.
- the uniform platinum-supported alumina catalyst of the present invention has higher catalytic performance than the conventional uniform platinum-supported alumina catalyst, and is particularly excellent in terms of catalyst life. Further, according to the production method of the present invention, these catalysts can be easily mass-produced in the existing catalyst production equipment. These catalysts can be used as a substitute for the existing platinum-supported alumina catalyst, and can also be suitably used as a dehydrogenation catalyst for methylcyclohexane or the like in the organic chemical hydride method, which is one of the hydrogen storage and transportation technologies.
- the egg-shell type metal-supported catalyst refers to a state in which the metal species supported on the cross section of the molded catalyst are dispersed and supported only on the outer shell portion of the cross section. That is, a metal-supported portion 2 in which a metal species is supported is formed on the outer shell portion of the porous carrier 1.
- the metal species are dispersed over the entire cross section of the catalyst, and the metal-supporting portion 2 on which the metal species is supported is formed throughout the inside of the molded body of the porous carrier 1. say.
- the homogeneous platinum-supported alumina catalyst is an alumina carrier, sulfur or a sulfur compound dispersed over the entire cross section of the alumina carrier, platinum dispersed and supported over the entire cross section of the alumina carrier, sodium, potassium, and It has one or more alkali metals selected from the group of calcium.
- the alumina carrier has a surface area of 150 m 2 / g or more, a pore volume of 0.40 cm 3 / g or more, an average pore diameter of 40 ⁇ or more and 300 ⁇ or less, and an average pore diameter of ⁇ 30 ⁇ or less with respect to the total pore volume. Occupies more than 60%.
- the alumina carrier is preferably a porous ⁇ -alumina carrier.
- alumina carrier for example, as disclosed in Japanese Patent Publication No. 6-72,005, a slurry of aluminum hydroxide produced by neutralizing an aluminum salt is filtered and washed, and the obtained alumina hydrogel is dehydrated and dried, and then 400.
- It is preferably a porous ⁇ -alumina carrier obtained by firing at ° C. or higher and 800 ° C. or lower for about 1 to 6 hours, and more preferably, the pH value of alumina hydrogel is set in the alumina hydrogel dissolved pH range and the boehmite gel precipitated pH range.
- Porousness obtained through a pH swing step in which an alumina hydrogel-forming substance is added to grow an alumina hydrogel crystal when the pH is changed from at least one of the pH regions to the other. It is preferably a sex ⁇ -alumina carrier.
- the porous ⁇ -alumina carrier obtained through this pH swing step has excellent uniformity of pore distribution, and there is little variation in physical properties even in the molded alumina carrier pellets, and the physical properties of each pellet are stable. It is excellent in that it is.
- the sulfur or sulfur compound to be contained in the alumina carrier by pre-dispersing it has a sulfur element and is contained in the catalyst carrier in a uniformly dispersed state at the time of preparing the catalyst carrier or after the preparation of the catalyst carrier.
- sulfur crystal powder and sulfur-containing compounds such as sulfates such as sulfuric acid and ammonium sulfate, and water or water or from the viewpoint that sulfur is easily dispersed on the carrier.
- Sulfur compounds that are soluble in organic solvents are preferred, and examples of such sulfur compounds include sulfate, ammonium sulfate, and the like.
- the amount of sulfur contained in the carrier is preferably 0.15 wt% or more and 5.0 wt% or less as a sulfur element, and more preferably 0.15 wt% or more and 3.0 wt% or less.
- the sulfur content is less than 0.15 wt%, the effect is low to the extent that the metal is uniformly supported up to the center of the catalyst, and when the sulfur content exceeds 5 wt%, sulfur tends to aggregate locally. The problem that the metal is not dispersed and supported in such a local area tends to occur. From these, the most preferable range of sulfur content in the effect of uniformly dispersing and supporting the metal is 0.15 wt% or more and 5.0 wt% or less.
- the method for preparing a sulfur-containing catalyst carrier containing the above-mentioned sulfur or sulfur compound may be such that the sulfur or sulfur compound can be contained in a state of being dispersed over the entire cross section of the carrier, for example, A.
- B catalyst carrier.
- a metal hydroxide gel that serves as a precursor of a metal oxide containing sulfur is prepared using metal sulfate and / or sulfuric acid at the time of preparation, formed into a predetermined shape, dried, and fired.
- Method C A metal hydroxide gel, which is a precursor of a metal oxide, is formed into a predetermined shape at the time of preparation of a catalyst carrier, and then dried to obtain a dry metal hydroxide gel, and a sulfur compound is added to the dry metal oxide.
- Method of preparing by impregnating with a solution and then firing D: A metal hydroxide gel that is a precursor of a metal oxide is formed into a predetermined shape at the time of preparing a catalyst carrier, and then dried and dried. Then, the dry metal hydroxide is impregnated with a sulfur compound solution and then fired to prepare.
- E A metal hydroxide gel as a precursor of the metal oxide is formed into a predetermined shape, and then dried.
- the dried metal hydroxide gel is then calcined to obtain a calcined metal oxide obtained by calcining the dry metal hydroxide gel, and the calcined metal oxide is impregnated with a sulfur compound solution such as an aqueous sulfuric acid solution or an aqueous ammonium sulfate aqueous solution. After that, a method of preparing by firing again can be exemplified.
- the firing temperature is usually 100 ° C. or higher and 1000 ° C. or lower, preferably 350 ° C. or higher and 800 ° C. or lower, and the firing time is 0.5 hours or longer. It is 48 hours or less, preferably 1 hour or more and 24 hours or less. If the calcination temperature is lower than 350 ° C., the conversion from hydroxide to oxide may not be sufficiently performed, and conversely, if the calcination temperature is higher than 800 ° C., the surface area after calcination may be significantly reduced.
- the amount of platinum supported on the sulfur-containing catalyst carrier is 0.05 wt% or more and 5.0 wt% or less, preferably 0.1 wt% or more and 3.0 wt% or less as the platinum element. If the amount of platinum supported is less than 0.05 wt%, there is a problem that the activity is low. On the contrary, if it is more than 5.0 wt%, the particle size of platinum becomes large, the selectivity is lowered, and sintering is easy. There is a problem that it is easily deteriorated.
- the above alumina carrier may be impregnated with a solution of a platinum compound, dried, and then fired at a predetermined temperature.
- the platinum compound include various complex compounds such as chloride, bromide, ammonium salt, carbonyl compound, amine and ammine complex of platinum and acetylacetonato complex.
- the platinum compound include platinum compounds such as platinum chloride, acetylacetonato platinum, ammonium platinum salt, platinum bromide, platinum dichloride, platinum tetrachloride hydrate, and carbonyl platinum dichloride dichloride. ..
- the alumina carrier to which the platinum compound is attached is dried under the conditions of 50 ° C. or higher and 200 ° C. or lower, 0.5 hours or higher and 48 hours or lower, and then 350 ° C. or higher and 600. It is fired at a temperature of ° C. or lower, 0.5 hours or more and 48 hours or less, more preferably 350 ° C. or higher and 450 ° C. or lower, under conditions of 0.5 hours or more and 5 hours or less.
- the amount of alkali added to the homogeneous platinum-supported alumina catalyst is 0.1 wt% or more and 5.0 wt% or less, preferably 0.3 wt% or more and 3.0 wt% or less, and more preferably 0.5 wt% or more and 1.5 wt% or less. Is. If the amount of the alkali metal supported is less than 0.1 wt%, the catalyst life is short and the effect is low. On the contrary, if it is more than 5.0 wt%, the activity is lowered and the catalyst life is shortened. Occurs.
- Examples of the compound of the alkaline metal used when supporting the alkaline metal on the homogeneous platinum-supported alumina catalyst include chloride, bromide, iodide, nitrate, sulfate, acetate, propionate and the like of the alkaline metal, which is preferable. Is water-soluble and / or soluble in an organic solvent such as acetone, for example, sodium chloride, sodium bromide, sodium iodide, sodium nitrate, sodium sulfate, sodium acetate, sodium propionate, potassium chloride, etc.
- Examples thereof include potassium bromide, potassium iodide, potassium nitrate, potassium sulfate, potassium acetate, potassium propionate, calcium chloride, calcium bromide, calcium iodide, calcium nitrate, calcium sulfate, calcium acetate, calcium propionate and the like.
- the temperature is room temperature or higher and 200 ° C. or lower and 0.5 hours or higher and 48 hours or lower, preferably 50 ° C. or higher.
- the temperature is room temperature or higher and 200 ° C. or lower and 0.5 hours or higher and 48 hours or lower, preferably 50 ° C. or higher.
- It is fired under the conditions of 48 hours or more, preferably 350 ° C. or more and 450 ° C. or less, and 0.5 hours or more and 5 hours or less.
- the alkali metal-supported dried product obtained by impregnating a uniform platinum-supported alumina catalyst with an alkali metal and drying it is finally hydrogen-reduced and used in the reaction.
- the reduction conditions for this hydrogen reduction are preferably 350 ° C. or higher and 600 ° C. or lower and 0.5 hours or longer and 48 hours or lower, preferably 350 ° C. or higher and 550 ° C. or lower and 3 hours or longer and 24 hours or shorter under the atmosphere of hydrogen gas. .. If the temperature at the time of hydrogen reduction is less than 350 ° C., there is a problem that platinum is not sufficiently reduced, and if it exceeds 600 ° C., there is a problem that platinum particles are syntarated at the time of reduction and the metal dispersity is lowered.
- the method for producing a uniform platinum-supported alumina catalyst includes a step of preparing a uniform platinum-supported alumina catalyst, a step of impregnating the uniform platinum-supported alumina catalyst with an aqueous solution of an alkali metal compound, and then drying the catalyst. It has a step of reducing the type platinum-supported alumina catalyst in a hydrogen atmosphere, or firing a dried uniform platinum-supported alumina catalyst, and then reducing the type in a hydrogen atmosphere.
- the uniform platinum-supported alumina catalyst of the present invention is used, for example, as a dehydrogenation catalyst for hydrogenated aromatics used as a hydrogen energy carrier in the organic chemical hydride method, which is one of the storage and transportation methods for hydrogen energy.
- the hydrogenated aromatics are one or more selected from the group consisting of hydrides of monocyclic aromatics, hydrides of bicyclic aromatics, and hydrides of compounds having three or more aromatic rings. It is preferable to be a mixture of.
- the hydrogenated aromatics are one or a mixture of two or more selected from the group consisting of methylcyclohexane, cyclohexane, dimethylcyclohexane, tetralin, decalin, methyldecalin, biphenyl, diphenylmethyl, dibenzotriol, and tetradecahydroanthracene. It should be.
- catalyst deterioration is observed in which the performance gradually deteriorates with the lapse of the reaction time.
- the cause of catalyst deterioration is carbon precipitation called caulking.
- Caulking is a phenomenon in which carbon precipitation occurs on the surface of platinum metal, which is an active metal, mainly due to a decomposition reaction of a raw material compound such as methylcyclohexane, and as a result, the effective active points of the active metal are covered and do not function.
- Hydrogen has been attracting attention as a clean secondary energy since the 1970s, and in Japan, hydrogen production technology and hydrogen production technology were used in the 1974-1992 Sunshine Project, the 1978-1992 Moonlight Project, and the 1993-2001 New Sunshine Project. Research and development of fuel cells has been promoted.
- the development of the liquefied hydrogen method was started in the WE-NET project from 1992 to 2002.
- the development of the organic chemical hydride method has a long history, dating back to the Euro Quebec project implemented as an international research and development project by the Quebec government of Canada and 12 European countries in the 1980s. The plan was to use the abundant surplus hydroelectric power in Quebec to electrolyze water to produce hydrogen and transport the Atlantic Ocean for use in Europe.
- a liquid hydrogen method is being studied as a first candidate, a liquid ammonia method as a second candidate, and an organic chemical hydride method as a third candidate.
- the organic chemical hydride method was called the MCH method.
- the Euro Quebec project was carried out for about 10 years until around 1992, but neither method was put into practical use and the plan was completed. Since then, the technology for storing and transporting hydrogen on a large scale has been put into practical use. Not converted.
- the Organic Chemical Hydrolide Method is a saturated cyclic compound such as methylcyclohexane (MCH) that incorporates hydrogen into the molecule by hydrogenating hydrogen with an aromatic such as toluene (TOR).
- MCH methylcyclohexane
- TOR aromatic such as toluene
- TOR is a fuel base material contained in high-octane gasoline in an amount of 10 wt% or more, and is also widely used as an industrial solvent. It is easy to procure in large quantities because it is a general-purpose chemical that is produced in the world with more than 20 million tons per year.
- the first of this method is that it is a highly safe method that can reduce the potential risk of hydrogen storage and transportation on a large scale to the risk of conventional gasoline storage and transportation in principle. It is a feature and is the first reason why the applicant paid attention to this method.
- storage in large tanks of TOR and MCH and transportation by chemical tankers and chemical lorries have been put into practical use as chemical substances for a long time.
- Demand for gasoline and light oil automobile fuels is expected to decrease due to the trend toward electrification of automobiles in the future, and it is also a great merit that existing infrastructure such as these storage tanks can be diverted.
- a repeated demonstration demonstration plant was constructed in 2013, and a total of about 10,000 hours of demonstration operation was carried out from April of the same year to November 2014, and it was confirmed that high performance as designed could be maintained stably, and the technology was established. Completed.
- NEDO New Energy and Industrial Technology Development
- Japan has included a policy to promote the practical application and dissemination of hydrogen energy as a national policy from the 4th basic energy plan after the earthquake, and following the formulation of the hydrogen and fuel cell technology roadmap, the basic hydrogen strategy will be implemented in 2017. It has been decided by the Cabinet.
- the above-mentioned organic chemical hydride method is included in the basic hydrogen strategy as a hydrogen energy carrier that "stores” and "carries" hydrogen energy on a large scale, and its practical application is included in the hydrogen supply price target of 30 yen by 2030.
- / Nm 3 , 20 ⁇ / Nm 3 is set as a target for 2030. From this, cost reduction by continuous development of improved technology is required, and improvement of catalyst performance is an important factor for cost reduction. Therefore, the present invention is effective in practical use of the organic chemical hydride method and is industrially effective. Is an invention with high utility.
- the homogeneous platinum-supported alumina catalyst can be effectively used not only as a catalyst but also as an adsorbent and the like. It is also useful as a guard column filler for the purpose of pretreatment for adsorbing impurities and the like in a catalytic reaction process to which the catalyst of the present invention can be applied, such as application to the organic chemical hydride method.
- the uniform platinum-supported alumina catalyst according to the present embodiment may be used together with an egg-shell type platinum-supported alumina catalyst.
- the egg-shell type second component-added platinum-supported alumina catalyst is one or more selected from the group of an alumina carrier, platinum dispersed and supported on the outer shell of the alumina carrier, and vanadium, chromium, molybdenum, and phosphorus. It is preferable to have the second component of.
- the alumina carrier has a surface area of 150 m 2 / g or more, a pore volume of 0.40 cm 3 / g or more, an average pore diameter of 40 ⁇ or more and 300 ⁇ or less, and pores having an average pore diameter of ⁇ 30 ⁇ with respect to the total pore volume.
- the proportion should be 60% or more.
- the amount of platinum supported on the alumina carrier is preferably 0.05 wt% or more and 5.0 wt% or less, preferably 0.1 wt% or more and 3.0 wt% or less.
- the egg shell type platinum-supported alumina catalyst may contain a second component for the purpose of extending the life.
- the amount of the second component added is preferably 0.1 wt% or more and 5 wt% or less, preferably 0.3 wt% or more and 3.0 wt% or less, and more preferably 0.5 wt% or more and 2.0 wt% or less.
- Examples of the compound of the second component used when adding the second component to the egg shell type platinum-supported alumina catalyst include chloride, bromide, iodide, nitrate, sulfate, acetate, propionate and the like of the second component element.
- an organic solvent such as acetone
- examples thereof include inorganic phosphates such as phosphoric acid and ammonium dihydrogen phosphate, and organic phosphoric acid compounds.
- the egg shell type second component-added platinum-supported alumina catalyst and the uniform type platinum-supported alumina catalyst may be filled in the same reactor.
- the egg-shell type second component-added platinum-supported alumina catalyst and the homogeneous platinum-supported alumina catalyst may be arranged in series or mixed with each other.
- the uniform platinum-supported alumina catalyst can be suitably used for the dehydrogenation reaction of hydrogenated aromatics such as methylcyclohexane used as a hydrogen energy carrier, and can be used for practical use of an organic chemical hydride method hydrogen storage and transportation system.
- hydrogenated aromatics such as methylcyclohexane used as a hydrogen energy carrier
- organic chemical hydride method hydrogen storage and transportation system In addition to contributing, it has the potential to be widely applied to existing catalytic reaction processes in which platinum-supported alumina catalysts are used, and has extremely high industrial utility.
- a suspension of aluminum hydroxide slurry (pH 10) was obtained by instantly adding an aqueous solution of sodium aluminate to hot dilute sulfuric acid with vigorous stirring, and this was used as seed aluminum hydroxide, and hot dilute sulfuric acid and aluminum were continuously stirred. The operation of alternately adding the aqueous acid soda solution at regular intervals was repeated to obtain a sulfuric acid-washed cake, which was extruded and dried, and then baked at 500 ° C. for 3 hours.
- the alumina carrier thus obtained has a BET surface area of 257 m 2 / g, a pore volume of 0.66 cm 3 / g by the mercury intrusion method, and an average pore diameter of 9.3 nm, and most of the pores are near the average pore diameter. It has a sharp pore distribution concentrated in, and the volume occupied by pores with a pore diameter of 7-13 nm is 85% or more of the total pore volume, and the porous ⁇ -alumina obtained from this result.
- the carrier has a surface area of 150 m 2 / g or more, a pore volume of 0.40 cm 3 / g or more, an average pore diameter of 40 ⁇ or more and 300 ⁇ or less, and pores having an average pore diameter of ⁇ 30 ⁇ with respect to the total pore volume.
- the ratio meets the requirement of 60% or more.
- Example 1 (Catalyst No. 5)]
- an aqueous sodium potassium nitrate solution having a concentration of 0.085 mol / L was added, left to stand for 3 hours for impregnation, and then water was removed by an evaporator.
- the mixture was dried at 120 ° C. for 3 hours and then calcined in an air flow at 450 ° C. for 3 hours in a muffle furnace to obtain a homogeneous alkali-added sulfur-platinum-supported alumina catalyst (catalyst No. 5) according to Example 1.
- This catalyst contains 1.0 wt% of platinum and 0.4 wt% of sodium as an alkali metal as a sodium element.
- Examples 2 and 3 (catalyst Nos. 6 and 7)] Using the same method as in Example 1, the concentration of the sodium nitrate aqueous solution added to 20 g of the uniform sulfur-platinum-supported alumina catalyst of Comparative Example 3 was changed to adjust the sodium-supported amount to 0.8 and 1.6 wt%. A homogeneous alkali-added sulfur-platinum-supported alumina catalyst (catalyst Nos. 6 and 7) was prepared.
- Example 4 (Catalyst No. 8)] Using the same method as in Example 1, the solution added to 20 g of the homogeneous sulfur-platinum-supported alumina catalyst of Comparative Example 3 was changed from a sodium nitrate aqueous solution to a sodium chloride aqueous solution, and the sodium supporting amount was 0.8 wt%. A homogeneous alkali-added sulfur-platinum-supported alumina catalyst (catalyst No. 8) was prepared.
- Example 5 (Catalyst No. 9)
- water was removed by an evaporator.
- the mixture was dried at 120 ° C. for 3 hours and then calcined in an air flow at 450 ° C.
- This catalyst contains 1.0 wt% of platinum and 0.8 wt% of sodium as an alkali metal as a sodium element.
- Example 6 (Catalyst No. 10)] To 20 g of the uniform platinum-supported alumina catalyst of Comparative Example 3, 40 mL of an aqueous potassium nitrate (K) solution having a concentration of 0.044 mol / L was added, left to stand for 3 hours for impregnation, and then water was removed by an evaporator. Next, the mixture was dried at 120 ° C. for 3 hours and then calcined in an air flow at 450 ° C. for 3 hours in a muffle furnace to obtain a homogeneous alkali-added sulfur-platinum-supported alumina catalyst (catalyst No. 10) according to Example 6. .. This catalyst contains 1.0 wt% of platinum and 0.34 wt% of potassium as an alkali metal as a potassium element.
- K potassium nitrate
- Examples 7 and 8 (catalyst Nos. 11 and 12)] Using the same method as in Example 6, the concentration of the potassium nitrate aqueous solution added to 20 g of the homogeneous sulfur-platinum-supported alumina catalyst of Comparative Example 3 was changed to make the potassium-supported amount 0.7, 1.4 wt% uniform. A type alkali-added sulfur-platinum-supported alumina catalyst (catalyst Nos. 11 and 12) was prepared.
- Example 9 (Catalyst No. 13)]
- a calcium acetate (Ca) aqueous solution having a concentration of 0.10 mol / L was added, left to stand for 3 hours for impregnation, and then water was removed by an evaporator.
- the mixture was dried at 120 ° C. for 3 hours and then calcined in an air flow at 450 ° C. for 3 hours in a muffle furnace to obtain a homogeneous alkali-added sulfur-platinum-supported alumina catalyst (catalyst No. 13) according to Example 9. ..
- This catalyst contains 1.0 wt% of platinum and 0.8 wt% of calcium as an alkali metal as a calcium element.
- the temperature of the catalyst layer was raised to 380 ° C., and pretreatment reduction was performed for 15 hours under a hydrogen stream.
- the catalyst layer inlet temperature was set to 400 ° C.
- the catalyst layer outlet temperature was set to 410 ° C.
- the pressure was 0.3 MPa.
- Gas was supplied to the reactor at a flow rate of 2.9 L / h (LHSV: 8h -1).
- a cooler is provided on the outlet side of the reaction tube to cool the gas emitted from the reactor, and the liquid product such as liquefied toluene (TOR) and gas such as hydrogen gas are collected in a stainless steel container. The liquid was separated.
- the recovered liquid product and gas were each subjected to composition analysis by gas chromatography, and the MCH conversion rate (%) and TOR selectivity (%) from the start of the reaction to 140 hours later were calculated.
- the catalyst after the reaction test was extracted, and the amount of carbon produced, which is a factor of catalyst deterioration, was measured by a carbon / sulfur analyzer.
- each catalyst has an outer diameter of 5 mm at the center of a stainless steel reaction tube with an inner diameter of 21.2 mm x 816 mm and a thermocouple protective tube with an outer diameter of 1/4 inch at the center of the reaction tube cross section.
- a reaction test for evaluating the catalyst stability for a long period of time was carried out in the following manner.
- 8.5 g of each catalyst has an outer diameter of 5 mm at the center of a stainless steel reaction tube with an inner diameter of 21.2 mm x 816 mm and a thermocouple protective tube with an outer diameter of 1/4 inch at the center of the reaction tube cross section.
- the upper side of the catalyst was filled with spherical ⁇ -alumina beads having an outer diameter of 1 mm as a preheating layer.
- the catalyst layer temperature was set to 380 ° C., and pretreatment reduction was performed under the condition of 15 hours under a hydrogen stream. After the pretreatment reduction is completed, the catalyst layer inlet temperature is set to 280 ° C., the catalyst layer outlet temperature is set to 380 ° C., and the reaction pressure is set to 0.55 MPa, and the MCH gas is reacted at a flow rate of 2.8 L / h (LHSV: 2.6 h -1). Supplied to the vessel.
- a cooler is provided on the outlet side of the reaction tube to cool the gas emitted from the reactor, and the liquid product such as liquefied toluene (TOR) and gas such as hydrogen gas are collected in a stainless steel container. The liquid was separated. The recovered liquid product and gas were each subjected to composition analysis by gas chromatography, and the MCH conversion rate (%) and TOR selectivity (%) from the start of the reaction to 1400 hours later were calculated.
- the homogeneous sulfur-platinum-supported alumina catalyst of Comparative Example 3 exhibits excellent catalytic performance, but the amount of carbon produced after the reaction test is 2.6 wt%, which is that of Comparative Example 2 (catalyst No. 2). It can be seen that the amount is increased as compared with the egg shell type alkali-added platinum-supported alumina catalyst.
- platinum which is a catalyst component, is uniformly dispersed on the carrier to improve the dispersibility and has a large number of active sites effective for the reaction, so that the amount of carbon precipitation increases. Even so, it is presumed that it still retains an active site that is effective for the reaction.
- the improvement of the TOR selectivity is a difference of 0.1% as a numerical value, but since the amount of impurities generated is calculated by the following formula, the TOR selectivity is improved from 99.8% to 99.9%. This means that the amount of impurities produced is suppressed to about half.
- Impurity production amount MCH supply amount x MCH conversion rate / 100 x (100-TOR selectivity) / 100
- Example 6 in which 0.3 wt% of potassium as an alkali metal was further added to the homogeneous sulfur-platinum-supported alumina catalyst of Comparative Example 3, the initial MCH conversion rate of the accelerated reaction test and Comparative Example 3 were also obtained.
- the MCH conversion rate after 140 hours was maintained at 96.6%, which was higher than 95.0% in Comparative Example 3, and the amount of carbon produced after the reaction test was 1.3%, which was about half. It can be seen that it is reduced to some extent.
- Example 9 in which 0.8 wt% of calcium as an alkali metal was further added to the homogeneous sulfur-platinum-supported alumina catalyst of Comparative Example 3, the initial MCH conversion rate of the accelerated reaction test was 96.4. Although the MCH conversion rate is slightly lower than that of Comparative Example 3, the TOR selectivity is improved, and the amount of carbon produced after the reaction test is reduced to about half, which is 1.5%. I understand.
- Example 2 the amount of sodium added was 0.8 wt%) in which the effect of the amount of sodium added to the homogeneous sulfur-platinum-supported alumina catalyst was examined, the initial MCH conversion rate was 98.5%, 140 hours later. Although the MCH conversion rate of MCH was 97.2%, which was slightly lower than that of Example 1, it was found that the value was still higher than that of Comparative Example 3 and the amount of carbon produced was further reduced to 0.7 wt%.
- Example 3 the amount of sodium added was 1.6 wt%) in which the effect of the amount of sodium added to the homogeneous sulfur-platinum-supported alumina catalyst was examined, the initial MCH conversion rate was 96.1% and 140 hours. It can be seen that the subsequent MCH conversion rate is 93.9%, which is further lower than that of Example 2, and is about the same as that of Comparative Example 3, but the amount of carbon produced is reduced to 0.7 wt%.
- Example 3 From the results of Examples 1-3, the addition of sodium to the uniform sulfur-platinum-supported alumina catalyst is effective in reducing the amount of carbon produced, and exerts the effect of stabilizing the MCH conversion rate due to the decrease in the amount of carbon produced. It is thought that it is. On the other hand, in Example 3, the MCH conversion rate was reduced at the initial stage and after 140 hours, suggesting that excessive addition of sodium may also reduce the reactivity of platinum.
- Example 4 in which the sodium raw material was changed to NaCl in the addition of sodium to the homogeneous sulfur-platinum-supported alumina catalyst, the results were almost the same as in Example 2 in which the same amount of sodium was added. It can be seen that there is no influence of the raw materials.
- Example 5 in which sodium and platinum were simultaneously supported in the addition of sodium to the homogeneous sulfur-platinum-supported alumina catalyst, the results were almost the same as in Example 2 in which the same amount of sodium was added. , It can be seen that there is almost no effect even if platinum and sodium are supported at the same time.
- Example 2 Catalyst No. 6, sodium 0.8 wt%) having a relatively high MCH conversion rate and stable transition, and a small amount of carbon produced. From the results of Table 2 in which On the other hand, the MCH conversion rate of the uniform platinum-supported alumina catalyst of Comparative Example 3 (catalyst No. 3) was reduced by 0.9%, and the uniform alkali-added sulfur-platinum-supported alumina catalyst had a long catalyst life. I understand.
- the TOR selectivity of the homogeneous alkali-added sulfur-platinum-supported alumina catalyst was maintained at 99.9% from 50 hours after the start of the reaction to 1400 hours after the start of the reaction, and Comparative Example 3 (Catalyst No. 3). It can be seen that the catalyst exhibits a higher TOR selectivity than the uniform platinum-supported alumina catalyst of No. 1 and produces a small amount of impurities. In total, the amount of carbon produced after the 1400-hour reaction test was as small as 1.2% in Example 2 compared to 3.1% in Comparative Example 3, and the stability of the catalyst was improved by suppressing the amount of carbon produced. It was confirmed that the effect was obtained.
- the alkali-added uniform platinum-supported alumina catalyst of the present invention can be suitably used for the dehydrogenation reaction of hydrogenated aromatics such as methylcyclohexane used as a hydrogen energy carrier, and the organic chemical hydride method hydrogen storage and transportation system can be put into practical use.
- hydrogenated aromatics such as methylcyclohexane used as a hydrogen energy carrier
- organic chemical hydride method hydrogen storage and transportation system can be put into practical use.
- it has the potential to be widely applied to existing catalytic reaction processes in which a platinum-supported alumina catalyst is used, and is an invention with extremely high industrial utility.
Abstract
Description
熱希硫酸中に激しく撹拌しながら瞬時にアルミン酸ソーダ水溶液を加えることにより水酸化アルミニウムスラリーの懸濁液(pH10)を得、これを種子水酸化アルミニウムとして、撹拌を続けながら熱希硫酸とアルミン酸ソーダ水溶液を交互に一定時間おいて加える操作を繰り返し、ろ過洗浄ケーキを得、これを押し出し成形して乾燥した後、500℃で3時間焼成した。このようにして得られたアルミナ担体は、BET表面積257m2/g、水銀圧入法による細孔容積0.66cm3/g、平均細孔径9.3nmであり、ほとんどの細孔が平均細孔径付近に集中したシャープな細孔分布を有しており、7-13nmの細孔径を有する細孔が占める容積は全細孔容積の85%以上であり、この結果から得られた多孔性γ-アルミナ担体は、表面積が150m2/g以上、細孔容積が0.40cm3/g以上、平均細孔径が40Å以上300Å以下、及び全細孔容積に対して平均細孔径±30Åの細孔が占める割合が60%以上の要件を満たしている。
実施例と比較する目的で比較例1に係るエッグシェル型白金担持アルミナ触媒(触媒No.1)を製造した。上記のように調製した多孔性γ-アルミナ担体20gに、pH値が2.0になるように調製した0.026mol/Lの塩化白金酸水溶液40mLを添加し、3時間放置して含浸させた後、エバポレーターにより水を除去し、次いで120℃で3時間乾燥させてからマッフル炉により空気流通下に450℃で3時間焼成して、1wt%の白金を担持したエッグシェル型白金担持アルミナ触媒(触媒No.1)を調製した。
比較例1と同様に調製して得られたエッグシェル型白金担持アルミナ触媒20gに、0.085mol/Lの硝酸ナトリウム(Na)水溶液40mLを添加し、3時間放置して含浸させた後、エバポレーターにより水を除去した。次いで120℃で3時間乾燥させてからマッフル炉により空気流通下に450℃で3時間焼成して、0.8wt%のナトリウム(Na)と1wt%の白金を担持した、エッグシェル型アルカリ添加白金担持アルミナ触媒(触媒No.2)を得た。比較例2に係るエッグシェル型アルカリ添加白金担持アルミナ触媒は、上記の特許文献1に記載された触媒に相当する。
前述の方法で調整した多孔性γ-アルミナ担体20gに、濃度0.16mol/Lの硫酸アンモニウム水溶液40mLを添加し、3時間放置して含浸させた後、エバポレーターにより水を除去した。次いで、120℃で3時間乾燥させてからマッフル炉により空気流通下に500℃で3時間焼成して硫黄分を含むアルミナ担体を得た。
比較例3(触媒No.3)と同様の方法で調整した硫黄分を含むアルミナ担体20gに、濃度0.18mol/Lのジニトロジアミン白金水溶液5.6mLを用いて焼成後の白金担持量が1.0wt%となるように含浸させた後、エバポレーターにて水分を除去した。次いで120℃で3時間乾燥させてからマッフル炉により空気流通下に450℃で3時間焼成して、硫黄分1.0wt%を含み、1.0wt%の白金をエッグシェル型に担持したエッグシェル型硫黄-白金担持アルミナ触媒を得た。
比較例3の均一型白金担持アルミナ触媒20gに、濃度0.085mol/Lの硝酸ナトリウムカリウム水溶液40mLを添加し、3時間放置して含浸させた後、エバポレーターにより水を除去した。次いで120℃で3時間乾燥させてからマッフル炉により空気流通下に450℃で3時間焼成して、実施例1に係る均一型アルカリ添加硫黄-白金担持アルミナ触媒(触媒No.5)を得た。この触媒は、白金を1.0wt%含有し、アルカリ金属としてのナトリウムをナトリウム元素として0.4wt%含有する。
実施例1と同様の方法を用い、比較例3の均一型硫黄-白金担持アルミナ触媒20gに添加する硝酸ナトリウム水溶液の濃度を変更して、ナトリウム担持量を0.8、1.6wt%とした均一型アルカリ添加硫黄-白金担持アルミナ触媒(触媒No.6、7)を調製した。
実施例1と同様の方法を用い、比較例3の均一型硫黄-白金担持アルミナ触媒20gに添加する溶液を硝酸ナトリウム水溶液から塩化ナトリウム水溶液に変更して、ナトリウム担持量を0.8wt%とした均一型アルカリ添加硫黄-白金担持アルミナ触媒(触媒No.8)を調製した。
比較例3と同様の方法で調製した硫黄分を含むアルミナ担体20gにpH=2.0に調製した濃度0.026mol/Lの塩化白金酸と0.17mol/Lの塩化ナトリウムとを同時に加えた水溶液40mLを添加し、3時間放置して含浸させた後、エバポレーターにより水を除去した。次いで120℃で3時間乾燥させてからマッフル炉により空気流通下に450℃で3時間焼成して、実施例5に係る均一型アルカリ添加硫黄-白金担持アルミナ触媒(触媒No.9)を得た。この触媒は、白金を1.0wt%含有し、アルカリ金属としてのナトリウムをナトリウム元素として0.8wt%含有する。
比較例3の均一型白金担持アルミナ触媒20gに、濃度0.044mol/Lの硝酸カリウム(K)水溶液40mLを添加し、3時間放置して含浸させた後、エバポレーターにより水を除去した。次いで120℃で3時間乾燥させてからマッフル炉により空気流通下に450℃で3時間焼成して、実施例6に係る均一型アルカリ添加硫黄-白金担持アルミナ触媒(触媒No.10)を得た。この触媒は白金を1.0wt%含有し、アルカリ金属としてのカリウムをカリウム元素として0.34wt%含有する。
実施例6と同様の方法を用い、比較例3の均一型硫黄-白金担持アルミナ触媒20gに添加する硝酸カリウム水溶液の濃度を変更して、カリウム担持量を0.7、1.4wt%とした均一型アルカリ添加硫黄-白金担持アルミナ触媒(触媒No.11、12)を調製した。
比較例3の均一型白金担持アルミナ触媒20gに、濃度0.10mol/Lの酢酸カルシウム(Ca)水溶液40mLを添加し、3時間放置して含浸させた後、エバポレーターにより水を除去した。次いで120℃で3時間乾燥させてからマッフル炉により空気流通下に450℃で3時間焼成して、実施例9に係る均一型アルカリ添加硫黄-白金担持アルミナ触媒(触媒No.13)を得た。この触媒は白金を1.0wt%含有し、アルカリ金属としてのカルシウムをカルシウム元素として0.8wt%含有する。
次に、上記の比較例1~4(触媒No.1~4)及び実施例1~9(触媒No.5~13)を用い、比較的に短時間で性能の差とカーボン析出量とが観察されるように加速条件(高温)での反応試験を実施した。反応試験は比較的に短時間で性能の差が得られるよう加速条件で実施した。反応管断面の中心に外形1/8インチの熱電対用保護管を備えた内径12.6mm×300mmサイズのステンレス製反応管の長さ方向の中心部に、1.3gの各触媒をα-アルミナビーズ11.7gで希釈して充填した。触媒の上側に予熱層として外径1mmの球状α-アルミナビーズを充填した。その後、触媒層温度を380℃に昇温して、水素気流下で15時間の前処理還元を行った。前処理還元終了後、触媒層入口温度を400℃、触媒層出口温度が410℃、圧力0.3MPaに設定し、前処理還元として供給した水素ガスを止め、ヒーターで蒸発させたメチルシクロヘキサン(MCH)ガスを2.9L/h(LHSV:8h-1)の流量で反応器に供給した。反応管の出口側には、反応器から出たガスを冷却する冷却器を設け、ステンレス製の容器に回収して、液化したトルエン(TOL)等の液状生成物と水素ガス等の気体を気液分離した。回収された液状生成物と気体を各々ガスクロマトグラフィで組成分析を行って、反応開始から140時間後までのMCH転化率(%)とTOL選択率(%)とを算出した。また、反応試験後の触媒を抜き出し、触媒劣化要因であるカーボン生成量を炭素・硫黄分析装置により測定した。
次に上記の比較例3(触媒No.3)及び実施例2(触媒No.6)を用いて次の要領で長時間の触媒安定性を評価する反応試験を実施した。反応管断面の中心に外形1/4インチの熱電対用保護管を備えた内径21.2mm×816mmサイズのステンレス製反応管の長さ方向の中心部に、各触媒8.5gを外径5mmの球状α-アルミナビーズ129gで希釈して充填した。触媒の上側に予熱層として外径1mmの球状α-アルミナビーズを充填した。触媒層温度を380℃に設定し、水素気流下で15時間の条件で前処理還元を行った。前処理還元終了後、触媒層入口温度280℃、触媒層出口温度380℃、反応圧力0.55MPaに設定し、MCHガスを2.8L/h(LHSV:2.6h-1)の流量で反応器に供給した。反応管の出口側には、反応器から出たガスを冷却する冷却器を設け、ステンレス製の容器に回収して、液化したトルエン(TOL)等の液状生成物と水素ガス等の気体を気液分離した。回収された液状生成物と気体を各々ガスクロマトグラフィで組成分析を行って、反応開始から1400時間後までのMCH転化率(%)とTOL選択率(%)を算出した。
不純物生成量=MCH供給量×MCH転化率/100×(100-TOL選択率)/100
2 金属担持部分
Claims (10)
- 均一型白金担持アルミナ触媒であって、
アルミナ担体と、
前記アルミナ担体の断面全体に亘って分散した硫黄又は硫黄化合物と、
前記アルミナ担体の断面全体に亘って分散して担持された白金と、
ナトリウム、カリウム、及びカルシウムの群から選ばれる1種又は2種以上のアルカリ金属を有する均一型白金担持アルミナ触媒。 - 前記白金の含有量が白金元素として0.05以上5.0wt%以下である請求項1に記載の均一型白金担持アルミナ触媒。
- 前記硫黄又は前記硫黄化合物の含有量が硫黄元素として0.15以上5.0wt%以下である請求項1又は請求項2に記載の均一型白金担持アルミナ触媒。
- 前記アルカリ金属の含有量が、アルカリ金属元素として0.1wt%以上5.0wt%以下である請求項1~請求項3のいずれか1つの項に記載の均一型白金担持アルミナ触媒。
- 前記アルミナ担体は、表面積が150m2/g以上、細孔容積が0.40cm3/g以上、平均細孔径が40Å以上300Å以下、及び全細孔容積に対して平均細孔径±30Å以下の細孔が占める割合が60%以上である請求項1~請求項4のいずれか1つの項に記載の均一型白金担持アルミナ触媒。
- 均一型白金担持アルミナ触媒の製造方法であって、
均一型白金担持アルミナ触媒を調製するステップと、
前記均一型白金担持アルミナ触媒にアルカリ金属化合物の水溶液を含浸させ、その後に乾燥させるステップと、
乾燥させた前記均一型白金担持アルミナ触媒を水素雰囲気にて還元する、又は乾燥させた前記均一型白金担持アルミナ触媒を焼成し、その後に水素雰囲気にて還元するステップとを有する均一型白金担持アルミナ触媒の製造方法。 - 請求項1~請求項5のいずれか1つの項に記載された前記均一型白金担持アルミナ触媒を用いて水素化芳香族類を脱水素化する水素化芳香族類の脱水素方法。
- 前記水素化芳香族類が、単環芳香族類の水素化物、2環芳香族類の水素化物、及び3環以上の芳香環を有する化合物の水素化物からなる群から選ばれる1種又は2種以上の混合物である請求項7に記載の水素化芳香族類の脱水素方法。
- 前記水素化芳香族類が、メチルシクロヘキサン、シクロヘキサン、ジメチルシクロヘキサン、テトラリン、デカリン、メチルデカリン、ビフェニル、ジフェニルメチル、ジベンゾトリオール、テトラデカヒドロアントラセンからなる群から選ばれる1種又は2種以上の混合物である請求項7に記載の水素化芳香族類の脱水素方法。
- 前記均一型白金担持アルミナ触媒とエッグシェル型白金担持アルミナ触媒との両方を用いて行う請求項7~請求項9のいずれか1つの項に記載の水素化芳香族類の脱水素方法。
Priority Applications (9)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/JP2020/017563 WO2021214954A1 (ja) | 2020-04-23 | 2020-04-23 | 均一型白金担持アルミナ触媒、その製造方法、及びその使用方法 |
EP20932604.0A EP4140579A4 (en) | 2020-04-23 | 2020-04-23 | UNIFORM PLATINUM-SUPPORTED ALUMINUM OXIDE CATALYST, METHOD FOR PRODUCING THEREOF AND METHOD FOR USE THEREOF |
CN202080099971.XA CN115485064A (zh) | 2020-04-23 | 2020-04-23 | 均匀型载铂氧化铝催化剂、其制备方法及其使用方法 |
KR1020227040509A KR20230002892A (ko) | 2020-04-23 | 2020-04-23 | 균일형 백금 담지 알루미나 촉매, 그 제조 방법, 및 그 사용 방법 |
CA3175486A CA3175486A1 (en) | 2020-04-23 | 2020-04-23 | Uniform-type platinum-loaded alumina catalyst, method of producing same, and method of using same |
US17/918,591 US20230141512A1 (en) | 2020-04-23 | 2020-04-23 | Uniform-type platinum-loaded alumina catalyst, method of producing same, and method of using same |
AU2020443710A AU2020443710A1 (en) | 2020-04-23 | 2020-04-23 | Uniform platinum-supported alumina catalyst, method for producing same, and method for using same |
JP2022516774A JPWO2021214954A1 (ja) | 2020-04-23 | 2020-04-23 | |
TW110114570A TWI803856B (zh) | 2020-04-23 | 2021-04-22 | 均相型鉑載持氧化鋁觸媒、其製造方法、及其使用方法 |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/JP2020/017563 WO2021214954A1 (ja) | 2020-04-23 | 2020-04-23 | 均一型白金担持アルミナ触媒、その製造方法、及びその使用方法 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2021214954A1 true WO2021214954A1 (ja) | 2021-10-28 |
Family
ID=78270692
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2020/017563 WO2021214954A1 (ja) | 2020-04-23 | 2020-04-23 | 均一型白金担持アルミナ触媒、その製造方法、及びその使用方法 |
Country Status (9)
Country | Link |
---|---|
US (1) | US20230141512A1 (ja) |
EP (1) | EP4140579A4 (ja) |
JP (1) | JPWO2021214954A1 (ja) |
KR (1) | KR20230002892A (ja) |
CN (1) | CN115485064A (ja) |
AU (1) | AU2020443710A1 (ja) |
CA (1) | CA3175486A1 (ja) |
TW (1) | TWI803856B (ja) |
WO (1) | WO2021214954A1 (ja) |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2006052110A (ja) * | 2004-08-12 | 2006-02-23 | Chiyoda Corp | 水素の精製方法 |
JP2008050338A (ja) * | 2006-08-22 | 2008-03-06 | Hyosung Corp | 金属触媒を用いたジメチルナフタレンの製造方法 |
JP4142733B2 (ja) | 2005-06-20 | 2008-09-03 | 千代田化工建設株式会社 | 均一型高分散金属触媒及びその製造方法 |
JP4652695B2 (ja) | 2004-01-30 | 2011-03-16 | 千代田化工建設株式会社 | 水素化芳香族類の脱水素触媒及びその製造方法 |
JP2012206909A (ja) * | 2011-03-30 | 2012-10-25 | Chiyoda Kako Kensetsu Kk | ハイブリッド型水素製造・発電システム |
CN106693993A (zh) * | 2016-12-21 | 2017-05-24 | 北京赛诺时飞石化科技有限公司 | 一种含硫型低碳烷烃脱氢催化剂及制备方法 |
CN110882703A (zh) * | 2019-12-03 | 2020-03-17 | 北京赛诺时飞石化科技有限公司 | 一种含碱土金属的环烷烃脱氢催化剂及其制备方法 |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2019730A4 (en) * | 2006-05-02 | 2010-12-22 | Reliance Ind Ltd | OXIDATION CATALYZER FOR CLEANING NITROGEN GAS CONTAINING ORGANIC CONTAMINATION |
CN105268459B (zh) * | 2014-07-21 | 2018-02-23 | 中国石油化工股份有限公司 | 一种含硫的低碳烷烃脱氢催化剂及其制备方法 |
CN105363446B (zh) * | 2014-08-25 | 2019-06-14 | 中国石油化工股份有限公司 | 一种石脑油重整催化剂及制备方法 |
-
2020
- 2020-04-23 CA CA3175486A patent/CA3175486A1/en active Pending
- 2020-04-23 JP JP2022516774A patent/JPWO2021214954A1/ja active Pending
- 2020-04-23 AU AU2020443710A patent/AU2020443710A1/en active Pending
- 2020-04-23 CN CN202080099971.XA patent/CN115485064A/zh active Pending
- 2020-04-23 KR KR1020227040509A patent/KR20230002892A/ko unknown
- 2020-04-23 EP EP20932604.0A patent/EP4140579A4/en active Pending
- 2020-04-23 US US17/918,591 patent/US20230141512A1/en active Pending
- 2020-04-23 WO PCT/JP2020/017563 patent/WO2021214954A1/ja unknown
-
2021
- 2021-04-22 TW TW110114570A patent/TWI803856B/zh active
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP4652695B2 (ja) | 2004-01-30 | 2011-03-16 | 千代田化工建設株式会社 | 水素化芳香族類の脱水素触媒及びその製造方法 |
JP2006052110A (ja) * | 2004-08-12 | 2006-02-23 | Chiyoda Corp | 水素の精製方法 |
JP4142733B2 (ja) | 2005-06-20 | 2008-09-03 | 千代田化工建設株式会社 | 均一型高分散金属触媒及びその製造方法 |
JP2008050338A (ja) * | 2006-08-22 | 2008-03-06 | Hyosung Corp | 金属触媒を用いたジメチルナフタレンの製造方法 |
JP2012206909A (ja) * | 2011-03-30 | 2012-10-25 | Chiyoda Kako Kensetsu Kk | ハイブリッド型水素製造・発電システム |
CN106693993A (zh) * | 2016-12-21 | 2017-05-24 | 北京赛诺时飞石化科技有限公司 | 一种含硫型低碳烷烃脱氢催化剂及制备方法 |
CN110882703A (zh) * | 2019-12-03 | 2020-03-17 | 北京赛诺时飞石化科技有限公司 | 一种含碱土金属的环烷烃脱氢催化剂及其制备方法 |
Non-Patent Citations (4)
Title |
---|
"Agency for Natural Resources and Energy", HYDROGEN BASIC STRATEGY, December 2017 (2017-12-01) |
OKADA YOSHIMI, BULLETIN OF THE HIGH PRESSURE GAS SAFETY INSTITUTE OF TOKYO, August 2019 (2019-08-01) |
OKADA YOSHIMI, ENERGY/NATURAL RESOURCES, vol. 33, no. 3, 2018, pages 168 |
See also references of EP4140579A4 |
Also Published As
Publication number | Publication date |
---|---|
EP4140579A1 (en) | 2023-03-01 |
CN115485064A (zh) | 2022-12-16 |
AU2020443710A1 (en) | 2022-12-08 |
CA3175486A1 (en) | 2021-10-28 |
TW202144075A (zh) | 2021-12-01 |
KR20230002892A (ko) | 2023-01-05 |
US20230141512A1 (en) | 2023-05-11 |
TWI803856B (zh) | 2023-06-01 |
JPWO2021214954A1 (ja) | 2021-10-28 |
EP4140579A4 (en) | 2024-02-28 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US6573214B2 (en) | Preferential oxidation catalyst | |
JP4907210B2 (ja) | 水素の貯蔵輸送システム | |
CN110327933B (zh) | 二氧化碳加氢制备甲醇的催化剂及其制备方法和应用 | |
CN109999820A (zh) | 一种用于氢化石油树脂制备的镍基催化剂及其制备方法与应用 | |
TW202243989A (zh) | 加氫站及氫生成方法 | |
CN109759073B (zh) | 一种中低温煤焦油加氢脱氧催化剂及其制备和应用 | |
KR20210057926A (ko) | 액상화합물 기반 수소저장용 탈수소화 반응 촉매 및 그 제조방법 | |
Liu et al. | Highly dispersed Ni–Fe alloy catalysts on MgAl2O4 derived from hydrotalcite for direct ethanol synthesis from syngas | |
WO2021214954A1 (ja) | 均一型白金担持アルミナ触媒、その製造方法、及びその使用方法 | |
WO2021214955A1 (ja) | エッグシェル型白金担持アルミナ触媒、その製造方法、及びその使用方法 | |
TWI831153B (zh) | 鉑載持氧化鋁觸媒及其製造方法、以及使用該觸媒之氫化芳香族類之去氫方法 | |
CN113952957A (zh) | 镍系加氢催化剂及其制备方法和应用 | |
JP5948657B2 (ja) | 水素製造方法 | |
Garidzirai | Dehydrogenation of perhydrodibenzyltoluene for hydrogen production: the effect of Mg and Zn dopants on the catalytic activity of Pt/Al₂O₃ | |
JP5351089B2 (ja) | 水蒸気改質用触媒、水素製造装置および燃料電池システム | |
Chen et al. | Effect of Particle Size of Regeneration Pt-Al2o3 Catalysts on Methylcyclohexane Dehydrogenation | |
CN117282443A (zh) | 环烷烃类储氢剂深度脱氢过程催化剂及其制备方法 | |
CN113507985A (zh) | 包括在预浸渍中形成Ni-Cu合金的步骤的制备用于芳族化合物的氢化的催化剂的方法 | |
JP2001270705A (ja) | 炭化水素の水蒸気改質方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 20932604 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 2022516774 Country of ref document: JP Kind code of ref document: A |
|
ENP | Entry into the national phase |
Ref document number: 3175486 Country of ref document: CA |
|
ENP | Entry into the national phase |
Ref document number: 20227040509 Country of ref document: KR Kind code of ref document: A |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
ENP | Entry into the national phase |
Ref document number: 2020932604 Country of ref document: EP Effective date: 20221123 |
|
ENP | Entry into the national phase |
Ref document number: 2020443710 Country of ref document: AU Date of ref document: 20200423 Kind code of ref document: A |