EP2683479A1 - Hydrocracking catalysts containing stabilized aggregates of small crystallites of zeolite y and associated hydrocarbon conversion processes - Google Patents
Hydrocracking catalysts containing stabilized aggregates of small crystallites of zeolite y and associated hydrocarbon conversion processesInfo
- Publication number
- EP2683479A1 EP2683479A1 EP12755532.4A EP12755532A EP2683479A1 EP 2683479 A1 EP2683479 A1 EP 2683479A1 EP 12755532 A EP12755532 A EP 12755532A EP 2683479 A1 EP2683479 A1 EP 2683479A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- zeolite
- catalyst
- secondary particles
- hydrocracking catalyst
- aggregated
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 215
- 239000010457 zeolite Substances 0.000 title claims abstract description 146
- 229910021536 Zeolite Inorganic materials 0.000 title claims abstract description 122
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 title claims abstract description 122
- 238000004517 catalytic hydrocracking Methods 0.000 title claims abstract description 114
- 238000000034 method Methods 0.000 title claims abstract description 60
- 230000008569 process Effects 0.000 title claims abstract description 44
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 20
- 229930195733 hydrocarbon Natural products 0.000 title claims description 32
- 150000002430 hydrocarbons Chemical class 0.000 title claims description 32
- 239000004215 Carbon black (E152) Substances 0.000 title claims description 28
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 102
- 239000013078 crystal Substances 0.000 claims abstract description 69
- 239000011163 secondary particle Substances 0.000 claims abstract description 67
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 55
- 239000000463 material Substances 0.000 claims abstract description 41
- 239000000377 silicon dioxide Substances 0.000 claims abstract description 38
- 238000004519 manufacturing process Methods 0.000 claims abstract description 10
- 239000011230 binding agent Substances 0.000 claims description 47
- 229910052751 metal Inorganic materials 0.000 claims description 36
- 239000002184 metal Substances 0.000 claims description 36
- 238000009835 boiling Methods 0.000 claims description 22
- 239000011148 porous material Substances 0.000 claims description 22
- 238000010025 steaming Methods 0.000 claims description 15
- 239000002253 acid Substances 0.000 claims description 14
- 239000002808 molecular sieve Substances 0.000 claims description 12
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 12
- 229910052697 platinum Inorganic materials 0.000 claims description 11
- 229910052783 alkali metal Inorganic materials 0.000 claims description 10
- 150000001340 alkali metals Chemical class 0.000 claims description 10
- 239000007789 gas Substances 0.000 claims description 9
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 8
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 claims description 8
- 229910044991 metal oxide Inorganic materials 0.000 claims description 8
- 150000004706 metal oxides Chemical class 0.000 claims description 8
- 229910052763 palladium Inorganic materials 0.000 claims description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 7
- 229910052750 molybdenum Inorganic materials 0.000 claims description 6
- 229910052759 nickel Inorganic materials 0.000 claims description 6
- 229910052721 tungsten Inorganic materials 0.000 claims description 6
- 150000002739 metals Chemical class 0.000 claims description 5
- 229910052680 mordenite Inorganic materials 0.000 claims description 5
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 claims description 4
- 229910052796 boron Inorganic materials 0.000 claims description 4
- 239000001257 hydrogen Substances 0.000 claims description 4
- 229910052739 hydrogen Inorganic materials 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 4
- ILRRQNADMUWWFW-UHFFFAOYSA-K aluminium phosphate Chemical class O1[Al]2OP1(=O)O2 ILRRQNADMUWWFW-UHFFFAOYSA-K 0.000 claims description 3
- 229910000323 aluminium silicate Inorganic materials 0.000 claims description 3
- 229910001657 ferrierite group Inorganic materials 0.000 claims description 3
- 229920000642 polymer Polymers 0.000 claims description 3
- 229910052727 yttrium Inorganic materials 0.000 claims 2
- 239000003921 oil Substances 0.000 abstract description 10
- 239000000446 fuel Substances 0.000 abstract description 2
- 239000000295 fuel oil Substances 0.000 abstract 1
- 239000000047 product Substances 0.000 description 43
- 239000000203 mixture Substances 0.000 description 41
- 229910001868 water Inorganic materials 0.000 description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 35
- 239000002245 particle Substances 0.000 description 28
- 239000000243 solution Substances 0.000 description 19
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 18
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 17
- 229910052782 aluminium Inorganic materials 0.000 description 17
- 238000011282 treatment Methods 0.000 description 15
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Substances [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 13
- 238000001354 calcination Methods 0.000 description 10
- 230000000052 comparative effect Effects 0.000 description 10
- 238000001878 scanning electron micrograph Methods 0.000 description 10
- 238000003756 stirring Methods 0.000 description 10
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 9
- VXAUWWUXCIMFIM-UHFFFAOYSA-M aluminum;oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Al+3] VXAUWWUXCIMFIM-UHFFFAOYSA-M 0.000 description 9
- 238000009826 distribution Methods 0.000 description 9
- 239000011734 sodium Substances 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical group 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 description 8
- 238000002441 X-ray diffraction Methods 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- 229910052708 sodium Inorganic materials 0.000 description 8
- 238000012360 testing method Methods 0.000 description 8
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 7
- 238000000605 extraction Methods 0.000 description 7
- 229910000510 noble metal Inorganic materials 0.000 description 7
- -1 sulfate aluminum alkoxides Chemical class 0.000 description 7
- 238000002360 preparation method Methods 0.000 description 6
- 230000002776 aggregation Effects 0.000 description 5
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 5
- 239000002585 base Substances 0.000 description 5
- 238000006555 catalytic reaction Methods 0.000 description 5
- 238000003795 desorption Methods 0.000 description 5
- 238000004231 fluid catalytic cracking Methods 0.000 description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 5
- 229910001388 sodium aluminate Inorganic materials 0.000 description 5
- 238000004458 analytical method Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 238000005336 cracking Methods 0.000 description 4
- 238000009792 diffusion process Methods 0.000 description 4
- 239000012013 faujasite Substances 0.000 description 4
- 239000003502 gasoline Substances 0.000 description 4
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000011164 primary particle Substances 0.000 description 4
- 239000011541 reaction mixture Substances 0.000 description 4
- 229910052703 rhodium Inorganic materials 0.000 description 4
- 229910001415 sodium ion Inorganic materials 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 3
- 238000004220 aggregation Methods 0.000 description 3
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical compound [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O ammonium group Chemical group [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 3
- 150000003863 ammonium salts Chemical class 0.000 description 3
- 230000009920 chelation Effects 0.000 description 3
- 230000007547 defect Effects 0.000 description 3
- 238000005342 ion exchange Methods 0.000 description 3
- 235000006408 oxalic acid Nutrition 0.000 description 3
- 230000000737 periodic effect Effects 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 229910052707 ruthenium Inorganic materials 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 238000005054 agglomeration Methods 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 238000004523 catalytic cracking Methods 0.000 description 2
- 229910052804 chromium Inorganic materials 0.000 description 2
- 239000011651 chromium Substances 0.000 description 2
- 239000008367 deionised water Substances 0.000 description 2
- 229910021641 deionized water Inorganic materials 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 229910001683 gmelinite Inorganic materials 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000010348 incorporation Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- POILWHVDKZOXJZ-ARJAWSKDSA-M (z)-4-oxopent-2-en-2-olate Chemical compound C\C([O-])=C\C(C)=O POILWHVDKZOXJZ-ARJAWSKDSA-M 0.000 description 1
- VXEGSRKPIUDPQT-UHFFFAOYSA-N 4-[4-(4-methoxyphenyl)piperazin-1-yl]aniline Chemical compound C1=CC(OC)=CC=C1N1CCN(C=2C=CC(N)=CC=2)CC1 VXEGSRKPIUDPQT-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- QZYDAIMOJUSSFT-UHFFFAOYSA-N [Co].[Ni].[Mo] Chemical compound [Co].[Ni].[Mo] QZYDAIMOJUSSFT-UHFFFAOYSA-N 0.000 description 1
- YCOASTWZYJGKEK-UHFFFAOYSA-N [Co].[Ni].[W] Chemical compound [Co].[Ni].[W] YCOASTWZYJGKEK-UHFFFAOYSA-N 0.000 description 1
- QXLYKLCDAFSZCM-UHFFFAOYSA-N [Mo].[W].[Co] Chemical compound [Mo].[W].[Co] QXLYKLCDAFSZCM-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- 150000004645 aluminates Chemical class 0.000 description 1
- 239000011260 aqueous acid Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- BFGKITSFLPAWGI-UHFFFAOYSA-N chromium(3+) Chemical compound [Cr+3] BFGKITSFLPAWGI-UHFFFAOYSA-N 0.000 description 1
- 101150091051 cit-1 gene Proteins 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- WHDPTDWLEKQKKX-UHFFFAOYSA-N cobalt molybdenum Chemical compound [Co].[Co].[Mo] WHDPTDWLEKQKKX-UHFFFAOYSA-N 0.000 description 1
- JPNWDVUTVSTKMV-UHFFFAOYSA-N cobalt tungsten Chemical compound [Co].[W] JPNWDVUTVSTKMV-UHFFFAOYSA-N 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000008119 colloidal silica Substances 0.000 description 1
- 239000012084 conversion product Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000001066 destructive effect Effects 0.000 description 1
- 238000005906 dihydroxylation reaction Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- 239000000499 gel Substances 0.000 description 1
- 238000003837 high-temperature calcination Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000010335 hydrothermal treatment Methods 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052741 iridium Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000013507 mapping Methods 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 1
- MOWMLACGTDMJRV-UHFFFAOYSA-N nickel tungsten Chemical compound [Ni].[W] MOWMLACGTDMJRV-UHFFFAOYSA-N 0.000 description 1
- 238000000696 nitrogen adsorption--desorption isotherm Methods 0.000 description 1
- 150000002898 organic sulfur compounds Chemical class 0.000 description 1
- 229910052762 osmium Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000011295 pitch Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000013341 scale-up Methods 0.000 description 1
- 239000003079 shale oil Substances 0.000 description 1
- 150000004760 silicates Chemical class 0.000 description 1
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000005049 silicon tetrachloride Substances 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 239000011275 tar sand Substances 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 125000000101 thioether group Chemical group 0.000 description 1
- 238000010555 transalkylation reaction Methods 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/10—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
- B01J29/12—Noble metals
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- 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
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/42—Platinum
-
- 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
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/88—Molybdenum
- B01J23/882—Molybdenum and cobalt
-
- 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
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/88—Molybdenum
- B01J23/883—Molybdenum and nickel
-
- 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
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/888—Tungsten
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/10—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
- B01J29/12—Noble metals
- B01J29/123—X-type faujasite
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/10—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
- B01J29/12—Noble metals
- B01J29/126—Y-type faujasite
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/16—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/16—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J29/166—Y-type faujasite
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/80—Mixtures of different zeolites
-
- B01J35/30—
-
- B01J35/40—
-
- B01J35/51—
-
- B01J35/613—
-
- B01J35/615—
-
- B01J35/647—
-
- B01J35/69—
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
- B01J37/0027—Powdering
- B01J37/0045—Drying a slurry, e.g. spray drying
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
- B01J37/0063—Granulating
-
- 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
- B01J37/0207—Pretreatment of the support
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
- C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
- C10G47/12—Inorganic carriers
- C10G47/16—Crystalline alumino-silicate carriers
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
- C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
- C10G47/12—Inorganic carriers
- C10G47/16—Crystalline alumino-silicate carriers
- C10G47/18—Crystalline alumino-silicate carriers the catalyst containing platinum group metals or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
- C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
- C10G47/12—Inorganic carriers
- C10G47/16—Crystalline alumino-silicate carriers
- C10G47/20—Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
- C10L1/08—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/36—Steaming
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/42—Addition of matrix or binder particles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/084—Y-type faujasite
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/60—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the type L, as exemplified by patent document US3216789
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/65—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the ferrierite type, e.g. types ZSM-21, ZSM-35 or ZSM-38, as exemplified by patent documents US4046859, US4016245 and US4046859, respectively
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/7026—MFS-type, e.g. ZSM-57
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/82—Phosphates
- B01J29/84—Aluminophosphates containing other elements, e.g. metals, boron
- B01J29/85—Silicoaluminophosphates (SAPO compounds)
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1048—Middle distillates
- C10G2300/1059—Gasoil having a boiling range of about 330 - 427 °C
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/301—Boiling range
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
Definitions
- This invention relates to hydrocracking catalysts containing stabilized aggregates of small crystallites of zeolite Y and hydrocarbon conversion processes utilizing such catalysts.
- Small primary crystallites of zeolite Y can cluster into larger secondary particles, at least 80% of which may comprise at least 5 primary crystallites.
- the average size (width/diameter) of the primary crystallites may be about 0.5 iim or less, or about 0.3 micron or less, though the average size of the secondary particles may be about 0.8 ⁇ or more, or about 1.0 ⁇ or more.
- the silica to alumina ratio of the resulting stabilize zeolite Y products may be 4: 1 or more.
- Methods for stabilizing the aggregates of Y crystals as well as the catalyst synthesis using the aggregated stabilized Y crystals herein are also disclosed. Catalysts and the use of such catalysts in processes for hydrocracking of hydrocarbon feedstocks are also disclosed herein.
- Zeolite Y a member of the Faujasite family, is widely used in many catalytic processes such as fluid catalytic cracking (FCC), hydrocracking, aromatics alkylation, and aromatics transalkylation.
- FCC fluid catalytic cracking
- A. particular type of zeolite Y is known as ultra-stable Y zeolite (USY).
- USY ultra-stable Y zeolite
- Typical USY has crystal morphology of non-aggregated and submicrosized crystals and may contain intra-crystal mesopores after post-treatment involving high temperature steaming.
- the individual submicrosized crystals may have crystal defects which produce variously oriented crystal grains within an individual crystal particle.
- U.S. Patent No. 6,284,21 8 states that such defects include stacking faults and screw defects.
- U.S. Patent No. 5,620,590 reports that small crystal zeolite Y of less than 1 micron shows activity benefit in hydrocracking compared to larger crystals.
- small crystal zeolites often present problems in manufacturing (e.g., difficulties in filtration and formulation) due to their small particle sizes and low bulk density.
- one ideal zeolite morphology includes large secondary particles (often greater than 1 micron) formed by agglomeration of smaller primar crystallites (often less than, or even much less than, 1 micron). Furthermore, to improve mass transportation rates, zeolite crystals with small size or aggregated crystals containing inter-crystal mesopores can be desirable, e.g., for reducing diffusion limitations.
- Conventional zeolite Y tends to have a crystal or primary crystallite size of much greater than 0.1 um, even greater than 1 ⁇
- Examples of such conventional forms of zeolite Y include U.S. Patent Nos. 3,343,913, 3,690,823, and 3,808,326, for example.
- Small crystal size zeolite Y may be prepared by methods disclosed in U.S. Patent Nos. 3,516,786 and 3,864,282.
- Zeolite X, zeolite Y, and natural faujasite have identical structure types and differ only in the ratio of silica to alumina in the final crystal structure.
- zeolite X is generally referred to as having a Si/AU molar ratio of 2-3
- zeolite Y is generally referred to as having a Si/Al? molar ratio of 3-7.
- U.S. Patent Nos. 5,993,773 and 6,306,363 describe various forms of low-silica faujasite zeolite, referred to as LSX, having silica to alumina molar ratios of 1.9-2.1. These patents include SEM photographs showing LSX zeolite particle size and
- Primary crystallites of zeolites may have their shapes predetermined, depending upon the type of zeolite.
- A-type zeolite tends to have a cubic shape
- faujasite- type zeolite tends to have an octahedral shape or a polyhedral shape developed from a generally spherical shape with some angularity, as shown in Figure 3 of this patent.
- faujasite-type zeolites it is possible for faujasite-type zeolites to have other shapes, such as elongated shapes (e.g., rod-like shapes).
- particle sizes distributions of these particles are roughly symmetric about an average peak maximum.
- a method for obtaining an average particle size from particles having a distribution is described in detail, for example, at pages I to 31 of "Powder Engineering Theory", Shigeo Miwa ed., 1981 , Nikkan Kogyo Shinbun K.K.
- the primary crystaliite size of the faujasite-type zeolite may be described as a number average particle size of the primaiy crystallite particle diameters (observed by SEM) as
- 5,993,773 is said to be characterized not only by high purity, but also a peculiar primary crystallite size distribution, wherein the primary crystallite size of a smaller set of particl es is from 1-8 ⁇ , the primary crystallite size of a larger set of particles is from 5-15 um. and 90% or more of the particles are in the smaller set.
- the right hand portion of Figure 2 of this patent illustrates a large single crystal or primary crystallite having a spherical polyhedral shape with angularity or edges developed.
- a stabilized aggregated form of zeolite Y utilized in the hydrocracking catalysts and associated hydrocarbon conversion processes disclosed herein comprises small primary crystallites and secondary particles of larger size. At least 80%, e.g., at least 90% or at least 95%, of the primary crystallites may be aggregated or clustered to form th e secondary particles.
- the ratio of the average size (wid th/diameter) of the secondary particles to the average size (width/diameter) of the primary crystallites, when the outer (i.e., external) surfaces of the secondary particles are viewed, may be at least 3: 1, for example at least 5: 1 or at least 10: 1.
- the average size of the primary crystallites in a secondary particle may be about 0.5 ⁇ /m or less, for example about 0.3 ⁇ or less, about 0.2 ( um or less, or about 0.1 ⁇ or less, whereas the average size of the secondary particles may be about 0.8 ⁇ or more, for example about 1.0 ⁇ or more or about 2.0 ⁇ or more.
- At least 80%, e.g., at least 90% or at least 95%, of the aggregated secondary particles may comprise at least 5, for example at least 10, primary crystallites.
- the average sizes of the primary crystallites and secondary particles can be determined, for instance, by viewing one or more sufficient two-dimensional SEM images of the secondary particles and approximating the shape of the primary crystallites and secondary particles roughly as two-dimensional spherical projections (circles).
- percentages e.g., 80%, 90%, 95%, or the like
- percentages are based on numbers of these particles.
- SEM images referred to herein do not necessarily depict all of the particles in an entire batch of primary crystallites and secondary particles, it should also be understood that the SEM images referred to herein are viewed as representative of an entire batch of primary crystal lites and secondary particles, including even those particles not specifically observed.
- the aggregates of zeolite Y of the present invention can have enhanced stability, particularly enhanced thermal and/or hydrothermal stability, relative to the as- synthesized forms of these aggregates.
- the present stabilized aggregates of zeolite Y which can advantageously have an alkali metal content less than 4 wt%, can further have different chemical compositions than the as-synthesized forms of these aggregates, which can typically comprise as much as 8 wt% or more alkali metal content.
- aggregates of zeolite Y may attain increased stability through one or more of the following treatments: by exchanging alkali metal (e.g., sodium) atoms from the as-synthesized form of the aggregates with an ammonium salt and by calcining the ammonium exchanged aggregates under conditions sufficient to decompose ammonium; by steaming the calcined, ammonium exchanged form of the aggregates under steaming conditions sufficient, e.g., to remove framework aluminum from the zeolite Y crystallites; and/or by contacting (washing) steamed aggregates with an aqueous acid, e.g., to remove non- framework aluminum from the zeolite Y aggregates.
- alkali metal e.g., sodium
- the aggregates of zeolite Y herein are incorporated into a catalyst by the use of a suitable binder material or mixtures of suitable binder materials.
- suitable binder materials include materials selected from metal oxides, zeolites, aluminum phosphates, polymers, carbons, and clays.
- the binder is comprised of at least one metal oxide, preferably selected from silica, alumina, silica- alumina, amorphous aluminosilicates, boron, titania, and zirconia.
- the binder is selected from silica, alumina, and silica-alumina.
- the binder is comprised of pseudoboehmite alumina.
- a significant advantage of the present invention over the prior art is that in the prior art, the zeolite crystals typically require a significant amount of binder material in order to get obtain sufficient mesoporositv which is defined herein as pore diameters from 2 to 30 nm (20 to 300 angstroms, A) for optimum hydrocracking of hydrocarbon feedstocks.
- the zeolite is aggregated into a structure containing a high relative mesoporosity and as such, the hydrocracking catalyst can made with very low concentration levels of binders and still mai tain the necessary overall mesoporositv of the hydrocracking catalyst.
- the catalysts of invention can contain from 0 to 99 wt% binder materials, due to the high mesoporosity of the aggregate Y zeolite, in preferred embodiments, the binders levels can be about 0 to about 80 wt%, more preferably, from about 5 to 50 wt%, or even from about 5 to about 25 wt% of the overall final hydrocracking catalyst. In other preferred embodiments, the hydrocracking catalyst can be less than 50 wt%, more preferably less than 25 wt%, and most preferably less than 10 wt% binder materials. As noted, in embodiments, the aggregated Y zeolites of the present invention may be used as the final catalyst without any binder materials.
- the high relative mesoporosity of the catalysts of invention are indicated by the high Relative External Surface Areas of the catalysts.
- the Relative External Surface Area is defined herein as:
- the catalyst has a Relative External Surface Area of at least 0.35, more preferably at least 0.50.
- the catalyst has a low BET surface area of less than 600 m7g; more preferably less than 500 m /g, and most preferably less than 450 m7g.
- the average pore diameter of the catalyst is at least 7.0 nanometers (nm), preferably at least 7.5 nm, more preferably at least 8,0 nm, and most preferably at least 9.0 nm.
- the catalyst may contain additional zeolites or molecular sieves.
- the catalyst further comprises at least one of the following molecular sieves: beta, ZSM-5, ZSM-1 1 , ZSM-57, MCM-22, MCM-49, MCM-56, ITQ-7, ITQ-27, ZSM-48, mordenite, zeolite L, ferrierite, ZSM-23, MCM-68, SSZ-26/-33, CIT-1 , SAPO-37, ZSM-12, ZSM-18, and EMT faujasites.
- the catalyst comprises at least one of the following molecular sieves: beta, ZSM-5, ZSM-48, mordenite, and zeolite L.
- the molecular sieves listed above can be present in the as-synthesized form, or alternatively, can be post-modified chemically, thermally, or mechanically to create a stabilized form of the material.
- the aggregates of zeolite Y, binder and additional components may be extruded, spray dried, or otherwise shaped into a catalyst particle for use in
- the final catalyst contains an active Group VIA and/or Group VIIIA metal.
- the hydrocracking catalyst is comprised of at least one Group VIA metal selected from Mo and W, and at least one Group V I IIA metal selected from Ni and Co.
- the hydrocracking catalyst is comprised at least one Group VIIIA metal selected from Pt, Pd, Rh. and Ru.
- the hydrocracking catalyst is comprised at least one Group VI HA metal selected from Pt and Pd.
- the Group VIA metal is Mo and the Group VIIIA metal is Co.
- the hydrocracking catalyst is comprised of at least one Group VIA metal selected from Mo and W, and at least one Group V I IIA metal selected from Ni and Co.
- the hydrocracking catalyst is comprised at least one Group VIIIA metal selected from Pt, Pd, Rh. and Ru.
- the hydrocracking catalyst is comprised at least one Group VI HA metal selected from Pt and Pd.
- the Group VIA metal is Mo and the Group VIIIA metal is Co.
- hydrocracking catalyst is comprised of Pt.
- the active Group VIA or Group VIIIA metals may be incorporated into the catalyst by any technique known in the art.
- a preferred technique for active metal incorporation into the catalyst herein is the incipient wetness technique.
- Figures 1A & I B show scanning electron microscope (SEM) images of comparative non-aggregated NaY samples prepared according to Examples 1A & IB,
- Figure 2 shows a scanning electron microscope (SEM) image of a sample comprising a mixture of aggregated & non-aggregated NaY prepared according to Example 2,
- Figure 3 shows a scanning electron microscope (SEM) image of a highly aggregated NaY ' sample prepared according to Example 3 ,
- Figure 4 shows a scanning electron microscope (SEM) image of a highly aggregated NaY sample prepared according to Example 4.
- Figure 5 shows a plot of pore size distributions based on BJH Desorption from N2 BET analysis of samples: calcined at ⁇ 600°C, steamed treated at ⁇ 600°C, and steam treated at ⁇ 700°C, as prepared according to Example 4,
- Figure 6 shows XRD patterns of samples prepared according to Example 5.
- Figure 7 depicts a plot of pore size distributions based on BJH Desorption from N2 BET analysis of samples prepared according to Examples 7A-B.
- Figure 8 depicts a plot showing hydrocracking diesel product yields comparing two (2) embodiments of hydrocracking catalysts containing the aggregated Y zeolites of the present invention as compared to four (4) comparative hydrocracking catalysts containing USY zeolites of the prior art per Example 8A-B,
- Figure 9 depicts a plot showing the selectivity of the diesel product yields of two (2) embodiments of hydrocracking catalysts containing the aggregated Y zeolites of the present invention as compared to four (4) comparative hydrocracking catalysts containing USY zeolites of the prior art per Example 8A-B, DETAILED DESCRIPTION OF THE EMBODIMENTS
- Smaller crystallites of zeolite Y can be clustered into discrete, larger particle size bodies.
- the smaller particle size crystallites are also referred to herein as primary crystallites or primary particles.
- the clusters of these primary crystallites are also referred to herein as secondary particles, aggregates, and/or agglomerates.
- the zeolite Y can alternately be described as esoporous-Y (Meso-Y).
- the secondary particles may be essentially uniform in size. For instance, at least 80%, e.g., at least 90% or at least 95%, of the sizes of the secondary particles may vary on average by no more than -0.5 micron, for example no more than -0.3 micron or no more than - ⁇ .1 micron, as observed by SEM, measuring average diameters as approximated using spherical secondary particulate shapes.
- the secondary particles may be essentially spherical in shape.
- at least 80%, e.g., at least 90% or at least 95%, of the secondary particles may have an aspect ratio of between 0.7 and 1 , for exampl e, between 0.8 and 1 .
- Aspect ratio may be calculated by dividing the shortest cross-sectional dimension of a secondary particle by the longest cross-sectional dimension of the secondary particle, as observed by SEM.
- the secondary particles may appear as clusters of primary particles, having a broccoli-like morphology/appearance.
- the primary crystallites may have a non-spherical shape.
- the primary crystallites may have a smooth or roughened octahedral shape, which is more or less typical of certain faujasite type zeolite crystals.
- the primary crystallites may have other less common shapes, such as elongated or rod-like shapes.
- the secondary particles of the present invention may possess or lack primary crystallites in the interior regions of the secondary particles, which cannot be observed by SEM.
- some or ail of the primary crystallites may or may not be elongated along an axis extending from the center of the secondary particles to the center of the surface of each crystallite, as observed using SEM.
- the secondary particles may possess an external surface area of about 10 m 7g or more, for example, about 20 m /g or more or about 40 m 2 /g or more, especially after undergoing calcination and/or steaming.
- Conventional forms of zeolite Y such as those having non-aggregated primary crystallites with a size of 1 micron or more, tend to have an external surface area of less than 10 m ' Vg.
- the relatively high external surface area of the secondary particles can be an indication generally of porous gaps between individual primary crystallites, and specifically of mesopores in the internal regions of the secondary particles.
- a single crystal of comparable size in the form of a generally spherical shape (with angularity or edges developed) would be expected to have a smaller external surface area.
- the centers of the secondary particles may, in certain cases, be less dense than the ed ges of the secondary particles, as measured by SEM or TEM. This lack of density in the centers of the secondary particles can be a further indication that these secondary particles are indeed an aggregation of primary crystallites, rather than a single large crystal.
- Elemental mapping of secondary particles may reveal that the Si/Al. ratio can be relatively uniform throughout the secondary particles. Such a uniform Si/Al ratio can provide further indication that these secondary particles are indeed an aggregation of primary crystallites, rather than a single large crystal or large particles with an aluminum-, or a silicon-, rich (amorphous) core.
- the zeolite Y in the aggregates may have a silica-to-alumina (Si/Al?) ratio of at least 4 (i.e., at least 4: 1), for example of at least 4.5, of at least 5, or from 5 to 6.
- the aggregated zeolite Y has a silica-to-alumina (Si/Al 2 ) ratio of at least 10, more preferably, at least 25, and even more preferably at least 50.
- the aggregated form of zeolite Y may have a mesopore volume of at least 0.025 cm gram (abbreviated cc/g herein), particularly in the inter-crystalline regions of the aggregates.
- Non-aggregated forms of zeolite Y thus tend to lack mesopores (which are defined herein as pores having a diameter from about 20 to about 300 Angstroms).
- the unit cell size (IJCS) of the zeolite Y can be 25 Angstroms or less, e.g., between 24 and 25 Angstroms.
- Small size zeolite Y can be prepared using a reaction mixture containing a source of alumina, a source of silica, a source of sodium ions, a source of water, and optionally a source of hydroxy! ions.
- the reaction mixture is described as containing sources of alumina and silica, it should be understood that these are actually sources of aluminum atoms and silicon atoms, respectively.
- the zeolite Y structure is usually described in terms of oxidized versions of these atoms, and indeed to facilitate the standard characterization of such zeolitic structures with respect to ratios of silica to alumina, and the like, the sources are referred to herein for convenience in their oxidized forms.
- Sources of alumina for preparing aggregates of small size zeolite Y can be in the form of a soluble salt, for example a sodium salt of alumina, e.g. sodium aluminate, such as commercially available from US Aluminate.
- alumina sources can additionally or alternately include other aluminum salts, such as the chloride, sulfate aluminum alkoxides, hydrated aluminas such as gamma alumina, pseudoboehmite, and colloidal alumina, and the like, and combinations thereof.
- the silica source for preparing aggregates of small size zeolite Y can be a precipitated silica, such as Ultrasil®, which is commercially available from Evonik Degussa.
- Other suitable silica sources can additionally or alternately include powdered silica (including precipitated silica, such as Ultrasil PM Modified® and/or Zeosil®, as well as silica gels), silicic acid, colloidal silica (such as Ludox®), dissolved silica, and the like, and combinations thereof.
- certain silica sources may form silicates.
- a sodium si licate solution can further additionally or alternately be used as a source of silica.
- a precipitated silica particularly Ultrasil PM
- Modified®, Ultrasil®, and/or Sipemat® can be used as a source of silica.
- the reaction mixture for forming the aggregates of small size zeolite Y can comprise one or more of a Si/Al 2 molar ratio of about 10 or more, an H 2 0/Si molar ratio of about 15 or less, and an OHVSi molar ratio of about 0.85 or less.
- the reaction mixture for forming the aggregates of small size zeolite Y may comprise one or more of a silica to alumina molar ratio from about 10 to about 20, an H 2 0/Si0 2 molar ratio from about 10 to about 20, when hydroxyl ion sources are present an OH7Si0 2 molar ratio from about 0.5 to about 1.0, and a NaV ' SiC molar ratio from about 0.5 to about 1.0.
- the thermal and hydrothermal stability of the aggregates of zeolite Y can be improved by removal of aluminum from the aggregates, by high temperature steaming. This is illustrated further in Examples 7A-B and 8A-B of the disclosure herein.
- Forms of the present aggregates of zeolite Y may be subjected to other various treatments to remove structural aluminum therefrom. Many of these techniques rely upon the removal of aluminum from the structural framework of the zeolite by chemical agents appropriate to this end.
- a considerable amount of work on the preparation of aluminum-deficient faujasites has been performed and is reviewed in Advances in Chemistry Series No. 121, Molecular Sieves, G. T. Kerr, American Chemical Society, 1973, Specific methods for preparing dealumimzed zeolites are described in the following, and reference is made to them for details of the method, which are hereby incorporated by reference herein: Catalysis by Zeolites ((International Symposium on Zeolites, Lyon, Sept.
- zeolite Y may be prepared by steaming and/or by acid extraction of structural aluminum, but, because zeolite Y in its usual as-synthesized condition tends to be relatively unstable to acid, it must first be converted to an acid-stable form. Methods for doing this are known, and one of the most common forms of acid- resistant zeolite Y is known as "Uitrastable Y" (USY), e.g., as described in U.S. Patent Nos. 3,293,192 and 3,402,996 and in Society of Chemical Engineering (London)
- zeolite Monograph Molecular Sieves, page 186 (1968), by C. V. McDaniel and P. K. Maher, each of which are hereby incorporated by reference herein for details of the zeolite and preparation, in general, "uitrastable” refers to Y-type zeolite that is highly resistant to degradation of crystallinity by high temperature and steam treatment and that can be characterized by an R 2 Q content (wherein R is Na, K, or any other Group 1 metal ion) of less than 4 wt% (for example less than 2 wt%, preferably less than 1 wt%), a unit ceil size less than 24.5 Angstroms, and a silica to alumina mole ratio in the range of 3.5 to 7 or higher.
- R 2 Q content wherein R is Na, K, or any other Group 1 metal ion
- the ultrastabie form of Y-type zeolite can be obtained primarily by a substantial reduction of the alkali metal (Group 1) ion content and of the unit cell size.
- the ultrastabie zeolite Y can be identified both by the smal ler unit cell and the low alkali metal content in the crystal structure.
- the ultrastabie form of the Y-type zeolite can be prepared by successively base exchanging a Y-type zeolite with an aqueous solution of an ammonium salt, such as ammonium nitrate, until the alkali metal content of the Y-type zeolite is reduced to less than 4 wt%.
- an ammonium salt such as ammonium nitrate
- the base exchanged zeolite can then be calcined at appropriate conditions (e.g., at a temperature from about 540°C to about 800°C for up to several hours), cooled, and successively base exchanged again with, an aqueous solution of an ammonium salt until the alkali metal content is reduced to less than ⁇ 1 wt% (e.g., less than -0.5 wt%), which can be followed by washing and calcination again at appropriate conditions to produce an ultrastabie zeolite Y.
- appropriate conditions e.g., at a temperature from about 540°C to about 800°C for up to several hours
- an aqueous solution of an ammonium salt until the alkali metal content is reduced to less than ⁇ 1 wt% (e.g., less than -0.5 wt%), which can be followed by washing and calcination again at appropriate conditions to produce an ultrastabie zeolite Y.
- the sequence of ion exchange and heat treatment can result in the substantial reduction of the alkali metal content of the original zeolite and can also advantageously result in a unit cell shrinkage, which is believed to lead to the rather high stability of the resulting Y-type zeolite.
- the ultrastabie zeolite Y may then be extracted, e.g., with acid to remove extra- framework aluminum containing species, to produce a highly siliceous form of the zeolite.
- acid to remove extra- framework aluminum containing species
- Methods for increasing the silica to alumina ratio of zeolite Y by acid extraction are described, e.g., in U.S. Patent Nos. 4,218,307, 3,591 ,488, and 3,691 ,099, which are each incorporated herein by reference for details of these methods,
- the aggregated Y zeolite (“Meso-Y”) zeolites herein may be used as catalysts without the use of any binder materials or with, the use of very low amounts of binders materials as compared to the prior art.
- This is mainly due to the fact that the aggregation of the crystal structures in the Meso-Y zeolite impart into the base Meso-Y zeolite aggregated crystal (i.e., catalyst as zeolite alone) with sufficient mesoporosity as to not require any, or conversely, very low amounts, of binder materials as it is know that the binder materials tend impart most of the mesoporosity required for a high activity, selective hydrocracking catalyst.
- the aggregates of zeolite Y herein are incorporated into a catalyst by the use of a suitable binder material.
- suitable binder materials include materials selected from metal oxides, zeolites, aluminum phosphates, polymers, carbons, and clays.
- the binder is comprised of at least one metal oxide, preferably selected from silica, alumina, silica-alumina, amorphous aluminosilicates, boron, titania, and zirconia.
- the binder is selected from silica, alumina, and silica-alumina, in a preferred embodiment, the binder is comprised of pseudoboehmite alumina.
- the catalysts of invention can contain from 0 to 99 wt% binder materials, due to the high mesoporosity of the aggregate Y zeolite, in preferred embodiments, the binders levels can be about 0 to about 80 wt%, more preferably, from about 5 to 50 wt%, or even from about 5 to about 25 wt% of the overall final hydrocracking catalyst. In other preferred embodiments, the hydrocracking catalyst can be less than 50 wt%, more preferably less than 25 wt%, and most preferably less than 10 wt% binder materials. As noted, in embodiments, the aggregated Y zeolites of the present invention may be used as the final catalyst without any binder materials.
- versions of the Meso-Y with relatively high silica-to-alumina (S1/AI 2 ) ratio are utilized (i.e., ranges wherein the silica-to-alumina (Si/Ah) ratio of the Meso-Y is in ranges stated encompassing at least 10 or greater (e.g., at least 10, or 25, or 50).
- a significant advantage of the present invention over the prior art is that in the prior art, the zeolite crystals typically require a significant amount of binder material in order to get obtain sufficient meso porosity which is defined herein as pore diameters from 2 to 30 nm (20 to 300 angstroms, A) for optimum hydrocracking of hydrocarbon feedstocks, in the present invention, the zeolite is aggregated into a structure containing a high relative mesoporosity and as such, the hydrocracking catalyst can made with very low concentration l evels of binders and still maintain th e necessary overall mesoporosity of the hydrocracking catalyst.
- the high relative mesoporosity of the catalysts of invention are indicated by the high Rel ative External Surface Areas of the catalysts as noted in equation [1] herein.
- the catalyst has a low BET surface area of less than 600 m g; more preferably less than 500 m7g, and most preferably less than 450 m /g.
- the embodiments of the catalysts of invention (as shown in embodiments MesoY-A and MesoY-B) have very low total surface areas compared to the catalysts of the prior art while maintaining external surface areas near those of the prior art. This contributes to high diesel hydrocracking selectivity.
- the catalyst has a Relative External Surface Areas, as noted in equation [ 1] herein, of at least 0.35, more preferably at least 0.50.
- the catalysts of invention additionally have significantly higher average pore diameters than the conventional USY catalysts. This is indicative of the high
- the average pore diameter of the catalyst is at least 7.0 nanometers (nm), preferably at least 7.5 nm, more preferably at least 8,0 nm, and most preferably at least 9.0 nm.
- This aspect of the catalysts of invention (as exemplified by MesoY-A and MesoY-B) is further exemplified in Examples 8A-B and associated data in Table 3. These catalyst aspects contribute to high diesel selectivity in the catalysts of invention.
- the hydrocracking catalysts of invention are particularly beneficial for diesel production when the catalyst has both a high Relative External Surface Area as noted prior in conjunction with a low Alpha Value as is noted in the catalyst property data associated with Examples 8A-B.
- the Alpha Value for the catalyst is less than 15, more preferably less than 10, and most preferably less than 5,
- the catalyst may contain additional zeolites or molecular sieves.
- the catalyst further comprises at least one of the following zeolites or molecular sieves.
- the catalyst further comprises at least one of the following molecular sieves: beta, ZSM-5, ZSM-11 , ZSM-57, MCM-22, MCM-49, MCM-56, fl Q-7. ITQ-27, Z8M-48, mordenite, zeolite L, ferrierite, ZSM-23, MCM-68, SSZ-26/-33, ClT-1, SAPO-37, ZSM-12, ZSM-18, and EMT faujasites.
- the catalyst comprises at least one of the following molecular sieves: beta, ZSM-5, ZSM-48, mordenite, and zeolite L.
- the molecular sieves listed above can be present in the as-synthesized form, or alternatively, can be post-modified chemically, thermally, or mechanically to create a stabilized form of the material.
- the hydrocracking catalyst of the invention herein contains the Meso-Y zeolite in an amount of at least 10 wt% , more preferably at least at least 25 wt%, and even more preferably at least at least 35 wt% based on the finished catalyst, particularly when a binder is utilized.
- the Meso-Y zeolite may be present in hydrocracking catalysts in an amount of at least 50 wt%, or even at least 75 wt%, based on the finished catalyst.
- the aggregates of zeolite Y are combined with at least one metal oxide binder (as described prior) and further with at least one hydrogenating metal component, in order to form a catalyst suitable for hydrocracking.
- hydrogenating metal components can include one or more noble metals or one or more non-noble metals.
- the aggregates of zeolite Y, binder and additional components may be extruded, spray-dried, or otherwise shaped into a catalyst particle for use in
- the final catalyst contains an active Group VIA and/or Group VIIIA metal.
- the hydrocracking catalyst is comprised of at least one Group VIA. metal selected from Mo and W, and at least one Group VIIIA metal selected from Ni and Co.
- the Group VIA metal is Mo and the Group VIIIA. metal is Co.
- the hydrocracking catalyst is comprised at least one Group VIIIA metal selected from Pt, Pd, Rh and Ru (noble metals).
- the hydrocracking catalyst is comprised at least one Group VIIIA metal selected from Pt and Pd.
- the hydrocracking catalyst is comprised of at least one Group VIIIA metal selected from Pt and Pd.
- the hydrocracking catalyst is comprised of Pt.
- the active Group VIA or Group VIIIA metals may be incorporated into the catalyst by any technique known in the art.
- a preferred technique for active metal incorporation into the catalyst herein is the incipient wetness technique.
- Group VIA and Group VIIIA herein corresponds to the older IUPAC designations such as shown in the Periodic Table of Elements, published by the Sargent-Welch Scientific Company, 1979, wherein the Group VIA. elements include the column from the periodic table of elements containing Cr, Mo, and W, and the Group VIIIA elements include the columns from the periodic table of elements containing Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, and Pt.
- the amount of hydrogenation metal in the catalyst can be at least 0.1 wt.% based on catalyst, or at least 0.15 wt%, or at least 0.2 wt%, or at least 0.25 wt%, or at 0.3 wt%, or at least 0.5 wt% based on the catalyst.
- the amount of metal is preferably from 0.1 to 5 wt%, more preferably from 0.2 to 4 wt%, and even more preferably from 0.25 to 3.5 wt%.
- the metal is a combination of a non-noble Group VIIIA non-noble metal with a Group VIA metal
- the combined amount of metal is preferabiy from 0.25 wt% to 40 wt%, more preferably from 0.3 wt% to 35 wt%, and even more preferably from 1 wt% to 25 wt%.
- non-noble metals and non-noble metal combinations utilized in the hydrocracking catalysts herein can include chromium, molybdenum, tungsten, cobalt, nickel, and combinations thereof such as cobalt-molybdenum, nickel-molybdenum, nickel-tungsten, cobalt-tungsten, cobalt-nickel-molybdenum, cobalt-nickel-tungsten, nickel-molybdenum-ttmgsten, and cobalt-molybdenum-tungsten.
- Non-noble metal components may be pre-sulfided prior to use by exposure to a sulfur-containing gas (such as hydrogen sulfide) or liquid (such as a sulfur-containing hydrocarbon stream, e.g., derived from crude oil and/or spiked with an appropriate organosulfur compound) at an elevated temperature to convert the oxide form to the corresponding sulfide form of the metal.
- a sulfur-containing gas such as hydrogen sulfide
- liquid such as a sulfur-containing hydrocarbon stream, e.g., derived from crude oil and/or spiked with an appropriate organosulfur compound
- the embodiments of the hydrocracking catalysts described herein incorporating the aggregated Y zeolite are utilized in processes for conversion of heavy hydrocarbon feedstocks into lighter, more valuable hydrocarbon products (such, as gasoline, kerosene, and diesel products).
- the catalysts herein have been unexpectedly found to possess very high selectivities toward diesel production (i.e., increased yield volumes) when utilized under hydrocracking conditions.
- increased diesel production is a main focus of refineries in the United States (and even more particularly in the markets of Europe and Asia), as the vehicle pool is ever shifting more toward higher mileage diesel powered vehicles as compared to less efficient gasoline powered engines.
- hydrocracked may include, in whole or in part, a gasoii (e.g., light, medium, heavy, vacuum, and/or atmospheric) having an initial boiling point above about 40Q°F (204°C), a T50 boiling point (i.e., the point at which approximately 50 percent by weight boils, or becomes or is gaseous, under atmospheric pressure) of at least about 500°F (260°C), and an end boiling point of at least about 600°F (315°C).
- a gasoii e.g., light, medium, heavy, vacuum, and/or atmospheric
- T50 boiling point i.e., the point at which approximately 50 percent by weight boils, or becomes or is gaseous, under atmospheric pressure
- hydrocracking catalysts of invention are particularly useful in maximizing diesei production ⁇ 400 T to 700°F boiling range products) from higher boiling point feedstocks.
- the hydrocarbon feedstock contains at least 25 wt%, more preferably at least 50 wt%, and even more preferably, at least 75 wt% hydrocarbons with boiling points above 700°F (371°C).
- it is preferred that the portion the hydrocarbon feedstock boiling above 700°F (371°C) has a T50 boiling point above 800°F (427°C), more preferably above 825°F (441 °C), and most preferably above 850°F (454°C).
- the feedstock can include one or more of thermal oils, residual oils, cycle stocks, whole top crudes, partial crudes, tar sand oils, shale oils, synthetic fuels, heavy hydrocarbon fractions derived from the destructive hydrogenation of coal, tar, pitches, and/or asphalts, hydrotreated feedstocks derived therefrom, and the like.
- the distillation of higher boiling petroleum fractions above about 750°F (399°C) can generally be carried out under vacuum (i.e., at subatmospheric pressure), typically to avoid thermal cracking.
- the boi ling temperatures utilized herein are thus conveniently expressed in terms of the boiling point corrected to atmospheric pressure.
- resid compositions and/or deeper cut gasoils such as with relatively high metals contents, can be cracked using catalysts employing the aggregated zeolite materials of the invention.
- a hydrocarbon feedstock is contacted with embodiments of the Meso-Y-containing hydrocracking catalysts disclosed and described herein under hydrocracking conditions.
- the contacting of the hydrocarbon feedstock with the Meso-Y-containing hydrocracking catalysts is typically performed in a hydrocracker reactor in eth presence of excess hydrogen gas.
- the hydrocracking process may contain one or more reactor stages in series, but most preferably, there is either one or two reactor stages, but each stage may contain one or more reactor vessels. In preferred embodiments of the present invention, there are at least two reactor stages, with the first reactor stage being operated at a total pressure of at least 250 psig, more preferably at least 500 psig, higher than the second reactor stage.
- hydrocraeking process comprises an intermediate vapor separation between the first reactor stage and the second reactor stage in which at least a portion of the hydrogen gas from the first reactor stage effluent is removed.
- at least a portion of the hydrogen gas removed in the intermediate vapor separation step is recycled to the first reactor stage.
- Preferred hydrocracking operating conditions herein include a reaction temperature from about 550°F (about 288°C) to about 800°F (about 427°C); a total pressure from about 300 psig (about 2.1 MPag) to about 3000 psig (about 20.7 MPag), more preferably from about 700 psig (about 4.8 MPag) to about 2500 psig (about 17.2 MPag); an LHSV from about 0.1 hr "1 to about 20 hr "1 , preferably from about 0.2 hr '1 to about 10 hr "1 ; and a hydrogen treat gas rate from about 500 scf/bbl (about 85 Nm ' Vnr 1 ) to about 10000 scf/bbl (about 1700 Nm ' /m " ).
- scf/bbl preferably from about 750 scf/bbl (about 130 Nm ' Vnr) to about 7000 scf/bbl (about 1200 Nrn J /m J ), more preferably from about 1000 scf/bbl (about 170 Nm 3 /m 3 ) to about 5000 scf/bbl (about 850 Nm 3 /m 3 ).
- Examples 7A-B and 8A-B herein show the high diesel selectivity present in the hydrocracking catalyst of the present invention.
- at least 30 wt%, for example at least 35 wt%, or at least 40 wt% of the 700°F feed is converted into diesel boiling range products (i.e., 400 to 7G0°F boiling range hydrocarbons).
- the diesel selectivity i.e., the % diesel product / % 700°F+ conversion
- the formula for calculating diesel selectivity is shown in equation [2] in Examples 8A-B.
- the Alpha values are a measure of the degree of hexane cracking activity in a catalyst, with the higher Alpha values tending to result in higher relative cracking activity (or conversion) in the catalyst.
- the Alpha Value is an approximate indication of the catalytic cracking activity of the catalyst compared to a standard catalyst, and it gives the rel ative rate constant (rate of normal hexane conversion per volume of catalyst per unit time).
- the eso-Y containing hydrocracking catalysts of invention have extremely low Alpha values as can be seen in the catalyst property data shown in Table 3 of Example 8A-B.
- the Alpha values of the MesoY-A and MesoY-B catalysts have alpha values of less than 5 or 10, while the comparative US Y catalysts have alpha values over 20. It is believed that these lower Alpha values contribute to the selective diesel products of the catalysts of the present invention.
- the Alpha values for the catalysts are preferably less than 15, more preferably less than 10, and even more preferably less than 5.
- Comparative Example 1 A Non-aggregated NaY recipe under static conditions
- a mixture was prepared from --885 grams of water, --262 grams of Uitrasil® silica, -150 grams of sodium alurainate solution (45% in water), and -167 grams of 50% sodium hydroxide solution (in w r ater).
- the mixture had the following molar composition:
- the mixture was first aged at room temperature (about 20-25°C) for about 24 hours, while stirring at -250 rpm. Then, the aged mixture was reacted at ⁇ 20G°F ( ⁇ 93°C) in a -2-liter autoclave without stirring for -24 more hours. The product was filtered, washed with deionized (DI) water, and dried at ⁇ 250°F ( ⁇ ! 20°C).
- XRD X-ray diffraction pattern
- the SEM image of the as-synthesized product material sho wed that the material was composed of typical non-aggregated Y crystals, as shown in Figure 1A.
- the as-synthesized Y crystals had a S1O2/AI2O3 molar ratio of -5,0
- a mixture was prepared from -885 grams of water, -262 grams of Ultrasil® silica, -150 grams of sodium aluminate solution (45% in water), and -167 grams of 50% sodium hydroxide solution (in water).
- the mixture had the following molar composition:
- the mixture was first aged at room temperature (about 20-25°C) for about 24 hours, while stirring at -250 rpm. Then, the aged mixture was reacted at -200°F (-93°C) in a ⁇ 2-liter autoclave, while stirring at -250 rpm, for -24 more hours. The product was filtered, washed with deionized (DI) water, and dried at -250°F (- 120°C).
- DI deionized
- XRD X-ray diff action
- the SEM image of the as-synthesized product material showed that the material was composed of typical non -aggregated Y crystals, of the type shown in Figure I B, The as-synthesized Y crystals had a S1O2/AI2O3 molar ratio of -5.12, No major differences in crystal size and morphology were observed compared with product of Comparative Example 1 A based on the SEM data.
- a mixture was prepared from -728 grams of water, --275 grams of Ultrasil® silica, -166 grams of sodium aluminate solution (45% in water), and -120 grams of 50% sodium hydroxide solution (in water).
- the mixture had the following molar composition:
- the mixture was first aged at room temperature (about 20-25°C) for about 24 hours, while stirring at -250 rpm. Then, the aged mixture was reacted at ⁇ 176°F (-80°C) in a -2-liter autoclave, while stirring at -250 rpm, for -192 more hours. The product was filtered, washed with deionized (DI) water, and dried at ⁇ 250°F ( ⁇ 120°C).
- DI deionized
- XRD X-ray diffraction
- the SEM image of the as-synthesized product material showed that the material was composed of aggregates of small crystals and non-aggregated crystals, as shown in Figure 2.
- the as- synthesized Meso-Y crystals had a molar ratio of -5.54 and a unit cell size (UCS) of approximately 24.61 Angstroms.
- a mixture was prepared from -830 grams of water, -258 grams of Ultrasil® si lica, -96 grams of sodium aluminate solution (45% in water), and -180 g of 50% sodium hydroxide solution (in water).
- the mixture had the following molar composition:
- the SEM image of the as-synthesized product material showed that the material was composed of aggregates ( ⁇ 1 micron) of small crystals, as shown in Figure 3.
- the as-synthesized Meso-Y crystals had a Si0 2 / ' A.[ 2 0 3 molar ratio of -5.6 and a unit cell size (UCS) of approximately 24,65 Angstroms.
- One portion of the as- synthesized crystals was ion-exchanged with. -IN ammonium nitrate solution (in water) at room temperature to reduce sodium levels down to - 2 % and was then calcined various temperatures ( ⁇ 600°C and ⁇ 800°C) in air for about 24 hours to stabilize their structures.
- Typical stabilized zeolite Y (USY) products tend to exhibit a very low -40 Angstroms (inter-crystal) pore volume, which can classically be generated/increased either by relatively high temperature calcination or steaming treatments (intra-crystal mesoporosity may additionally be generated/ ncreased by such treatments).
- intra-crystal mesoporosity may additionally be generated/ ncreased by such treatments.
- a relatively high intensity of existing mesoporosity on Meso-Y crystals prior to steam treatment was observed after calcination at ⁇ 600°C or above.
- an increase of inter- crystal (alternately termed "primary particle") mesopore volume and a creation of an additional larger intra-crystal mean mesopore of at least 80 Angstroms were observed after both milder and high temperature steam treatments.
- the mixture was first aged at room temperature (about 20-25°C) for about 24 hours, while stirring at -250 rpm. Then, the aged mixture was reacted at -200°F (-93°C) in a -2-liter autoclave under static conditions for -120 more hours. The product was filtered, washed with deionized (DI) water, and dried at ⁇ 250°F (-120°C).
- XRD X-ray diffraction
- the SEM image of the as-synthesized product material showed that the material was composed of aggregates of small ciystals with an aggregate (i.e., secondary) particle size of -2 microns, as shown in Figure 4, which is larger than the secondary particle size of the product of Example 3.
- the as-synthesized Y crystals had a Si0 2 /A1 2 Q 3 molar ratio of -5.5.
- Figure 5 shows nitrogen adsorption-desorption isotherms and pore size distribu tions from BJH desolation of N 2 BET analysis of a sample of the product after calcination at about 600°C.
- Example 5 Preparation of aggregated NaY (Meso-Y) crystals f-lQx scale-up of Example 4) [ ⁇ 086] A mixture was prepared from -8,3 kilograms of water, -2.58 kilograms of Ultrasil® silica, -960 grams of sodium aluminate solution (45% in water), and -1 .8 kilograms of 50% sodium hydroxide solution (in water). The mixture had the following molar composition:
- Example 6 Stabilization by mild steaming conditions on Meso-Y/ alumina catalysts
- the extrudate was washed with deionized water to remove residual nitrate ions, prior to drying at ⁇ 121°C overnight again and subsequent calcination in air at ⁇ 538°C.
- the resulting extrudates were then steamed at ⁇ 700°C for about 4 hours, followed by additional ion-exchange to obtain the final extrudate for Pt impregnation.
- the final extrudate was then impregnated via incipient wetness to -0.6 wt% Pt using
- Examples 7A-B Stabilization of Meso-Y/ ' alumina catalysts by hi gh temperature (>700°C) steam treatment
- the extrudate was w r ashed with deionized water to remove residual nitrate ions, prior to drying at -121°C overnight again and subsequent calcination in air at ⁇ 538°C, The resulting extrudates were then steamed at -760°C for about 1 hour, followed by additional ion-exchange to obtain a treated extrudate.
- Properties of the treated extrudate included an Alpha Value of -140, a UCS of -24.52 Angstroms, and a total surface area of -484 m7g (with a micropore surface area of -307 m7g and an external surface area of -177 m g).
- the resulting treated extrudate was then steamed again at -760 °C for about 16 hours, and a portion was washed with oxalic acid to remove non- framework alumina.
- the portion that was washed with oxalic acid is referred to herein as Meso-Y-B extrudate, and the other portion that was not washed is referred to herein as Meso-Y -A extrudate.
- the pore size distributions of these two extrudates are shown in Figure 7.
- extrudates were then each impregnated via incipient wetness to -0.6 wt% Pt using tetraammmeplatinumnitrate, followed by calcination in air for about 3 hours at ⁇ 680°F ( ⁇ 05°C).
- Examples 8A-B Hydrocracking of vacuum gas oils ( VGO) with the high temperature - stabilized Meso-Y/alurnina catalysts of Examples 7A-B
- Example 7A the HT Stabilized Meso-Y Sample A (labeled as "MesoY-A”) and the HT Stabilized Meso-Y Sample B (labeled as "MesoY-B") hydrocracking catalyst embodiments of the invention from Example 7A-B were comparatively tested under simulated hydrocracking conditions with four (4) comparative hydrocracking catalysts made with commercial USY zeolites.
- Tetraethylammomum Hydroxide (TEAOH) was added to a sufficient quantity of water to produce a 2% solution, and was ad ded to produce an extrudabie paste on a ⁇ 2" ( ⁇ 5.1 cm) diameter BonnotTM extruder.
- TEAOH Tetraethylammomum Hydroxide
- the two (2) catalysts of invention (designated as “MesoY-A” and “MesoY-B") and the four (4) USY reference catalysts (designated as “USY-1”, “USY-2”, “USY-3” and “USY-4") had similar binder compositions and content, zeolite content, and platinum metal loadings.
- the properties of the six (6) catalysts utilized in this example are shown in Table 3.
- the catalysts of invention have a combination low Alpha values, low BET Total Surface Areas, and high External Surface Area : Total Surface Area ratios (i.e., "Relative External Surface Area” as defined in equation [1] herein).
- the catalysts of invention (as shown in embodiments MesoY-A and MesoY-B) also have a significantly higher average pore diameter than the comparable reference catalysts. It is believed that these aspects function to improve the diesel selectivity of the catalyst.
- the embodiments of the catalysts of invention (MesoY-A and MesoY-B) have very low total surface areas compared to the catalysts of the prior art while maintaining external surface areas near those of the prior art.
- the catalyst has a Relative External Surface Area of at least 0.35, more preferably at least 0.50.
- the catalysts of invention have significantly higher average pore diameters than the conventional IJSY catalysts.
- the average pore diameter of the catalyst is at least 7.0 nanometers (nm), preferably at least 7.5 nm, more preferably at least 8.0 nm, and most preferably at least 9.0 nm.
- the hydrocarbon feed utilized in the testing of this example was a typical hydrotreated and fractionated vacuum gas oil (VGO) feedstock.
- Table 4 shows the composition of the hydrocarbon feed utilized during the testing.
- the hydrocarbon feed that was utilized boiled above the 400 to 700 °F diesel range, and simulated a typical gas oil range feedstock.
- ail diesel range material present in the products was a resulting conversion product from higher boiling point hydrocarbons obtained under hydrocracking conditions.
- the MesoY -A and MesoY-B catalysts of invention produced a higher diesel yield than the reference USY hydrocracking catalysts even at lower overall conversions (at 700°F+ conversions of about 53-57% vs. about 81 to 96%).
- Figure 9 shows the results of the testing in terms of diesel selectivity.
- the bydrocracking catalysis embodiments of invention were about 100% more selective (i.e., about twice as selective) toward diesel production as the reference catalysts.
- the catalysts of invention would still be expected to be about twice as selective to diesel production than the reference catalysts simulating comparative USY bydrocracking catalysts of the prior art.
Abstract
Description
Claims
Applications Claiming Priority (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US13/041,597 US8852326B2 (en) | 2011-03-07 | 2011-03-07 | Aggregates of small particles of synthetic faujasite zeolite |
US201161512067P | 2011-07-27 | 2011-07-27 | |
US201161512042P | 2011-07-27 | 2011-07-27 | |
US13/412,945 US8778171B2 (en) | 2011-07-27 | 2012-03-06 | Hydrocracking catalysts containing stabilized aggregates of small crystallites of zeolite Y associated hydrocarbon conversion processes |
PCT/US2012/027960 WO2012122208A1 (en) | 2011-03-07 | 2012-03-07 | Hydrocracking catalysts containing stabilized aggregates of small crystallites of zeolite y and associated hydrocarbon conversion processes |
Publications (2)
Publication Number | Publication Date |
---|---|
EP2683479A1 true EP2683479A1 (en) | 2014-01-15 |
EP2683479A4 EP2683479A4 (en) | 2014-08-20 |
Family
ID=49152179
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP12755532.4A Withdrawn EP2683479A4 (en) | 2011-03-07 | 2012-03-07 | Hydrocracking catalysts containing stabilized aggregates of small crystallites of zeolite y and associated hydrocarbon conversion processes |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP2683479A4 (en) |
CA (1) | CA2825324C (en) |
SG (1) | SG192577A1 (en) |
WO (1) | WO2012122208A1 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU2779444C1 (en) * | 2021-12-15 | 2022-09-07 | Федеральное государственное бюджетное учреждение науки "Федеральный исследовательский центр "Институт катализа им. Г.К. Борескова Сибирского отделения Российской академии наук" (ИК СО РАН, Институт катализа СО РАН) | Catalyst for the second stage of hydrocracking |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN103934019B (en) * | 2014-04-21 | 2015-11-11 | 四川省中明环境治理有限公司 | A kind of preparations and applicatio method of producing ultra-clean low-coagulation diesel oil catalyst |
CN105435837B (en) * | 2014-08-29 | 2019-01-08 | 中国石油化工股份有限公司 | A kind of hydrocracking catalyst and its preparation and application |
CN105435835B (en) * | 2014-08-29 | 2019-01-08 | 中国石油化工股份有限公司 | A kind of hydrocracking catalyst and its preparation and application |
US11311866B2 (en) | 2020-08-27 | 2022-04-26 | Saudi Arabian Oil Company | Cracking catalyst comprising platinum encapsulated in microporous silica |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5993773A (en) * | 1997-11-27 | 1999-11-30 | Tosoh Corporation | Low-silica faujasite type zeolite and method for producing the same |
US20030100439A1 (en) * | 2000-03-24 | 2003-05-29 | Canos Avelino Corma | Catalytic cracking materials based on ITQ-7 zeolites and their use in hydrocarbons cracking processes |
US20090036294A1 (en) * | 2004-01-29 | 2009-02-05 | Younes Bouizi | Catalyst in the form of grains comprising an acidic porous core surrounded by a uniform outer layer |
US20100092383A1 (en) * | 2004-04-23 | 2010-04-15 | Massachusetts Institute Of Technology | Mesostructured Zeolitic Materials and Methods of Making and Using the Same |
WO2010077352A1 (en) * | 2008-12-16 | 2010-07-08 | Exxonmobil Research And Engineering Company | Integrated hydrocracking and dewaxing of hydrocarbons |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4897178A (en) * | 1983-05-02 | 1990-01-30 | Uop | Hydrocracking catalyst and hydrocracking process |
US6261441B1 (en) * | 1998-09-24 | 2001-07-17 | Mobil Oil Corporation | Integrated hydroprocessing scheme with segregated recycle |
US6500329B2 (en) * | 1998-12-30 | 2002-12-31 | Exxonmobil Research And Engineering Company | Selective ring opening process for producing diesel fuel with increased cetane number |
US6843977B2 (en) * | 2000-05-25 | 2005-01-18 | Board Of Trustees Of Michigan State University | Ultrastable porous aluminosilicate structures and compositions derived therefrom |
US6902664B2 (en) * | 2002-11-08 | 2005-06-07 | Chevron U.S.A. Inc. | Extremely low acidity USY and homogeneous, amorphous silica-alumina hydrocracking catalyst and process |
CN1839195A (en) * | 2003-06-26 | 2006-09-27 | 赫多特普索化工设备公司 | Hydrocarbon conversion process and catalyst |
-
2012
- 2012-03-07 SG SG2013055793A patent/SG192577A1/en unknown
- 2012-03-07 WO PCT/US2012/027960 patent/WO2012122208A1/en active Application Filing
- 2012-03-07 CA CA2825324A patent/CA2825324C/en not_active Expired - Fee Related
- 2012-03-07 EP EP12755532.4A patent/EP2683479A4/en not_active Withdrawn
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5993773A (en) * | 1997-11-27 | 1999-11-30 | Tosoh Corporation | Low-silica faujasite type zeolite and method for producing the same |
US20030100439A1 (en) * | 2000-03-24 | 2003-05-29 | Canos Avelino Corma | Catalytic cracking materials based on ITQ-7 zeolites and their use in hydrocarbons cracking processes |
US20090036294A1 (en) * | 2004-01-29 | 2009-02-05 | Younes Bouizi | Catalyst in the form of grains comprising an acidic porous core surrounded by a uniform outer layer |
US20100092383A1 (en) * | 2004-04-23 | 2010-04-15 | Massachusetts Institute Of Technology | Mesostructured Zeolitic Materials and Methods of Making and Using the Same |
WO2010077352A1 (en) * | 2008-12-16 | 2010-07-08 | Exxonmobil Research And Engineering Company | Integrated hydrocracking and dewaxing of hydrocarbons |
Non-Patent Citations (1)
Title |
---|
See also references of WO2012122208A1 * |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU2779444C1 (en) * | 2021-12-15 | 2022-09-07 | Федеральное государственное бюджетное учреждение науки "Федеральный исследовательский центр "Институт катализа им. Г.К. Борескова Сибирского отделения Российской академии наук" (ИК СО РАН, Институт катализа СО РАН) | Catalyst for the second stage of hydrocracking |
Also Published As
Publication number | Publication date |
---|---|
CA2825324A1 (en) | 2012-09-13 |
EP2683479A4 (en) | 2014-08-20 |
SG192577A1 (en) | 2013-09-30 |
CA2825324C (en) | 2017-09-05 |
WO2012122208A1 (en) | 2012-09-13 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US8778171B2 (en) | Hydrocracking catalysts containing stabilized aggregates of small crystallites of zeolite Y associated hydrocarbon conversion processes | |
US8932454B2 (en) | Mesoporous Y hydrocracking catalyst and associated hydrocracking processes | |
US8513150B2 (en) | Extra mesoporous Y zeolite | |
RU2202412C2 (en) | Method of preparing catalytic composition | |
US7790019B2 (en) | Zeolitic catalyst, substrate based on a silica-alumina matrix and zeolite, and hydrocracking process for hydrocarbon feedstocks | |
US9718050B2 (en) | Catalyst comprising at least one zeolite NU-86, at least one zeolite USY and a porous mineral matrix and process for hydroconversion of hydrocarbon feeds using said catalyst | |
KR20070004776A (en) | Catalyst carrier and catalyst composition, processes for their preparation and their use | |
US8882993B2 (en) | Stabilized aggregates of small crystallites of zeolite Y | |
JP7437412B2 (en) | Catalytic cracking catalyst and its preparation method | |
US20110042270A1 (en) | Catalyst comprising at least one particular zeolite and at least one silica-alumina, and process for hydrocracking hydrocarbon feeds using said catalyst | |
WO2021259347A1 (en) | Zsm-5/β core-shell molecular sieve and synthesis and use thereof | |
CA2825324C (en) | Hydrocracking catalysts containing stabilized aggregates of small crystallites of zeolite y and associated hydrocarbon conversion processes | |
CA2894483C (en) | Mesoporous zeolite-y hydrocracking catalyst and associated hydrocracking processes | |
CN1501841A (en) | Zeolite based catalyst of ultra-high kinetic conversion activity | |
CN114425421B (en) | Catalytic cracking catalyst and preparation method and application thereof | |
JP6046776B2 (en) | Hydrocracking catalyst and fuel substrate production method | |
JP2023523468A (en) | Modified Beta Zeolites, Catalytic Cracking Catalysts and Methods of Making and Using Them | |
US8778824B2 (en) | Aggregates of small crystallites of zeolite Y | |
JP4773420B2 (en) | Hydrocarbon oil catalytic cracking catalyst and hydrocarbon oil catalytic cracking method | |
CN114425418B (en) | Application of core-shell molecular sieve in heavy oil catalytic cracking catalyst | |
CN114425420B (en) | Catalytic cracking catalyst with rich pore channel structure and preparation method and application thereof |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
17P | Request for examination filed |
Effective date: 20131004 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR |
|
DAX | Request for extension of the european patent (deleted) | ||
A4 | Supplementary search report drawn up and despatched |
Effective date: 20140718 |
|
RIC1 | Information provided on ipc code assigned before grant |
Ipc: B01J 37/02 20060101ALI20140714BHEP Ipc: B01J 35/10 20060101ALI20140714BHEP Ipc: C10G 47/00 20060101ALI20140714BHEP Ipc: B01J 23/882 20060101ALI20140714BHEP Ipc: B01J 37/00 20060101ALI20140714BHEP Ipc: B01J 23/883 20060101ALI20140714BHEP Ipc: B01J 29/00 20060101AFI20140714BHEP Ipc: B01J 23/42 20060101ALI20140714BHEP Ipc: B01J 35/08 20060101ALI20140714BHEP Ipc: B01J 23/888 20060101ALI20140714BHEP Ipc: B01J 29/16 20060101ALI20140714BHEP |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: EXAMINATION IS IN PROGRESS |
|
17Q | First examination report despatched |
Effective date: 20180625 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: EXAMINATION IS IN PROGRESS |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN |
|
18D | Application deemed to be withdrawn |
Effective date: 20201103 |