AU2009309421A1 - Cobalt catalyst precursor - Google Patents
Cobalt catalyst precursor Download PDFInfo
- Publication number
- AU2009309421A1 AU2009309421A1 AU2009309421A AU2009309421A AU2009309421A1 AU 2009309421 A1 AU2009309421 A1 AU 2009309421A1 AU 2009309421 A AU2009309421 A AU 2009309421A AU 2009309421 A AU2009309421 A AU 2009309421A AU 2009309421 A1 AU2009309421 A1 AU 2009309421A1
- Authority
- AU
- Australia
- Prior art keywords
- catalyst precursor
- cobalt
- catalyst
- range
- hydrogen
- 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.)
- Abandoned
Links
- 239000012018 catalyst precursor Substances 0.000 title claims description 70
- 229910017052 cobalt Inorganic materials 0.000 title claims description 51
- 239000010941 cobalt Substances 0.000 title claims description 51
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 title claims description 51
- 238000000034 method Methods 0.000 claims description 52
- 239000003054 catalyst Substances 0.000 claims description 51
- 230000009467 reduction Effects 0.000 claims description 47
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 44
- 239000007789 gas Substances 0.000 claims description 38
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 35
- 239000000203 mixture Substances 0.000 claims description 27
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 24
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 24
- 229910052739 hydrogen Inorganic materials 0.000 claims description 24
- 239000001257 hydrogen Substances 0.000 claims description 24
- 229910052751 metal Inorganic materials 0.000 claims description 23
- 239000002184 metal Substances 0.000 claims description 23
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 claims description 22
- 229910052707 ruthenium Inorganic materials 0.000 claims description 21
- 239000000377 silicon dioxide Substances 0.000 claims description 20
- 230000008569 process Effects 0.000 claims description 19
- 239000000654 additive Substances 0.000 claims description 16
- 230000015572 biosynthetic process Effects 0.000 claims description 16
- 238000003786 synthesis reaction Methods 0.000 claims description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 15
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 15
- 150000001875 compounds Chemical class 0.000 claims description 14
- 229910052697 platinum Inorganic materials 0.000 claims description 13
- 229910052799 carbon Inorganic materials 0.000 claims description 12
- 229930195733 hydrocarbon Natural products 0.000 claims description 11
- 150000002430 hydrocarbons Chemical class 0.000 claims description 11
- 239000002002 slurry Substances 0.000 claims description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 239000002245 particle Substances 0.000 claims description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 9
- 239000000843 powder Substances 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000010949 copper Substances 0.000 claims description 8
- 229910052802 copper Inorganic materials 0.000 claims description 7
- 229910052746 lanthanum Inorganic materials 0.000 claims description 7
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims description 6
- 150000001869 cobalt compounds Chemical class 0.000 claims description 6
- 239000011261 inert gas Substances 0.000 claims description 5
- 229910052741 iridium Inorganic materials 0.000 claims description 5
- 150000002739 metals Chemical class 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 150000004645 aluminates Chemical class 0.000 claims description 4
- 229910052797 bismuth Inorganic materials 0.000 claims description 4
- 239000011651 chromium Substances 0.000 claims description 4
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 claims description 4
- 239000011777 magnesium Substances 0.000 claims description 4
- 239000011572 manganese Substances 0.000 claims description 4
- 229910052763 palladium Inorganic materials 0.000 claims description 4
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 claims description 4
- 229910010271 silicon carbide Inorganic materials 0.000 claims description 4
- 229910052709 silver Inorganic materials 0.000 claims description 4
- 239000010936 titanium Substances 0.000 claims description 4
- 229910018920 CoO(OH) Inorganic materials 0.000 claims description 3
- 230000004913 activation Effects 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 150000002431 hydrogen Chemical group 0.000 claims description 3
- 239000011787 zinc oxide Substances 0.000 claims description 3
- 229910052684 Cerium Inorganic materials 0.000 claims description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 claims description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 2
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 claims description 2
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 2
- 230000003213 activating effect Effects 0.000 claims description 2
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 claims description 2
- 229910052804 chromium Inorganic materials 0.000 claims description 2
- 229910052749 magnesium Inorganic materials 0.000 claims description 2
- 229910052748 manganese Inorganic materials 0.000 claims description 2
- 229910052750 molybdenum Inorganic materials 0.000 claims description 2
- 239000011733 molybdenum Substances 0.000 claims description 2
- 229920000307 polymer substrate Polymers 0.000 claims description 2
- VSZWPYCFIRKVQL-UHFFFAOYSA-N selanylidenegallium;selenium Chemical compound [Se].[Se]=[Ga].[Se]=[Ga] VSZWPYCFIRKVQL-UHFFFAOYSA-N 0.000 claims description 2
- JBQYATWDVHIOAR-UHFFFAOYSA-N tellanylidenegermanium Chemical compound [Te]=[Ge] JBQYATWDVHIOAR-UHFFFAOYSA-N 0.000 claims description 2
- 229910052719 titanium Inorganic materials 0.000 claims description 2
- 238000005470 impregnation Methods 0.000 description 22
- 239000000243 solution Substances 0.000 description 18
- 230000000052 comparative effect Effects 0.000 description 17
- 238000001354 calcination Methods 0.000 description 15
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Substances [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 15
- 239000000463 material Substances 0.000 description 14
- 235000010215 titanium dioxide Nutrition 0.000 description 12
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 9
- 230000000996 additive effect Effects 0.000 description 9
- 230000000694 effects Effects 0.000 description 9
- 238000011065 in-situ storage Methods 0.000 description 9
- 238000001035 drying Methods 0.000 description 8
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 6
- 239000011248 coating agent Substances 0.000 description 6
- 238000000576 coating method Methods 0.000 description 6
- 238000002474 experimental method Methods 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 239000011148 porous material Substances 0.000 description 6
- 229910052702 rhenium Inorganic materials 0.000 description 6
- 239000002904 solvent Substances 0.000 description 6
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 5
- 239000008188 pellet Substances 0.000 description 5
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- QGUAJWGNOXCYJF-UHFFFAOYSA-N cobalt dinitrate hexahydrate Chemical compound O.O.O.O.O.O.[Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O QGUAJWGNOXCYJF-UHFFFAOYSA-N 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000001556 precipitation Methods 0.000 description 4
- OJLCQGGSMYKWEK-UHFFFAOYSA-K ruthenium(3+);triacetate Chemical compound [Ru+3].CC([O-])=O.CC([O-])=O.CC([O-])=O OJLCQGGSMYKWEK-UHFFFAOYSA-K 0.000 description 4
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical compound [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 description 3
- 229910001981 cobalt nitrate Inorganic materials 0.000 description 3
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical class [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 description 3
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical compound [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 description 3
- 230000008021 deposition Effects 0.000 description 3
- 239000010931 gold Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 150000002736 metal compounds Chemical class 0.000 description 3
- 239000001272 nitrous oxide Substances 0.000 description 3
- KDLHZDBZIXYQEI-UHFFFAOYSA-N palladium Substances [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 3
- 239000002243 precursor Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- 102100022840 DnaJ homolog subfamily C member 7 Human genes 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 101000903053 Homo sapiens DnaJ homolog subfamily C member 7 Proteins 0.000 description 2
- 229910002651 NO3 Inorganic materials 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 2
- 238000003556 assay Methods 0.000 description 2
- XFWJKVMFIVXPKK-UHFFFAOYSA-N calcium;oxido(oxo)alumane Chemical compound [Ca+2].[O-][Al]=O.[O-][Al]=O XFWJKVMFIVXPKK-UHFFFAOYSA-N 0.000 description 2
- 229910000428 cobalt oxide Inorganic materials 0.000 description 2
- CRHLEZORXKQUEI-UHFFFAOYSA-N dialuminum;cobalt(2+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[O-2].[O-2].[Al+3].[Al+3].[Co+2].[Co+2] CRHLEZORXKQUEI-UHFFFAOYSA-N 0.000 description 2
- 229910021485 fumed silica Inorganic materials 0.000 description 2
- 238000004817 gas chromatography Methods 0.000 description 2
- 229910052737 gold Inorganic materials 0.000 description 2
- 238000002354 inductively-coupled plasma atomic emission spectroscopy Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 229910001960 metal nitrate Inorganic materials 0.000 description 2
- -1 nickel aluminate Chemical class 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- NWAHZABTSDUXMJ-UHFFFAOYSA-N platinum(2+);dinitrate Chemical compound [Pt+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O NWAHZABTSDUXMJ-UHFFFAOYSA-N 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- WUAPFZMCVAUBPE-UHFFFAOYSA-N rhenium atom Chemical compound [Re] WUAPFZMCVAUBPE-UHFFFAOYSA-N 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- XMWRBQBLMFGWIX-UHFFFAOYSA-N C60 fullerene Chemical class C12=C3C(C4=C56)=C7C8=C5C5=C9C%10=C6C6=C4C1=C1C4=C6C6=C%10C%10=C9C9=C%11C5=C8C5=C8C7=C3C3=C7C2=C1C1=C2C4=C6C4=C%10C6=C9C9=C%11C5=C5C8=C3C3=C7C1=C1C2=C4C6=C2C9=C5C3=C12 XMWRBQBLMFGWIX-UHFFFAOYSA-N 0.000 description 1
- 241000640882 Condea Species 0.000 description 1
- 102000002322 Egg Proteins Human genes 0.000 description 1
- 108010000912 Egg Proteins Proteins 0.000 description 1
- 101000801664 Homo sapiens Nucleoprotein TPR Proteins 0.000 description 1
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 1
- 102100033615 Nucleoprotein TPR Human genes 0.000 description 1
- 239000012494 Quartz wool Substances 0.000 description 1
- 150000001242 acetic acid derivatives Chemical class 0.000 description 1
- 125000005595 acetylacetonate group Chemical group 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000004703 alkoxides Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- CETPSERCERDGAM-UHFFFAOYSA-N ceric oxide Chemical compound O=[Ce]=O CETPSERCERDGAM-UHFFFAOYSA-N 0.000 description 1
- 229910000422 cerium(IV) oxide Inorganic materials 0.000 description 1
- 239000003426 co-catalyst Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 210000003278 egg shell Anatomy 0.000 description 1
- 238000005538 encapsulation Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 229910003472 fullerene Inorganic materials 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- YQNQTEBHHUSESQ-UHFFFAOYSA-N lithium aluminate Chemical compound [Li+].[O-][Al]=O YQNQTEBHHUSESQ-UHFFFAOYSA-N 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 1
- AZEGRRQOQSUJJK-UHFFFAOYSA-N nitrate;hydrochloride Chemical compound Cl.[O-][N+]([O-])=O AZEGRRQOQSUJJK-UHFFFAOYSA-N 0.000 description 1
- 150000002902 organometallic compounds Chemical class 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000003921 particle size analysis Methods 0.000 description 1
- 230000036581 peripheral resistance Effects 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 230000001698 pyrogenic effect Effects 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 229910052596 spinel Inorganic materials 0.000 description 1
- 239000011029 spinel Substances 0.000 description 1
- 229910052566 spinel group Inorganic materials 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
Classifications
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- 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
- B01J23/74—Iron group metals
- B01J23/75—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
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
- B01J23/8913—Cobalt and 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
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
- B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
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- B01J35/30—
-
- B01J35/612—
-
- 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
- B01J37/0203—Impregnation the impregnation liquid containing organic compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/16—Reducing
- B01J37/18—Reducing with gases containing free hydrogen
-
- C—CHEMISTRY; METALLURGY
- 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
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
- C10G2/331—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals
- C10G2/332—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals of the iron-group
-
- 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
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
- C10G2/331—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals
- C10G2/333—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals of the platinum-group
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
- B01J21/04—Alumina
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
- B01J21/08—Silica
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- 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
- B01J23/843—Arsenic, antimony or bismuth
- B01J23/8437—Bismuth
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- B01J35/40—
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- 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
- B01J37/08—Heat treatment
Description
WO 2010/049715 PCT/GB2009/051290 Cobalt Catalyst Precursor This invention relates to cobalt catalysts and in particular cobalt catalysts suitable for the Fischer-Tropsch synthesis of hydrocarbons. Cobalt catalysts suitable for use in the Fischer Tropsch process for synthesising hydrocarbons are generally subjected to pre-reduction and encapsulation in a suitable material prior to installation in the Fischer-Tropsch reactor. This is because the reduction processes typically are operated at temperatures > 250 0 C, and in particular >300'C, which are challenging for the fixed bed or slurry phase reactors used. Furthermore reduction is typically performed using hydrogen gas streams, and the gas streams available for in-situ reduction generally comprise synthesis gas mixtures containing carbon monoxide. Whereas in-situ reduction of cobalt Fischer-Tropsch catalysts is a desired aim, heretofore such processes have not been commercially used. We have found a specific combination of inert support and additive that allows effective cobalt reduction at low temperatures. Accordingly the invention provides a catalyst precursor comprising 5 to 50% by weight of one or more oxidic cobalt compounds selected from CoO, CoO(OH) and CoO 4 and 0.05 to 10% by weight of one or more reduction promoters selected from metals or compounds of Ru, Pt, Cu, Rh, Pd, Ir, Ag and Bi, supported on an inert support selected from alpha alumina, a metal aluminate, silica, titania, zirconia, zinc oxide, silicon carbide, carbon or mixtures thereof, wherein the cobalt is in a highly reducible form such that at least 75% of the cobalt is reducible by a reducing gas stream at temperatures 240'C. Hence, in the catalyst according to the present invention, the cobalt is present in a highly reducible form so that the oxidic cobalt compound may be effectively reduced by a reducing gas stream at temperatures ! 240'C. By "effectively reduced" we mean that the degree of reduction, i.e. the amount of cobalt reduced is 75% wt, preferably 85% wt, more preferably 90% wt of the Co present in the catalyst precursor. Such low temperature reduction offers the opportunity for commercially attractive in-situ reduction thereby removing the need for pre-reduced, encapsulated catalysts that can be difficult to manufacture and transport. Accordingly the invention further provides a process for activating a catalyst comprising placing the above catalyst precursor in a Fischer-Tropsch reactor and passing a reducing gas mixture over the catalyst precursor for a period of time to reduce cobalt present therein to elemental form, wherein the temperature of the reducing gas mixture throughout the activation step is 240 0
C.
WO 2010/049715 PCT/GB2009/051290 2 The invention further provides a process for the Fischer-Tropsch synthesis of hydrocarbons comprising the step of passing a gas mixture comprising hydrogen and carbon monoxide over a catalyst in a Fischer-Tropsch reactor wherein the catalyst has been activated by passing a reducing gas mixture at a temperature of 5 2400C over the above catalyst precursor in the Fischer Tropsch reactor,. The cobalt content of the catalyst precursor is in the range 5 to 50% by weight, preferably 10 to 35% by weight, most preferably 12 to 30% by weight. The additive or promoter content of the catalyst precursor is in the range 0.05 to 10% by weight, preferably 0.1 to 5% wt, most preferably 0.1 to 2% by weight . The total amount of additive or promoter in the catalyst precursor is preferably 5 10% by weight. The metal contents may be determined using known methods such as ICP AES or ICP OES. In the present invention preferably all of the cobalt is in reducible form, i.e. preferably <5% by weight, more preferably <1% by weight, most preferably < 0.05% by weight and especially none of the cobalt is in the form of a cobalt-support mixed oxide such as cobalt aluminate. The reducible cobalt is present as one or more of CoO, CoO(OH) and C0304. Preferably substantially all of the reducible cobalt is present as C0304. At least 75%, preferably at least 85%, more preferably at least 90% of the cobalt is reducible, i.e. the degree of reduction (DOR) is preferably 75%, more preferably 85%, especially t90%. A temperature-programmed reduction (TPR) method for estimating DOR may be used as follows: 1. Steadily increase the sample temperature to the desired temperature (52400C) at 10'C/min, hold at that temperature for ten hours (TPR1). 2. Without cooling back to room temperature, increase the sample temperature to 10000C at 1 0 0 C/min and hold at 1000 C for ten minutes. (TPR2). This gives complete reduction of all cobalt. 3. Integrate the hydrogen uptakes from TPRs 1 and 2. The ratio TPR1/(TPR1 + TPR2) is the degree of reduction (expressed as %). The reduction promoter in the present invention is selected from one or more compounds or metals of Ru, Pt, Cu, Rh, Pd, Ir, Ag and Bi, preferably one or more of Ru, Pt and Cu, more preferably Ru. The inert support in the present invention is one that is inert to the cobalt, i.e. does not readily form mixed oxides of cobalt, such as cobalt aluminate spinels. The inert support is selected from alpha alumina, a metal-aluminate, silica, titania, zirconia, zinc oxide, silicon carbide, carbon or mixtures thereof.
WO 2010/049715 PCT/GB2009/051290 3 The support and hence the resulting catalyst precursor may be in the form of a powder having a surface-weighted mean diameter D[3,2] in the range 1 to 200 microns. The term surface weighted mean diameter D[3,2], otherwise termed the Sauter mean diameter, is defined by M. Alderliesten in the paper "A Nomenclature for Mean Particle Diameters"; Anal. Proc., vol 21, May 1984, pages 167-172, and is calculated from the particle size analysis, which may conveniently be effected by laser diffraction for example using a Malvern Mastersizer. Agglomerates of such powders having particle sizes in the range 200 microns to 1 mm may also be used as the support. Alternatively the support and hence the resulting catalyst precursor may be in the form of shaped units such as pellets, extrudates or granules typically having particle sizes in the range 1-25 mm and an aspect ratio of less than 2. (By particle size we mean the smallest particle dimension such as width, length or diameter). Alternatively the support may be in the form of a monolith, e.g. a honeycomb, or a cellular material such as an open foam structure. The inert support may also be in the form of a wash-coat on a ceramic, metal, carbon or polymer substrate. Such catalysts advantageously offer in-situ reduction in micro GTL equipment. Carbon supports, such as activated carbons, high surface area graphites, carbon nanofibres, and fullerenes in powder, pellet or granular form and having suitable porosities, e.g. above 0.1 ml/g may be used as supports for the present invention. Such supports are preferably not used in methods where air calcination is employed because of oxidation of the support. Preferably catalyst precursors comprising carbon supports are produced where the gas stream to which the carbon is exposed during calcination contains preferably <1%, more preferably < 0.1%, oxygen by volume, e.g. oxygen free nitrogen, helium or argon. The support may be a silica support. Silica supports may be formed from natural sources, e.g. as kieselguhr, may be a pyrogenic or fumed silica or may be a synthetic, e.g. precipitated silica or silica gel. Structured mesoporous silicas, such as SBA-15 may be used as a support. Precipitated silicas are preferred. The silica may be in the form of a powder or a shaped material, e.g. as extruded, pelleted or granulated silica pieces. Suitable powdered silicas typically have particles of surface weighted mean diameter D[3,2] in the range 3 to 100 pm. Shaped silicas may have a variety of shapes and particle sizes, depending upon the mould or die used in their manufacture. For example the particles may have a cross-sectional shape which is circular, lobed or other shape and a length from about 1 to greater than 10 mm. The BET surface area of suitable powdered or granular silicas is generally in the range 10 - 500 m 2 /g, preferably 100 - 400 m 2 g . The pore volume is generally between about 0.1 and 4 ml/g, preferably 0.2 - 2 ml/g and the mean pore diameter is preferably in the range from 0.4 to about 30 nm. If desired, the silica may be mixed with another metal oxide, such as titania or zirconia. The silica may alternatively be present as a coating on a shaped unit, which is preferably of alumina typically as a coating of 0.5 to 5 monolayers of silica upon the underlying support.
WO 2010/049715 PCT/GB2009/051290 4 The support may be a titania support. Titania supports are preferably synthetic, e.g. precipitated titanias. The titania may optionally comprise e.g. up to 20% by weight of another refractory oxide material, typically silica, alumina or zirconia. The titania may alternatively be present as a coating on a support which is preferably of silica or alumina, for example as a coating of 0.5 to 5 monolayers of titania upon the underlying alumina or silica support. The BET surface area of suitable titania is generally in the range 10 - 500 m 2 /g, preferably 100 to 400 m 2 /g. The pore volume of the titania is preferably between about 0.1 and 4 ml/g, more preferably 0.2 to 2 ml/g and the mean pore diameter is preferably in the range from 2 to about 30 nm. Similarly zirconia supports maybe synthetic, e.g. precipitated zirconias. The zirconia may again optionally comprise e.g. up to 20% by weight of another refractory oxide material, typically silica, alumina or titania. Alternatively the zirconia may be stabilised e.g. an yttria- or ceria stabilised zirconia. The zirconia may alternatively be present as a coating on a support, which is preferably of silica or alumina, for example as a coating of 0.5 to 5 monolayers of zirconia upon the underlying alumina or silica support. The support may be a metal aluminate, for example a calcium aluminate. In one embodiment the inert support is alpha-alumina. The alpha alumina may be obtained commercially or made by heating transition aluminas, e.g. gamma-alumina, to temperatures in the range 1000-1500'C, preferably >12000C. The alpha alumina is preferably reasonably pure with an alkali content < 100ppm, preferably < 50 ppm and substantially no metal aluminate spinel present. The BET surface area is preferably < 50m 2 /g. A suitable alpha alumina powder generally has a surface-weighted mean diameter D[3,2] in the range 1 to 200 pm. In certain applications such as for catalysts intended for use in slurry reactions, it is advantageous to use very fine particles which are, on average, preferably less than 20 pm, e.g. 10 pm or less. For other applications e.g. as a catalyst for reactions carried out in a fluidised bed, it may be desirable to use larger particle sizes, preferably in the range 50 to 150 pm. The alumina support material may be in the form of a spray dried powder or formed into shaped units such as spheres, pellets, cylinders, rings, or multi-holed pellets, which may be multi-lobed or fluted, e.g. of cloverleaf cross-section, or in the form of extrudates known to those skilled in the art. The alpha alumina support may be advantageously chosen for high filterability and attrition resistance. Alpha-alumina supported cobalt Fischer-Tropsch catalysts are known. WO 02/47816 describes cobalt catalysts on an alpha alumina or alpha alumina-containing support. The list of possible promoters given includes Re, Pt, Ir or Rh. However, reduction of the catalyst precursors was performed at 250-400'C, preferably 300-4000C.
WO 2010/049715 PCT/GB2009/051290 5 Metal-aluminate supports such as nickel aluminate, lithium aluminate or calcium aluminate supports may also be used in the present invention. These supports have the advantage of being unable to readily interact with the cobalt oxides formed thereon. The catalyst precursors may be prepared using known methods. For example the catalysts may be prepared using impregnation methods, precipitation methods or deposition precipitation methods, or a combination of these, generally followed by a drying step to remove any solvents and a calcination step to effect conversion of the cobalt and additive or promoter compounds to their respective oxides. The cobalt and promoter may be uniformly distributed within the support or may be in the form of an eggshell on its surface. Deposition precipitation methods and impregnation methods are preferred. Deposition precipitation methods whereby cobalt ammine carbonate solutions are heated to deposit cobalt compounds onto supports are known. For example, suitable methods for preparing alumina-, silica- and titania-supported catalysts using cobalt ammine carbonate solutions are described in US 5874381, WO 01/62381, WO 01/87480, WO 04/28687 and WO 05/107942. In general, cobalt compounds may be deposited onto the inert support by either (a) impregnating the support with an aqueous cobalt ammine carbonate solution, separating the impregnated support from any excess solution, and then heating the impregnated support to a temperature in the range 60-110'C, in air or in the presence of a suitable oxidant or, (b) heating a slurry of support in cobalt ammine carbonate solution to a temperature in the range 60-110 C in air or in the presence of a suitable oxidant. The first method is particularly suitable when preparing catalysts on shaped supports such as extrudates or pellets, whereas the second method is particularly suitable for powder supports. In impregnation methods, a suitable soluble metal compounds, for example the metal nitrate or acetate may be impregnated onto a support material from an aqueous or non-aqueous solution, e.g. ethanol, which may include other materials, and then dried to remove the solvent or solvents. One or more soluble metal compounds may be present in the solution. One or more impregnation steps may be performed, with or without intervening drying and/or calcination steps, to increase metal loading or provide sequential layers of different metal compounds. Impregnation may be performed using any of the methods known to those skilled in the art of catalyst manufacture, but preferably is by way of a so-called 'dry' or 'incipient wetness' impregnation as this minimises the quantity of solvent used and to be removed in drying. Incipient wetness impregnation comprises mixing the support material with only sufficient solution to fill the pores of the support. Impregnation methods for producing cobalt catalysts generally comprise combining a catalyst support with a solution of cobalt nitrate, e.g.
WO 2010/049715 PCT/GB2009/051290 6 cobalt (II) nitrate hexahydrate at a suitable concentration. Whereas a number of solvents may be used such as water, alcohols, ketones or mixtures of these, preferably the support has been impregnated using aqueous solutions of cobalt nitrate. The reduction promoter may also be included in the catalyst precursor by impregnation, using suitable soluble compounds such as the nitrate chloride, acetate, or mixtures of these. The additive or promoter may be included in the catalyst precursor before or after the cobalt, or at the same time by combining the cobalt and additive or promoter compounds in the same impregnating solution. The amount of cobalt and additive or promoter compound in solution, or the amount of inert support may be varied to achieve the desired metal loadings. Single or multiple impregnations may be performed to achieve the desired cobalt and additive or promoter levels in the catalyst precursor. In a preferred embodiment, the catalyst precursor is made by co-impregnating an inert support with a solution of ruthenium acetate and cobalt nitrate. If desired, the catalyst precursor may be dried to remove solvent prior to calcination. The drying step may be performed at 20-120'C, preferably 95-110 C, in air or under an inert gas such as nitrogen, or in a vacuum oven. The catalyst precursor may then be heated in air to effect conversion of the cobalt and additive or promoter compounds to their respective oxides. The calcination temperature is preferably in the range 250 to 5000C. The calcination time is preferably 5 24, more preferably 5 16, most preferably 5 8, especially 5 6 hours. As an alternative to calcination in air, the dried catalyst precursor may be heated under an inert gas containing <5 % volume oxygen such as nitrogen or argon, which may include nitric oxide or nitrous oxide at a concentration in the range 0.001 to 15% by volume. We have found that calcination of supported nitrate materials under nitric oxide or nitrous oxide leads to improved cobalt dispersion and hence higher cobalt surface areas following reduction than similar air-calcined catalyst precursors. The drying and/or calcination steps may be carried out batch-wise or continuously, depending on the availability of process equipment and/or scale of operation. In a preferred embodiment, the method for making a catalyst precursor comprises the steps of (a) calcining a transition alumina such as gamma alumina at a temperature in the range 1000-1500'C to form an alpha alumina, (b) co-impregnating the alpha alumina with a solution comprising ruthenium and cobalt compounds, at least one of said compounds being a nitrate, (c) drying and calcining the impregnated alumina, said calcination step being performed in air or in an inert gas having <5 % volume oxygen and including nitric oxide or nitrous oxide at a concentration in the range 0.001 to 15% by volume, and WO 2010/049715 PCT/GB2009/051290 7 (d) optionally repeating steps (b) and (c). If desired, the catalyst precursor may in addition to cobalt and one or more of Ru, Pt, Cu, Rh, Pd, Ir, Ag and Bi, further comprise one or more suitable additives useful in Fischer-Tropsch catalysis. For example, the catalysts may comprise one or more additives that alter the physical properties and/or promoters that effect the reducibility or activity or selectivity of the catalysts. Suitable additives are selected from compounds of metals selected from molybdenum (Mo), iron (Fe), manganese (Mn), titanium (Ti), zirconium (Zr), lanthanum (La), cerium (Ce), chromium (Cr), magnesium (Mg) or zinc (Zn). The additives may be incorporated into the catalyst precursor by use of suitable compounds such as acids, metal salts, e.g. metal nitrates or metal acetates, or suitable metal-organic compounds, such as metal alkoxides or metal acetylacetonates. Typical amounts of the additives are 0.1 - 10% metal by weight on catalyst precursor. If desired, the compounds of the additional additives may be added in suitable amounts to the cobalt solution. Alternatively, they may be combined with the catalyst precursor before or after drying or calcination. To render the catalyst precursor catalytically active for Fischer-Tropsch reaction, at least a portion of the cobalt oxide may be reduced to the metal. Reducing gas streams that may be used include hydrogen- and/or carbon monoxide-containing gases. Reduction is preferably performed using hydrogen-containing gasses at elevated temperature. In the present invention the temperature of the reducing gas stream, and hence the catalyst precursor, during the entire reduction stage is 5 240'C, preferably 5 230 0 C, more preferably 5 225'C. The minimum reduction temperature is preferably 90'C, more preferably 100 C, although higher temperatures may speed up reduction and a particularly preferred reduction temperature range is 180-240'C. Before the reduction step, the catalyst precursor may, if desired, be formed into shaped units suitable for the process for which the catalyst is intended, using methods known to those skilled in the art. In the present invention the catalysts are desirably reduced in-situ, i.e. in the reactor in which they are to be used. Fischer Tropsch reactors take a variety of forms including fixed bed reactors in which a gas stream comprising carbon monoxide and hydrogen is passed through one or more beds of a particulate or monolithic catalyst, including catalyst supported on a wash-coated ceramic or metal substrate; and slurry phase reactors in which a gas stream comprising hydrogen and carbon monoxide is passed through a slurry of particulate catalyst in a suitable liquid medium. Such reactors include the well-known slurry bubble column reactors (SBCR's).
WO 2010/049715 PCT/GB2009/051290 8 The reduction, also termed activation, may be performed by passing a reducing gas stream such as hydrogen, synthesis gas (a gas mixture comprising hydrogen, carbon monoxide and/or carbon dioxide) or a mixture of hydrogen and/or carbon monoxide with nitrogen or other inert gas over the oxidic composition at elevated temperature, for example by passing the hydrogen containing gas over the catalyst precursor at temperatures in the range 140-240'C, preferably 160-220'C for between 1 and 16 hours, preferably 1 - 8 hours. Preferably the reducing gas stream comprises hydrogen at >25% vol, more preferably >50% vol, most preferably >75%, especially >90% vol hydrogen. However, in the present invention, it may also be possible to effectively reduce the catalyst precursor using a synthesis gas mixture containing less hydrogen. This may be particularly useful where the catalyst is to be activated in-situ. Preferably at least 90% of the reducible cobalt is reduced at 2400C. The cobalt surface areas of the reduced catalysts may be determined by H 2 chemisorption using known methods. Reduction may be performed at ambient pressure or increased pressure, i.e. the pressure of the reducing gas may suitably be from 1-50, preferably 1-20, more preferably 1-10 bar abs. Higher pressures >10 bar abs may be more appropriate where the reduction is performed in situ. The gas-hourly-space velocity (GHSV) for the reducing gas stream may be in the range 100 25000hr-, preferably 1000 - 15000hr-1. Where the catalyst is to be used in a SBCR, it may be preferable to disperse the catalyst precursor in a suitable liquid medium such as a molten hydrocarbon wax, e.g. a C6 to C40 hydrocarbon mixture, and pass the reducing gas stream through the resulting slurry. The solids content of such a slurry is preferably in the range 1 to 50% w/v, more preferably from 3 to 40% w/v, most preferably from 5 to 35 % w/v. The catalysts may be used for the Fischer-Tropsch synthesis of hydrocarbons. The Fischer-Tropsch synthesis of hydrocarbons with cobalt catalysts is well established. The Fischer-Tropsch synthesis converts a mixture of carbon monoxide and hydrogen to hydrocarbons. The mixture of carbon monoxide and hydrogen is typically a synthesis gas having a hydrogen: carbon monoxide ratio in the range 1.6-3.0:1, preferably 1.7 - 2.5:1. The reaction may be performed in a continuous or batch process using one or more stirred slurry phase reactors, bubble-column reactors, loop reactors or fluidised bed reactors. The process may be operated at pressures in the range 0.1-10Mpa and temperatures in the range 150 3500C. The gas-hourly-space velocity (GHSV) for continuous operation is in the range 100 25000hr-1. A preferred operating range is 1000-15000hr-1.
WO 2010/049715 PCT/GB2009/051290 9 The invention will now be further described by reference to the following Examples and by reference to Figures 1 to 5, which depict temperature-programmed reduction (TPR) plots for Ru-, Pt- and Cu-promoted catalysts that may be used according to the invention, in comparison with an un-promoted catalyst. Example 1: Preparation of alpha-alumina-supported catalyst precursors A gamma alumina (HP 14-150 available from Sasol Condea) was subjected to calcination in air at a temperature of 14000C for sufficient time to convert it to alpha alumina. (i) Examples 1(a) - (c) were prepared by a co-impregnation method. An impregnation solution was prepared by dissolving 5% wt ruthenium acetate in acetic acid and cobalt nitrate hexahydrate in demineralised water. The alpha alumina was treated with the solution by the dry impregnation method, dried at 1050C for 3 hours and calcined by heating to 4000C at 2 0 C/min, and holding at this temperature for 1 hour. The procedure was then repeated on the calcined material. The resulting catalyst precursor had a cobalt content of 17.8% by weight and a ruthenium content of 0.21% by weight. Catalyst precursors were made in the same way using copper (II) nitrate and platinum nitrate to achieve a cobalt content of about 18% wt and reduction promoter level of about 1% wt on the calcined material. (A Co content of about 18% wt in a catalyst precursor corresponds to a Co content of about 20% in a reduced catalyst assuming all the Co is reduced). Comparative catalyst precursor materials containing about 18% wt Co and no promoter, or differing amounts of gold, lanthanum and rhenium were also prepared using the same co impregnation method. (ii) Example 1(d) was prepared by a sequential impregnation method: The alpha alumina was treated with a solution of cobalt nitrate hexahydrate by dry the impregnation method, dried at 105'C for 3 hours and calcined by heating to 400'C at 2 0 C/min, and holding at this temperature for 1 hour. This procedure was then repeated on the calcined material. The resulting alpha alumina-supported cobalt oxide precursor was promoted by impregnation with 5% wt ruthenium acetate in acetic acid and then drying at 105'C for 3 hours. The resulting Ru-promoted catalyst precursor was not calcined. The analysis of the catalyst precursors gave the following; WO 2010/049715 PCT/GB2009/051290 10 Example Promoter Cobalt Assay / % Promoter Assay / % 1(a) Ru 17.8 0.21% Ru 1(b) Pt 18.9 0.89% Pt 1(c) Cu 17.9 0.92% Cu 1(d) Ru 18.8 0.71% Ru Comparative 1 None 18.1 Comparative 2 La 17.3 4.20% La Comparative 3 Re 17.8 0.46% Re Comparative 4 Au 18.5 0.04% Au BET surface areas were measured for the catalyst precursor 1(a), the uncoated alpha alumina and the comparative catalyst precursors. The results were as follows: Example Promoter BET SA / m2 g-1 Difference from support / m 2 g- 1 (%) 1(a) 0.21% Ru 9.45 4.76 (101) Comparative 1 None 5.87 1.18 (25) Comparative 2 4.20% La 7.47 2.78 (59) Comparative 3 0.46% Re 9.07 4.38 (93) alpha alumina 4.69 The ruthenium promoted catalyst gave the highest surface area result, followed by the Re promoted catalyst. Temperature-programmed reduction (TPR) experiments can be useful in predicting the behaviour of catalysts during reduction in situ. Thermal conductivity measurements were made on a sample exposed to hydrogen over time with increasing temperature using an AMI-200 instrument available from Altamira Instruments. The TPR experiments were run using 70 80mg of catalyst precursor in a quartz tube held in place by quartz wool plugs. The catalyst precursor was heated to 1 000 0 C from ambient at a rate of 1 O'C/min under a flow of 30ml/min of 10% H2/Ar, and then held at 1000 C for ten minutes. Figures 1 - 4 depict Examples 1(a)-(d) respectively and show the thermal conductivity changes associated with the reduction of of CoO 4 to CoO and then CoO to Co metal as the temperature is increased and with time. The figures show the copper, ruthenium and platinum containing catalysts to be reduced below 300'C and well below that of the corresponding un-promoted catalyst. The rhenium and lanthanum catalyst precursors were reduced at higher temperatures than the un-promoted catalyst precursor under these conditions. The results were as follows, WO 2010/049715 PCT/GB2009/051290 11 Example Promoter Temperature Temperature of Minor Peak of Major Peak Maxima / C Maxima / C 1(a) 0.21% Ru 108 208, 278 1(b) 0.89% Pt - 101,251 1(c) 0.92% Cu 148 268 1(d) 0.71% Ru 223,261 155 Comparative 1 None 297 341 Comparative 2 4.20% La 189 305, 352 Comparative 3 0.46% Re - 306, 359 Comparative 4 0.04% Au - 330 A series of two-step TPR experiments were performed as above, except that in the first step the catalyst was heated to 220'C at 1 0 0 C/min, and held for 10 hours, then in the second step heated to 1000'C at 10'C/min and held for 10 minutes. By comparing the two experiments, the degree of reduction at 220'C can then be calculated. A further comparative example was done using a catalyst prepared on the gamma alumina using the co-impregnation method described above. The gamma alumina used was HP14 150. The resulting Co content of the precursor was 16.4% and the Ru content, 0.77%. The results were as follows; Example Promoter Degree of Reduction / % 1(a) 0.21% Ru (ax-Al 2
O
3 ) 91 1(b) 0.89% Pt 95 1(c) 0.92% Cu 87 1(d) 0.71% Ru 91 Comparative 1 None 30, 22 Comparative 5 0.77% Ru (y-A1 2 0 3 ) 36 It can be seen that the degree of reduction obtained with the Ru or Pt catalyst is better than the copper catalyst or the catalyst prepared using gamma alumina. Example 2: Preparation of silica-supported catalyst precursors (i) Co-impregnation method. An impregnation solution was prepared by dissolving 5% wt ruthenium acetate in acetic acid and cobalt nitrate hexahydrate in demineralised water. The powdered silica (a precipitated silica with BET surface area of 342m 2 /g and a pore diameter of 6.6 nm) was treated with the solution by the dry impregnation method, dried at 105'C for 3 hours and calcined by heating to 400'C at 2 0 C/min, and holding at this temperature for 1 hour.
WO 2010/049715 PCT/GB2009/051290 12 A single impregnation was used. The resulting catalyst precursor had an estimated cobalt content of 18% by weight and an estimated ruthenium content of 1% by weight. A platinum-promoted catalyst was prepared using the same method except that platinum nitrate was used,to obtain a catalyst precursor having an estimated cobalt content of 18% wt and an estimated Pt content of 1 % wt. TPR experiments were performed according to the method described in Example 1. The TPR plot of the silica-supported Ru-promoted Co catalyst is depicted in Figure 5, along with that of a comparable un-promoted catalyst precursor and clearly shows the lower reduction temperature for the catalyst precursors of the invention. On silica, the performance of Pt as a reduction promoter is similar to that of Ru. The results are given below. Example Promoter Temperature Temperature of Minor Peak of Major Peak Maxima / C Maxima / C 2(a) 1% Ru 97 147,318 2(b) 1% Pt 96 140, 326 Comparative 6 None 287, 295 349 A two-step TPR experiment was also performed according to the method described in Example 1 and showed a degree of reduction of 86% for the Ru-promoted catalyst precursor. Example 3: In situ reduction tests and FT Reactivity The catalyst precursor of Example 1(a) was used for the Fischer-Tropsch synthesis of hydrocarbons in a laboratory-scale tubular reactor. About 0.1 g of catalyst precursor mixed with SiC was placed in bed (ca. 4 mm ID by 50 mm depth) and reduced by passing a reducing gas stream through the bed using three different regimes; a) reduction at 210'C for 7 hours under hydrogen gas, b) reduction at 210'C for 7 hours under a synthesis gas comprising hydrogen and carbon monoxide at a ratio of 2:1 and, c) for comparison, reduction at 380'C for 7 hours under hydrogen gas. Following the reduction step, the samples were cooled to 100 C, the flow for (a) and (c) changed to the synthesis gas and the pressure increased to 20 barg. The temperature was then increased at 1 C/min to 210'C and the Fischer-Tropsch reaction monitored over 120 hrs. The space velocity during reduction was 14400hr- 1 and this was maintained until 30 hrs at which point it was reduced to 3600hr-1. The activity and selectivity of the catalyst to CH 4 , C2 C4 and C5+ hydrocarbons were measured using known Gas Chromatography (GC) techniques. The results at 40 hrs, 100 hrs and 120 hrs for the catalyst reduced according to the different regimes are given below.
WO 2010/049715 PCT/GB2009/051290 13 40hrs at Fischer-Tropsch conditions Example Relative C02 CH 4 C2-C4 C5+ C5=/C5 Activity N N N N N 3(a) 1.2 0.60 7.42 9.27 82.71 2.09 3(b) 1.2 0.43 8.80 10.13 80.64 1.77 3(c) 1.0 0.41 7.11 6.25 86.23 1.65 100hrs at Fischer-Tropsch conditions Example Relative C02 CH 4 C2-C4 C5+ C5=/C5 Activity N N N N N 3(a) 1.1 0.28 6.96 8.34 84.42 2.21 3(b) 1.2 0.23 7.83 9.28 82.66 1.80 3(c) 1.0 0.19 5.36 5.08 89.37 1.74 120hrs at Fischer-Tropsch conditions Example Relative C02 CH 4 C2-C4 C5+ C5=/C5 Activity N N N N N 3(a) 1.1 0.29 6.86 8.38 84.47 2.22 3(b) 1.2 0.22 8.08 9.43 82.27 1.76 3(c) 1.0 0.21 5.80 5.29 88.70 1.71 The results show that the activity relative to the precursor reduced at 3800C is maintained and that the selectivity of the catalysts reduced under hydrogen or syngas is comparable.
Claims (20)
1. A catalyst precursor comprising 5 to 50% by weight of one or more oxidic cobalt compounds selected from CoO, CoO(OH) and C0304 and 0.05 to 10% by weight of one or more reduction promoter selected from metals or compounds of Ru, Pt, Cu, Rh, Pd, Ir, Ag and Bi, supported on an inert support selected from alpha alumina, a metal aluminate, silica, titania, zirconia, zinc oxide, silicon carbide, carbon or mixtures thereof, wherein the cobalt is in a highly reducible form such that at least 75% of the cobalt is reducible by a reducing gas stream at temperatures 5 240'C.
2. A catalyst precursor according to claim 1 wherein the reduction promoter is a compound or metal of Ru, Pt or Cu.
3. A catalyst precursor according to claim 2 wherein the reduction promoter is Ru or an oxide of Ru.
4. A catalyst precursor according to any one of claims 1 to 3 wherein the inert support is alpha alumina.
5. A catalyst precursor according to any one of claims 1 to 4 further comprising one or more additives selected from compounds of metals selected from molybdenum (Mo), iron (Fe), manganese (Mn), titanium (Ti), zirconium (Zr), lanthanum (La), cerium (Ce), chromium (Cr), magnesium (Mg) or zinc (Zn).
6. A catalyst precursor according to any one of claims 1 to 5 wherein the catalyst precursor is a powder with a surface-weighted mean diameter D[3,2] in the range 1 to 200 pm.
7. A catalyst precursor according to any one of claims 1 to 6 wherein the catalyst precursor is a powder with a surface-weighted mean diameter D[3,2] on average, in the range from 1 to 20 pm.
8. A catalyst precursor according to any one of claims 1 to 5 wherein the support and hence the resulting catalyst precursor is in the form of a shaped unit having a particle size in the range 1-25 mm and an aspect ratio of less than 2.
9. A catalyst precursor according to any one of claims 1 to 5 wherein the support is in the form of a wash-coat on a ceramic, metal, carbon or polymer substrate. WO 2010/049715 PCT/GB2009/051290 15
10. A process for activating a catalyst comprising placing a catalyst precursor according to any one of claims 1 to 9 in a Fischer-Tropsch reactor and passing a reducing gas mixture over the catalyst precursor for a period of time to reduce cobalt present therein to elemental form, wherein the temperature of the reducing gas mixture throughout the activation step is 5 2400C.
11. A process according to claim 10 wherein at least 90% of the reducible cobalt is reduced at 5 2400C.
12. A process according to claim 10 or claim 11 wherein the Fischer Tropsch reactor is a fixed bed reactor or a slurry phase reactor.
13. A process according to any one of claims 10 to 12 wherein the reducing gas mixture is hydrogen, synthesis gas or a mixture of hydrogen and/or carbon monoxide with nitrogen or other inert gas.
14. A process according to claim 13 wherein the reducing gas mixture comprises >90% vol hydrogen.
15. A process according to claim 13 wherein the reducing gas mixture comprises a synthesis gas mixture.
16. A process according to any one of claims 10 to 15 wherein the reducing gas mixture is passed over the catalyst precursor at temperatures in the range 140-240'C for between 1 and 16 hours.
17. A process for the Fischer-Tropsch synthesis of hydrocarbons by passing a gas mixture comprising hydrogen and carbon monoxide over a catalyst in a Fischer-Tropsch reactor that has been activated according to the process of any one of claims 10 to 16
18. A process according to claim 17 wherein the mixture of carbon monoxide and hydrogen is a synthesis gas having a hydrogen: carbon monoxide ratio in the range 1.6-3.0:1
19. A process according to claim 17 or claim 18 wherein the reaction is operated at pressures in the range 0.1-10Mpa and temperatures in the range 150-350'C.
20. A process according to any one of claims 17 to 19 wherein the Fischer Tropsch reactor is a fixed bed reactor or a slurry phase reactor.
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GB0819849.1 | 2008-10-30 | ||
GBGB0819849.1A GB0819849D0 (en) | 2008-10-30 | 2008-10-30 | Cobalt catalyst precursor |
PCT/GB2009/051290 WO2010049715A1 (en) | 2008-10-30 | 2009-10-01 | Cobalt catalyst precursor |
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AU (1) | AU2009309421A1 (en) |
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CA2826734C (en) | 2011-02-07 | 2021-06-08 | Oxford Catalysts Limited | Fischer-tropsch catalysts |
JP5795483B2 (en) | 2011-03-31 | 2015-10-14 | 独立行政法人石油天然ガス・金属鉱物資源機構 | Activated Fischer-Tropsch synthesis reaction catalyst and hydrocarbon production method |
FR2978682B1 (en) * | 2011-06-01 | 2016-01-01 | Sicat Llc | CATALYTIC PROCESS FOR THE CONVERSION OF SYNTHESIS GAS TO HYDROCARBONS |
CN102861583B (en) * | 2011-07-04 | 2014-10-15 | 中国石油化工股份有限公司 | Cobalt-based Fischer-Tropasch synthetic catalyst and preparation method |
JP6004528B2 (en) | 2011-08-29 | 2016-10-12 | 地方独立行政法人東京都立産業技術研究センター | Method for producing porous silica-encapsulated particles and porous silica |
FR2984346B1 (en) * | 2011-12-14 | 2013-12-27 | IFP Energies Nouvelles | PROCESS FOR PRODUCING HYDROCARBONS WITH CONTINUOUS CATALYST LOADING |
DK2864044T3 (en) * | 2012-06-26 | 2020-03-16 | Sicat Catalysts Inc | Silicon carbide catalyst supports coated with TiO2 for a Fischer-Tropsch synthesis |
GB201214122D0 (en) | 2012-08-07 | 2012-09-19 | Oxford Catalysts Ltd | Treating of catalyst support |
CN103736493B (en) * | 2012-10-17 | 2015-10-21 | 中国石油化工股份有限公司 | Synthesis gas prepares ferrum-based catalyst and the production method thereof of heavier liquid hydrocarbons |
CN103785415B (en) * | 2012-10-31 | 2016-03-30 | 中国石油化工股份有限公司 | Hydrogenation of carboxylic acids prepares the cobalt bismuth catalyst of alcohol |
EP3027314A2 (en) | 2013-07-31 | 2016-06-08 | Saudi Basic Industries Corporation | Catalyst for conversion of synthesis gas |
CN103638943B (en) * | 2013-10-15 | 2016-04-13 | 河南省科学院能源研究所有限公司 | A kind of co-based fischer-tropsch fixed bde catalyst for biomass synthesis gas and preparation method thereof |
RU2017113773A (en) * | 2014-09-23 | 2018-10-24 | Сабик Глобал Текнолоджиз Б.В. | COBALT-BASED CATALYST AND WAYS RELATED TO IT |
CN109072458A (en) * | 2016-04-18 | 2018-12-21 | 沙特基础工业全球技术公司 | The analysis oxygen elctro-catalyst of cobalt (II, III) oxide skin(coating) containing carbon coating |
GB201702251D0 (en) * | 2017-02-10 | 2017-03-29 | Bp Plc | Process for producting a fischer-tropsch synthesis catalyst |
CN108187708B (en) * | 2018-02-01 | 2021-05-04 | 中科合成油内蒙古有限公司 | Phosphorus-containing high-stability heavy hydrocarbon Fischer-Tropsch synthesis catalyst and preparation method and application thereof |
WO2021139898A1 (en) * | 2020-01-10 | 2021-07-15 | Bp P.L.C. | Process for producing a fischer-tropsch synthesis catalyst and fischer-tropsch start-up process |
WO2023089293A1 (en) | 2021-11-17 | 2023-05-25 | Johnson Matthey Public Limited Company | Method for retrofitting a hydrogen production unit |
GB202117591D0 (en) | 2021-12-06 | 2022-01-19 | Johnson Matthey Plc | Method for retrofitting a hydrogen production unit |
CN114561664B (en) * | 2022-02-17 | 2023-09-26 | 广东省科学院资源利用与稀土开发研究所 | Alkaline electrocatalytic water oxygen evolution material and preparation method and application thereof |
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GB0510316D0 (en) * | 2005-05-20 | 2005-06-29 | Johnson Matthey Plc | Catalyst manufacture |
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