WO2018141648A1 - Iron-doped nickel methanation catalysts - Google Patents
Iron-doped nickel methanation catalysts Download PDFInfo
- Publication number
- WO2018141648A1 WO2018141648A1 PCT/EP2018/051995 EP2018051995W WO2018141648A1 WO 2018141648 A1 WO2018141648 A1 WO 2018141648A1 EP 2018051995 W EP2018051995 W EP 2018051995W WO 2018141648 A1 WO2018141648 A1 WO 2018141648A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- catalyst
- precipitate
- solution
- methanation
- iron
- Prior art date
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- 239000003054 catalyst Substances 0.000 title claims abstract description 121
- 229910052759 nickel Inorganic materials 0.000 title claims abstract description 31
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 title description 67
- 239000002244 precipitate Substances 0.000 claims abstract description 23
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 22
- 229910052742 iron Inorganic materials 0.000 claims abstract description 21
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 12
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 11
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 11
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 10
- 238000000975 co-precipitation Methods 0.000 claims abstract description 9
- 238000001035 drying Methods 0.000 claims abstract description 9
- 238000001354 calcination Methods 0.000 claims abstract description 8
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000000243 solution Substances 0.000 claims description 27
- 238000000034 method Methods 0.000 claims description 20
- 239000000203 mixture Substances 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 10
- 230000008569 process Effects 0.000 claims description 8
- 229910052739 hydrogen Inorganic materials 0.000 claims description 7
- 230000003647 oxidation Effects 0.000 claims description 7
- 238000007254 oxidation reaction Methods 0.000 claims description 7
- 239000011149 active material Substances 0.000 claims description 6
- 239000007864 aqueous solution Substances 0.000 claims description 6
- 239000001257 hydrogen Substances 0.000 claims description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- 150000008040 ionic compounds Chemical class 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 4
- 150000001450 anions Chemical class 0.000 claims description 3
- 229910002651 NO3 Inorganic materials 0.000 claims description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 2
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 claims 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims 1
- 150000004820 halides Chemical class 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 41
- 230000000694 effects Effects 0.000 description 21
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 21
- 229910052751 metal Inorganic materials 0.000 description 18
- 239000002184 metal Substances 0.000 description 18
- 238000006243 chemical reaction Methods 0.000 description 17
- 230000032683 aging Effects 0.000 description 16
- 230000003197 catalytic effect Effects 0.000 description 12
- 239000012266 salt solution Substances 0.000 description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 230000015572 biosynthetic process Effects 0.000 description 8
- 238000005259 measurement Methods 0.000 description 8
- 238000003786 synthesis reaction Methods 0.000 description 7
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 239000011572 manganese Substances 0.000 description 6
- 238000003756 stirring Methods 0.000 description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 5
- 239000003637 basic solution Substances 0.000 description 5
- 238000012360 testing method Methods 0.000 description 5
- BNGXYYYYKUGPPF-UHFFFAOYSA-M (3-methylphenyl)methyl-triphenylphosphanium;chloride Chemical compound [Cl-].CC1=CC=CC(C[P+](C=2C=CC=CC=2)(C=2C=CC=CC=2)C=2C=CC=CC=2)=C1 BNGXYYYYKUGPPF-UHFFFAOYSA-M 0.000 description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 229910052748 manganese Inorganic materials 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 229910000480 nickel oxide Inorganic materials 0.000 description 4
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 description 4
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 description 4
- 229910010271 silicon carbide Inorganic materials 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 239000000654 additive Substances 0.000 description 3
- 230000000996 additive effect Effects 0.000 description 3
- 239000012298 atmosphere Substances 0.000 description 3
- 238000012512 characterization method Methods 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 238000002354 inductively-coupled plasma atomic emission spectroscopy Methods 0.000 description 3
- 238000011068 loading method Methods 0.000 description 3
- MIVBAHRSNUNMPP-UHFFFAOYSA-N manganese(2+);dinitrate Chemical compound [Mn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MIVBAHRSNUNMPP-UHFFFAOYSA-N 0.000 description 3
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 239000002243 precursor Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 229910052719 titanium Inorganic materials 0.000 description 3
- 239000010936 titanium Substances 0.000 description 3
- 238000011282 treatment Methods 0.000 description 3
- 229910052726 zirconium Inorganic materials 0.000 description 3
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 2
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 2
- 241000282326 Felis catus Species 0.000 description 2
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 238000013459 approach Methods 0.000 description 2
- 229910052788 barium Inorganic materials 0.000 description 2
- 229910002090 carbon oxide Inorganic materials 0.000 description 2
- 150000001768 cations Chemical class 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 229910052804 chromium Inorganic materials 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000009849 deactivation Effects 0.000 description 2
- 238000005868 electrolysis reaction Methods 0.000 description 2
- 238000011067 equilibration Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 description 2
- 238000005470 impregnation Methods 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- 150000002505 iron Chemical class 0.000 description 2
- UGKDIUIOSMUOAW-UHFFFAOYSA-N iron nickel Chemical compound [Fe].[Ni] UGKDIUIOSMUOAW-UHFFFAOYSA-N 0.000 description 2
- MVFCKEFYUDZOCX-UHFFFAOYSA-N iron(2+);dinitrate Chemical compound [Fe+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MVFCKEFYUDZOCX-UHFFFAOYSA-N 0.000 description 2
- VCJMYUPGQJHHFU-UHFFFAOYSA-N iron(3+);trinitrate Chemical compound [Fe+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O VCJMYUPGQJHHFU-UHFFFAOYSA-N 0.000 description 2
- 229910052746 lanthanum Inorganic materials 0.000 description 2
- MRELNEQAGSRDBK-UHFFFAOYSA-N lanthanum(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[La+3].[La+3] MRELNEQAGSRDBK-UHFFFAOYSA-N 0.000 description 2
- YIXJRHPUWRPCBB-UHFFFAOYSA-N magnesium nitrate Chemical compound [Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O YIXJRHPUWRPCBB-UHFFFAOYSA-N 0.000 description 2
- 239000000395 magnesium oxide Substances 0.000 description 2
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 229910052750 molybdenum Inorganic materials 0.000 description 2
- 239000012452 mother liquor Substances 0.000 description 2
- 230000007935 neutral effect Effects 0.000 description 2
- 150000002815 nickel Chemical class 0.000 description 2
- 150000002823 nitrates Chemical class 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 229910052703 rhodium Inorganic materials 0.000 description 2
- 239000010948 rhodium Substances 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- OERNJTNJEZOPIA-UHFFFAOYSA-N zirconium nitrate Chemical compound [Zr+4].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O OERNJTNJEZOPIA-UHFFFAOYSA-N 0.000 description 2
- NWZSZGALRFJKBT-KNIFDHDWSA-N (2s)-2,6-diaminohexanoic acid;(2s)-2-hydroxybutanedioic acid Chemical compound OC(=O)[C@@H](O)CC(O)=O.NCCCC[C@H](N)C(O)=O NWZSZGALRFJKBT-KNIFDHDWSA-N 0.000 description 1
- KWSLGOVYXMQPPX-UHFFFAOYSA-N 5-[3-(trifluoromethyl)phenyl]-2h-tetrazole Chemical compound FC(F)(F)C1=CC=CC(C2=NNN=N2)=C1 KWSLGOVYXMQPPX-UHFFFAOYSA-N 0.000 description 1
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- 229910052684 Cerium Inorganic materials 0.000 description 1
- 229910000531 Co alloy Inorganic materials 0.000 description 1
- 229910002483 Cu Ka Inorganic materials 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 239000012494 Quartz wool Substances 0.000 description 1
- 229910052772 Samarium Inorganic materials 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 238000002441 X-ray diffraction Methods 0.000 description 1
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 1
- QVYYOKWPCQYKEY-UHFFFAOYSA-N [Fe].[Co] Chemical compound [Fe].[Co] QVYYOKWPCQYKEY-UHFFFAOYSA-N 0.000 description 1
- MQRWBMAEBQOWAF-UHFFFAOYSA-N acetic acid;nickel Chemical compound [Ni].CC(O)=O.CC(O)=O MQRWBMAEBQOWAF-UHFFFAOYSA-N 0.000 description 1
- 239000002671 adjuvant Substances 0.000 description 1
- 229910001854 alkali hydroxide Inorganic materials 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 1
- 239000001099 ammonium carbonate Substances 0.000 description 1
- 235000012501 ammonium carbonate Nutrition 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 229910052787 antimony Inorganic materials 0.000 description 1
- 229960005070 ascorbic acid Drugs 0.000 description 1
- 235000010323 ascorbic acid Nutrition 0.000 description 1
- 239000011668 ascorbic acid Substances 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 229910052796 boron Inorganic materials 0.000 description 1
- XFWJKVMFIVXPKK-UHFFFAOYSA-N calcium;oxido(oxo)alumane Chemical compound [Ca+2].[O-][Al]=O.[O-][Al]=O XFWJKVMFIVXPKK-UHFFFAOYSA-N 0.000 description 1
- 239000012482 calibration solution Substances 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 description 1
- 229910000420 cerium oxide Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 229910000428 cobalt oxide Inorganic materials 0.000 description 1
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical compound [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- KYCIUIVANPKXLW-UHFFFAOYSA-N dimethyl-(2-phenoxyethyl)-(thiophen-2-ylmethyl)azanium Chemical compound C=1C=CSC=1C[N+](C)(C)CCOC1=CC=CC=C1 KYCIUIVANPKXLW-UHFFFAOYSA-N 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 238000000921 elemental analysis Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000013213 extrapolation Methods 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 230000002431 foraging effect Effects 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- IKDUDTNKRLTJSI-UHFFFAOYSA-N hydrazine monohydrate Substances O.NN IKDUDTNKRLTJSI-UHFFFAOYSA-N 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 229910052738 indium Inorganic materials 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 229910052741 iridium Inorganic materials 0.000 description 1
- 235000014413 iron hydroxide Nutrition 0.000 description 1
- 229910000358 iron sulfate Inorganic materials 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 1
- PVFSDGKDKFSOTB-UHFFFAOYSA-K iron(3+);triacetate Chemical compound [Fe+3].CC([O-])=O.CC([O-])=O.CC([O-])=O PVFSDGKDKFSOTB-UHFFFAOYSA-K 0.000 description 1
- NCNCGGDMXMBVIA-UHFFFAOYSA-L iron(ii) hydroxide Chemical compound [OH-].[OH-].[Fe+2] NCNCGGDMXMBVIA-UHFFFAOYSA-L 0.000 description 1
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 description 1
- 231100001231 less toxic Toxicity 0.000 description 1
- 239000000314 lubricant Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 239000002923 metal particle Substances 0.000 description 1
- 230000002211 methanization Effects 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- 230000011987 methylation Effects 0.000 description 1
- 238000007069 methylation reaction Methods 0.000 description 1
- 229910000476 molybdenum oxide Inorganic materials 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229940078494 nickel acetate Drugs 0.000 description 1
- QMMRZOWCJAIUJA-UHFFFAOYSA-L nickel dichloride Chemical compound Cl[Ni]Cl QMMRZOWCJAIUJA-UHFFFAOYSA-L 0.000 description 1
- LGQLOGILCSXPEA-UHFFFAOYSA-L nickel sulfate Chemical compound [Ni+2].[O-]S([O-])(=O)=O LGQLOGILCSXPEA-UHFFFAOYSA-L 0.000 description 1
- 229910000008 nickel(II) carbonate Inorganic materials 0.000 description 1
- 229910000363 nickel(II) sulfate Inorganic materials 0.000 description 1
- ZULUUIKRFGGGTL-UHFFFAOYSA-L nickel(ii) carbonate Chemical compound [Ni+2].[O-]C([O-])=O ZULUUIKRFGGGTL-UHFFFAOYSA-L 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 238000010606 normalization Methods 0.000 description 1
- BMMGVYCKOGBVEV-UHFFFAOYSA-N oxo(oxoceriooxy)cerium Chemical compound [Ce]=O.O=[Ce]=O BMMGVYCKOGBVEV-UHFFFAOYSA-N 0.000 description 1
- PQQKPALAQIIWST-UHFFFAOYSA-N oxomolybdenum Chemical compound [Mo]=O PQQKPALAQIIWST-UHFFFAOYSA-N 0.000 description 1
- -1 oxygen anions Chemical class 0.000 description 1
- 125000004430 oxygen atom Chemical group O* 0.000 description 1
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 239000000546 pharmaceutical excipient Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 238000000634 powder X-ray diffraction Methods 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 229910001404 rare earth metal oxide Inorganic materials 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 229910001954 samarium oxide Inorganic materials 0.000 description 1
- 229940075630 samarium oxide Drugs 0.000 description 1
- FKTOIHSPIPYAPE-UHFFFAOYSA-N samarium(iii) oxide Chemical compound [O-2].[O-2].[O-2].[Sm+3].[Sm+3] FKTOIHSPIPYAPE-UHFFFAOYSA-N 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 229910001379 sodium hypophosphite Inorganic materials 0.000 description 1
- 238000003980 solgel method Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004441 surface measurement Methods 0.000 description 1
- 229910052715 tantalum Inorganic materials 0.000 description 1
- 230000036962 time dependent Effects 0.000 description 1
- 229910052718 tin Inorganic materials 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 229910001928 zirconium oxide Inorganic materials 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—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
- B01J23/745—Iron
-
- 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
- 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
- B01J23/755—Nickel
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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
- B01J37/02—Impregnation, coating or precipitation
- B01J37/03—Precipitation; Co-precipitation
- B01J37/031—Precipitation
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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
- B01J37/06—Washing
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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
- B01J37/082—Decomposition and pyrolysis
- B01J37/088—Decomposition of a metal salt
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
- C07C1/12—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon dioxide with hydrogen
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper
- C07C2523/74—Iron group metals
- C07C2523/755—Nickel
Definitions
- the energy supply through the so-called renewable energy photovoltaic and wind energy suffers from the problem of weather and daytime dependent fluctuations in electricity production.
- a way has to be found to intercept weather and time-dependent fluctuations in electricity production.
- One potential method of chemically storing energy is the power-to-gas process, which uses excess electricity to split water into hydrogen and oxygen by electrolysis. Hydrogen in which the energy is stored after the electrolysis of water can itself be stored only with great effort or transported to the consumer. After the power-to-gas process, the hydrogen is therefore converted in a further step with carbon dioxide, which acts in the atmosphere as a greenhouse gas harmful to the climate, in the methanation reaction to methane and water.
- Methane can be easily stored in existing infrastructures, which have capacities for storage in the range of several months, can be transported almost lossless over longer distances and can be reconverted in times of energy demand.
- the methanation reaction which is associated with high energy release and usually catalyzes, forms the heart of the process.
- the high exothermicity of the reaction (-165 kJ / mol) gives rise to two direct problems.
- the thermodynamic equilibrium limits the maximum achievable methane yield at high temperatures.
- a purity of 95% is necessary in Germany. This results in the demand for a high catalyst activity, so that at industrially applied reaction pressures at low temperatures higher yields of methane can be achieved.
- catalysts which contain not only an active metal, but are promotiert. It is known from the literature that a promotion with iron or manganese can have a positive influence on the catalyst performance.
- a doping of nickel-based methanation catalysts with iron is described, for example, in CN 104399482 A, CN 104399466 A, CN 104209127 A, CN 102872874 A, CN 101703933 A, CN 101537357 A, WO 2007025691 A1, CN 103706366 A, CN 104028270 A and CN 101745401 A. by Pandey et al., Journal of Industrial and Engineering Chemistry (2016), 33, 99-107, and Gao, et al., RSC Advances (2015), 5 (29), 22759-22776.
- CN 104399482 A and CN 104399466 A disclose a natural ore loaded iron containing nickel catalyst for methanization and the production thereof.
- Nickel oxide makes up 2 to 15% by weight of the catalyst.
- the calcination temperature of the carrier, the calcination temperature of the catalyst, the reduction temperature of the catalyst and the like made a bimetallic iron-nickel methanation catalyst.
- the catalyst thus prepared is characterized by a low nickel loading capacity, high activity, good stability, high strength and the like.
- CN 104209127 A relates to a bimetallic nickel / iron methanation catalyst and the preparation and use thereof.
- the alumina carrier In a ratio of 0.7 to 1 ml of soluble salt solution to 1 g of alumina carrier, the alumina carrier is immersed in the prepared soluble salt solution.
- the carrier In a ratio of 0.7 to 1 ml of a soluble nickel salt solution to 1 g of the additive-containing carrier, the carrier is immersed in the nickel salt solution to obtain a nickel-containing carrier.
- the nickel-containing carrier In a ratio of 0.7 to 1 ml of an iron salt solution to 1 g of the nickel-containing carrier the nickel-containing carrier is dipped in the iron salt solution to be subsequently dried and calcined to obtain a catalyst containing 2.5 to 10% by weight of nickel oxide, 2.5 to 10% by weight of iron oxide, 0.01 to 5 wt .-% of an additive, wherein the additive is at least one element selected from lanthanum, cerium, barium, and magnesium.
- the catalyst thus prepared exhibits a greatly increased activity in cryogenic methanation, has reduced costs and improves methane selectivity and stability.
- CN 102872874 A relates to a nickel-based loaded catalyst used for the methylation in a suspension, a production process and the use thereof.
- the nickel-based loaded catalyst consists of 10 to 40% by weight of NiO, 56 to 90% by weight of a carrier and 0 to 4% by weight of an adjuvant.
- the nickel-based loaded catalyst is prepared by the steps of preparing a soluble salt solution with 0.5 to 1.3 g / ml nickel nitrate and the excipient; adding a catalyst carrier and a soluble organic fuel to the salt solution in tandem; impregnation for 6 to 24 hours with stirring; heating the solution, for concentration, in a water bath at a temperature of 60 to 90 ° C, after impregnation or heating to directly ignite the solution at a temperature of 300 to 700 ° C; isolating the post-combustion powder, grinding and granulating the powder, and reducing for 2 to 6 hours with a reducing gas in a fixed bed reactor at a temperature of 500 to 700 ° C.
- CN 101537357 A relates to a methanation catalyst produced from synthetic gas.
- the methanation catalyst comprises the following components: 1 to 20% iron oxide, 1 to 30% cobalt oxide, 1 to 30% nickel oxide, 0 to 10% of a rare earth oxide, 0 to 10% molybdenum oxide, and 50 to 97% silicon carbide support.
- the preparation of the methanation catalyst comprises the silicon carbide material, which is chemically stable and has good thermal conductivity, as a catalyst support for producing a methanation catalyst by synthetic gas.
- WO 2007025691 A1 relates to a process for the hydrogenation of carbon oxides comprising contacting a gas mixture containing carbon oxides and hydrogen with a catalyst comprising a bimetallic iron-nickel or iron-cobalt alloy as an active catalyst material, applied to an oxidic support.
- the support preferably has a surface area> 20 m 2 / g.
- CN 103706366 A describes a catalyst comprising 15 to 55% of an active component, 1 to 6% of a 1. catalytic promoter, 3 to 15% of a second catalytic promoter and, moreover, a catalytic support, wherein the active component is nickel oxide, the catalytic support is Al 2 O 3 , the 1.
- the catalytic promoter is one selected from lanthanum oxide, cerium oxide or samarium oxide, the second catalytic promoter is at least one of magnesium oxide, manganese oxide, iron oxide and zirconium oxide.
- the production method comprises the steps of dissolving a reducing agent in water to obtain a reducing solution, mixing in nickel nitrate, aluminum nitrate, the 1. Metal salt and the 2nd metal salt in water to obtain a raw material solution and adding the reducing mixture to the raw material solution with uniform stirring to obtain a 1.
- a metal salt of at least one selected from magnesium nitrate, manganese nitrate, iron nitrate and zirconium nitrate, the alkali metal solution is an aqueous solution of sodium carbonate, sodium hydroxide, potassium carbonate, ammonium carbonate, urea or NH 3 * H 2 0 is.
- the catalyst may be mixed with a binder (calcium aluminate), a lubricant (graphite) and water and then pressed in particulate form.
- the catalyst is suitable for the methanation of coal gas at high temperature and high pressure to produce synthetic natural gas.
- CN 104028270 A discloses a methanation catalyst comprising 5 to 60 wt .-% of a catalytically active NiO component, based on the total weight of the catalyst and otherwise Al 2 0 3 , which also 1 to 25 wt .-%, based on the total weight of Catalyst, may participate in participating component M, wherein the co-acting component M is selected from one or more oxides of the metals Ce, Ca, Co, La, Sm, Zr, Ba, Mn, Fe, Mo, Ti and Cu.
- the document also provides a method of making the methanation catalyst which comprises mixing the precursor of the catalytically active component, the precursor of the co-acting component M and a catalyst support according to the proportion in the methanation catalyst composition, adding an organic fuel and the thoroughly mixing and drying to form a gel-like product, carrying out a combustion reaction, cleaning and drying to obtain the final product.
- CN 101745401 discloses a supported sulfur-resistant methanation catalyst which is characterized in that it comprises a main metal M as active component, a second metal M1 as auxiliary and S as support material, the weight ratio between M1, M and S being between 0 Where M is one or more of Mo, W and / or V, the second metal M1 is one or more of Fe, Co, Ni, Cr, Mn, La , Y and / or Ce and the support S Zr0 2 , Al 2 0 3 , MgO or Ti0 2 .
- the supported sulfur-resistant methanation catalyst is prepared by a sol-gel method.
- a catalyst for the methanation of carbon monoxide and / or carbon dioxide comprising aluminum oxide and a Ni active composition which contains Fe, characterized in that the molar Ni / Fe ratio in the catalyst is 4.0 to 25.0, preferably 5.0 to 10.0, and more preferably 5.0 to 6.0.
- the stability of the catalyst in the sense of the application means the property of the catalyst to deactivate as little as possible under reaction conditions and to maintain the high selectivity / activity as far as possible.
- the alumina need not be stoichiometric Al 2 O 3, but may be a non-stoichiometric alumina.
- the molar Ni / Fe ratio may be in the range of 4.5 to 8.0, preferably in the range of 5.0 to 7.0, most preferably in the range of 5.3 to 5.5.
- the promoter Fe may be contained completely or partially in the Ni active material.
- the catalyst may contain other promoters in addition to Fe, but it may also contain exclusively the promoter Fe.
- the oxidation states of Al, Ni and the promoters can vary depending on the treatment of the catalyst. Al, Ni and the promoters are typically present as metal cations (eg, Al 3+, Ni 2+, Fe 2+, Fe 3+). After calcination, eg in air, high oxidation states or the maximum oxidation states can be achieved. Becomes the catalyst is reduced at temperatures above room temperature, for example under reaction conditions with hydrogen, AI, Ni and the promoters can assume lower oxidation states or occur partially or completely in the oxidation state 0. The charge balance to the metal cations is carried out by negatively charged oxygen atoms (0 2 ⁇ ).
- the catalyst according to the invention may contain other components besides aluminum oxide (AlO x with x ⁇ 1.5) Ni and Fe (as well as the oxygen anions necessary for charge equalization), but it may also consist exclusively of aluminum oxide, Ni and Fe.
- the Ni active material in addition to Fe may contain further promoters, but it may also contain only the promoter Fe.
- the catalyst does not contain any of the elements selected from Ta, In, Cu, Ce, Cr, Bi, Mn, P, B, Sb, Sn, Si, Ti, Zr, Co, Rh, Ru, Ag, Ir, Pd and Pt ,
- the catalyst does not contain a noble metal.
- the catalyst does not contain Mn.
- the atomic Al / Ni ratio may be between 0.5 and 1.5, preferably between 0.8 and 1.2, more preferably the Al / Ni ratio is approximately 1.
- the catalysts according to the invention can advantageously have crystallites in the Ni active composition with a diameter of less than 20 nm, preferably less than 10 nm.
- the Ni active material may also consist entirely or substantially of crystallites with a diameter of less than 20 nm, preferably less than 10 nm.
- the Ni active material is preferably in a metallic state.
- the C0 2 absorption capacity of the catalysts at 35 ° C may be greater than 150 ⁇ / g and is preferably in the range between 150 to 250 ⁇ / g, more preferably, between 180 to 210 ⁇ / g.
- the BET surface area (SBET) of the catalyst according to the invention may be greater than 100 m 2 / g, preferably greater than 200 m 2 / g, or in the range between 200 and
- 400 m 2 / g preferably in the range between 200 and 300 m 2 / g and in particular in the range between 200 and 250 m 2 / g.
- the specific metal surface area (Swiet) of the catalyst according to the invention is preferably greater than 5 m 2 / g, preferably greater than 10 m 2 / g, or in the range between 5 and 25 m 2 / g, preferably in the range between 10 and 20 m 2 / g, or in the range between 9 and 12 m 2 / g. Furthermore, the invention relates to a process for the preparation of a methanation catalyst, comprising the steps:
- step d) calcining the dried precipitate from step c).
- the solution from step a) is an aqueous solution and Al, Ni and Fe are present dissolved in the aqueous solution as ionic compounds.
- Al is preferably dissolved as aluminum nitrate, aluminum trichloride or aluminum sulfate.
- Ni is preferably dissolved as nickel nitrate, nickel dichloride, nickel sulfate, nickel acetate or nickel carbonate.
- Fe is preferably in the oxidation state II or III and is dissolved as iron nitrate, iron or trichloride, iron acetate, iron sulfate or iron hydroxide.
- Al, Ni and Fe are in dissolved form as ionic compounds in the aqueous solution and have the same anion, which may be, for example, nitrate.
- the coprecipitation is carried out by adding the solution containing Al, Ni and Fe to a basic solution or by adding a basic solution to the proposed solution containing Al, Ni and Fe.
- the solution containing Al, Ni and Fe and the basic solution are simultaneously added to a vessel which may already contain a solvent such as water and is mixed therein.
- the basic solution has a pH greater than 7, preferably in the range of 8 to 10, and preferably contains an alkali hydroxide and / or an alkali carbonate.
- the basic solution is an aqueous solution of sodium hydroxide and sodium carbonate.
- the coprecipitation is preferably carried out under temperature control, so that the temperature of the solution is approximately room temperature or, for example, 30 ° C.
- the precipitate in the solution is preferably more preferably for at least 30 minutes, preferably longer than 1 hour aged for more than 12 hours.
- the aging is preferably carried out by stirring the precipitate at approximately room temperature in the solution (mother liquor).
- the precipitate obtained by the coprecipitation is isolated, for example by filtering.
- the filtering can be done in a suitable manner, for example by a filter press.
- the isolated precipitate is preferably washed, for example with distilled water, until a neutral pH is reached.
- the isolated precipitate can be dried, for example at elevated temperature in air.
- the drying takes place at a temperature between 70 ° C and 90 ° C for a period longer than 4 hours, preferably longer than 12 hours.
- the isolated precipitate is calcined, this can be done in air at a temperature between 300 ° C to 600 ° C, preferably 400 ° C to 500 ° C and in a period of 3 to 10 hours, preferably 5 to 7 hours.
- the catalyst according to the invention is intended to be used in particular in the methanation of carbon monoxide and / or carbon dioxide.
- the methanation of carbon dioxide can be represented by the following reaction equation: 4H 2 + C0 2 -> CH 4 + 2H 2 0
- the methanation of carbon monoxide can be represented by the following reaction equation:
- the reaction gas containing carbon dioxide and / or carbon monoxide or a mixture of both is contacted with the catalyst at a temperature higher than 200 ° C.
- the figures show the catalytic behavior of the iron-doped catalysts Fe2, Fe4, Fe7 and Fe10 before and after aging.
- Figure 1 Catalytic test results for Fe2 (example).
- FIG. 3 Catalytic test results for Fe7 (example).
- FIG. 4 Catalytic test results for Fe10 (comparative example).
- FIG. 5 Normalized WTY (CH4) as a function of the aging time for Fe711 in comparison to Nill at an aging temperature of 450 ° C.
- FIG. 6 Normalized WTY (CH4) as a function of the aging time for Fe711 in comparison to Nill at an aging temperature of 350 ° C.
- the determination of the composition of the calcined catalysts was carried out by means of inductively coupled plasma optical emission spectroscopy (ICP-OES). 50 mg of catalyst were dissolved in 50 ml of 1 molar phosphoric acid (VWR, pA) at 60 ° C. To dissolve any brownstone formed, 50 mg Na 2 S0 3 (Sigma Aldrich, pA) was added to the solution. After cooling, the solutions were diluted 1/10 and filtered by 0.1 ⁇ filters (Pall). The calibration solutions were prepared at 1, 10 and 50 mg I -1 (Merck). Determination of metal concentrations was performed using an Agilent 700 ICP-OES.
- the specific surface area of the catalysts was determined by N 2 -BET analysis on a NOVA 4000e (Quantachrome). For this purpose, 100 mg of catalyst were degassed for 3 hours at 120 ° C and then absorbed adsorption and Desorptionsiso- therme in the p / p 0 range of 0.007 to 1. To determine the BET surface area, the data points in the p / p 0 range of 0.007 to 0.28 were used. chemisorption
- the equilibration time for the adsorption was set to 10 min with otherwise unchanged parameters. Before the absorption of the chemisorption data, any kinetic inhibition of CO 2 chemisorption under these conditions was experimentally excluded. Metal surfaces and CC uptake capacities were extrapolated to a pressure of 0 mmHg according to the extrapolation method.
- the catalysts were prepared by coprecipitation and the atomic ratio of nickel and aluminum was adjusted to 1.
- iron (III) nitrate was added to the salt solution of nickel and aluminum nitrate during catalyst synthesis.
- manganese (II) nitrate was added to the salt solution of nickel and aluminum nitrate during catalyst synthesis.
- the purity of all chemicals used was pa Water was purified by a Millipore filter system and the degree of purity verified by conductivity measurements.
- the synthesis was carried out in a double-walled, 3 l stirred tank. The water-filled double jacket allowed the temperature of the synthesis approach to 30 ° C via a thermostat, two baffles provided for an improved mixing. For stirring, a KPG stirrer with 150 revolutions min.
- the precipitation reagent was a mixture of 0.5M NaOH and 0.5 M Na 2 C0 3 solutions of equal volume, for the metering of which a titrator was used. With constant stirring, the suspension was aged overnight in the mother liquor, the precipitate was then filtered off and washed with H 2 0 until the filtrate had a neutral pH. After drying at 80 ° C in a drying oven overnight, the dried precipitate (precursor) was heated at a heating rate of 5 K min -1 to 450 ° C and calcined for 6 hours under synthetic air. Activity and stability measurement
- Table 1 Parameters of the measurement steps for determining the activity and stability profile
- the temperature in the specified range was gradually increased by 25 ° C and each determines the activity.
- a comparison of the two S-curves before and after 32 hours of aging at 500 ° C gives an insight into the stability of the systems in terms of high temperatures.
- the temperature T 7 5, i was determined, which is necessary in order to achieve a C0 2 conversion of 75% during the measuring step S-curve 1.
- the temperature in the specified range was gradually increased by 25 ° C. Therefore, the lower T 7 5, i, the higher the activity of the catalyst.
- the temperature T 7 5.2 which is necessary in order to achieve a C0 2 conversion of 75% during the measuring step S-curve 2, was determined representatively.
- the temperature in the specified range was gradually increased by 25 ° C.
- FIGS. 1 to 4 show that the promotion of a Ni / AlO x catalyst with iron, with a Ni / Fe ratio in the catalyst of 4.0 to 25.0, leads to a significant increase in the catalyst stability.
- 50 mg of the calcined catalyst was mixed with 450 mg Fe-free SiC (ESK) and placed in a quartz glass-coated tube reactor (4 mm ID).
- the catalyst bed was fixed with quartz wool plugs and positioned in the isothermal zone of a furnace.
- the catalyst temperature would be measured via a thermocouple in the catalyst bed.
- the catalyst was contacted with a heating rate of 2 K min-1 in 5% H2 in Ar with 50 min- NL 1 to 485 5 C. and reduced there for 5 h.
- the aging time was 2 h in the initial deactivation treatment and 4 h in all further treatments.
- the catalyst bed was cooled to 230 ° C before the catalyst activity was re-determined under the above conditions to follow the catalyst deactivation in the kinetic regime under conditions free of product or equilibrium limitations. These cycles were repeated to obtain catalysts aged for 0, 6, 40 and 72 hours. The aged catalysts were transferred under Ar atmosphere to a glovebox, from which further characterization studies were prepared.
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Abstract
The invention relates to a catalyst for the methanation of carbon monoxide and/or carbon dioxide, comprising aluminum oxide, an Ni active mass and Fe, characterized in that the molar Ni/Fe ratio in the catalyst is 4.0 to 25.0, preferably 5.0 to 10.0, and particularly preferably 6.5 to 7.5. The invention also relates to a method for producing a catalyst according to the invention, comprising the following steps: a) co-precipitation from a solution containing Al, Ni and Fe in a dissolved form in order to obtain a precipitate, b) isolating the precipitate of step a), c) drying the isolated precipitate of step b), and d) calcining the dried precipitate of step c).
Description
Eisendotierte Nickel-Methanisierungskatalysatoren Iron-doped nickel methanation catalysts
Die Energieversorgung durch die sogenannten erneuerbaren Energien Photovoltaik und Windenergie leidet unter der Problematik der witterungs- und tageszeitabhängigen Schwankungen in der Stromproduktion. Zur Gewährleistung der Versorgungssicherheit muss ein Weg gefunden werden, um witterungs- und tageszeitabhängige Schwankungen in der Stromproduktion abzufangen. Eine potentielle Methode, um die Energie chemisch zu speichern, stellt das Power-to-Gas Verfahren dar, in welchem überschüssiger Strom verwendet wird, um Wasser durch Elektrolyse in Wasserstoff und Sauerstoff zu spalten. Was- serstoff, in welchem die Energie nach der Wasserelektrolyse gespeichert ist, kann selbst nur mit hohem Aufwand gelagert oder zum Verbraucher transportiert werden. Nach dem Power-to-Gas Verfahren wird der Wasserstoff daher in einem weiteren Schritt mit Kohlendioxid, welches in der Atmosphäre als klimaschädliches Treibhausgas wirkt, in der Methanisierungsreaktion zu Methan und Wasser umgesetzt. Methan kann in bereits vorhandenen Infrastrukturen, welche Kapazitäten zur Speicherung im Bereich von mehreren Monaten umfassen, leicht gespeichert, über größere Strecken nahezu verlustfrei transportiert und in Zeiten von Energiebedarf wieder rückverstromt werden. Die Methanisierungsreaktion, die mit einer hohen Energiefreisetzung verbunden ist und üblicherweise katalysiert abläuft, bildet das Kernstück des Verfahrens. Aus der hohen Exothermie der Reaktion (-165 kJ/mol) ergeben sich zwei direkte Probleme. Zum einen limitiert bei hohen Temperaturen das ther- modynamische Gleichgewicht die maximal erreichbare Ausbeute an Methan. Für die Ein- speisung von Methan in das Erdgasnetz ist in Deutschland eine Reinheit von 95% notwendig. Daraus ergibt sich die Forderung nach einer hohen Katalysatoraktivität, sodass bei industriell angewandten Reaktionsdrücken bei niedrigen Temperaturen höhere Ausbeuten an Methan erzielt werden können. The energy supply through the so-called renewable energy photovoltaic and wind energy suffers from the problem of weather and daytime dependent fluctuations in electricity production. To ensure security of supply, a way has to be found to intercept weather and time-dependent fluctuations in electricity production. One potential method of chemically storing energy is the power-to-gas process, which uses excess electricity to split water into hydrogen and oxygen by electrolysis. Hydrogen in which the energy is stored after the electrolysis of water can itself be stored only with great effort or transported to the consumer. After the power-to-gas process, the hydrogen is therefore converted in a further step with carbon dioxide, which acts in the atmosphere as a greenhouse gas harmful to the climate, in the methanation reaction to methane and water. Methane can be easily stored in existing infrastructures, which have capacities for storage in the range of several months, can be transported almost lossless over longer distances and can be reconverted in times of energy demand. The methanation reaction, which is associated with high energy release and usually catalyzes, forms the heart of the process. The high exothermicity of the reaction (-165 kJ / mol) gives rise to two direct problems. On the one hand, the thermodynamic equilibrium limits the maximum achievable methane yield at high temperatures. For the feeding of methane into the natural gas network, a purity of 95% is necessary in Germany. This results in the demand for a high catalyst activity, so that at industrially applied reaction pressures at low temperatures higher yields of methane can be achieved.
Die hohe Exothermie der Methanisierungsreaktion bewirkt bei adiabatischer Reaktorfahrweise unter Umständen Hotspotbildungen im Reaktor. Dabei kommt es lokal zur Entwicklung hoher Temperaturen, die den Katalysator beschädigen können. Es besteht daher ein starkes Interesse darin, möglichst stabile Katalysatorsysteme zu entwickeln, um Kosten für Katalysatorwechsel/Stillstandzeit und Materialkosten zu minimieren. Weiterhin ergibt sich der Bedarf von möglichst aktiven und selektiven Katalysatoren für die Methanisierungsreaktion von C02. Für die Methanisierungsreaktion werden hauptsächlich nickelbasierte Katalysatoren verwendet, jedoch gibt es auch Ansätze mit anderen aktiven Metallen, wie beispielsweise Ru-
thenium oder Rhodium. Als Träger kommen neben Aluminiumoxid auch die Oxide von Silizium, Titan und Zirkonium zum Einsatz. Beschrieben werden solche Systeme zum Beispiel in den Offenlegungsschriften CN 104043454 A, CN 103480375 A, CN 102091629 A, CN 104888783 A und WO 20081 10331 A1 . The high exothermicity of the methanation reaction may cause hot spot formation in the reactor under adiabatic reactor operation. This leads to the development of high temperatures locally, which can damage the catalyst. There is therefore a strong interest in developing catalyst systems that are as stable as possible in order to minimize costs for catalyst replacement / downtime and material costs. Furthermore, there is a need for highly active and selective catalysts for the methanation reaction of C0 2 . For the methanation reaction mainly nickel-based catalysts are used, but there are also approaches with other active metals, such as Ru thenium or rhodium. In addition to aluminum oxide, the oxides of silicon, titanium and zirconium are also used as carriers. Such systems are described, for example, in the publications CN 104043454 A, CN 103480375 A, CN 102091629 A, CN 104888783 A and WO 20081 10331 A1.
Zusätzlich findet man Katalysatoren, welche nicht nur ein aktives Metall enthalten, sondern promotiert sind. Aus der Literatur ist bekannt, dass eine Promotierung mit Eisen oder Mangan einen positiven Einfluss auf die Katalysatorperformance haben kann. Eine Dotierung von nickelbasierten Methanisierungskatalysatoren mit Eisen wird zum Beispiel in CN 104399482 A, CN 104399466 A, CN 104209127 A, CN 102872874 A, CN 101703933 A, CN 101537357 A, WO 2007025691 A1 , CN 103706366 A, CN 104028270 A und CN 101745401 A beschrieben, sowie durch Pandey et al., Journal of Industrial and Engineering Chemistry (2016), 33, 99-107, und Gao, et al., RSC Advances (2015), 5(29), 22759-22776. Additionally one finds catalysts, which contain not only an active metal, but are promotiert. It is known from the literature that a promotion with iron or manganese can have a positive influence on the catalyst performance. A doping of nickel-based methanation catalysts with iron is described, for example, in CN 104399482 A, CN 104399466 A, CN 104209127 A, CN 102872874 A, CN 101703933 A, CN 101537357 A, WO 2007025691 A1, CN 103706366 A, CN 104028270 A and CN 101745401 A. by Pandey et al., Journal of Industrial and Engineering Chemistry (2016), 33, 99-107, and Gao, et al., RSC Advances (2015), 5 (29), 22759-22776.
CN 104399482 A und CN 104399466 A offenbaren einen mit natürlichem Erz beladenen eisenhaltigen Nickelkatalysator zur Methanisierung und die Herstellung desselben. Nickeloxid macht 2 bis 15 Gew.-% des Katalysators aus. Basierend auf der Redox-Kapazität des Trägers und der entstehenden Wechselwirkung zwischen Eisen und der Nickel-Beladung und auf den Maßnahmen zur Anpassung der Nickel-Beladungskapazität, der Kalzi- nierungstemperatur des Trägers, der Kalzinierungstemperatur des Katalysators, der Reduktionstemperatur des Katalysators und dergleichen, wird ein bimetallischer Eisen-Nickel- Methanisierungskatalysator hergestellt. Der so hergestellte Katalysator zeichnet sich durch eine geringe Nickel-Beladungskapazität, hohe Aktivität, gute Stabilität, hohe Festigkeit und dergleichen aus. Der Katalysator eignet sich für ein Verfahren zur C02/CO-Methanisierung von Koksofengas-, Kohle- oder Biomassen-basiertem Synthese Gas und dergleichen unter diversen H/C-Verhältnissen. CN 104209127 A betrifft einen bimetallischen Nickel/Eisen-Methanisierungskatalysator und die Herstellung sowie die Anwendung desselben. In einem Verhältnis von 0,7 bis 1 ml an löslicher Salzlösung zu 1 g an Aluminiumoxidträger wird der Aluminiumoxidträger in der hergestellten löslichen Salzlösung getaucht. In einem Verhältnis von 0,7 bis 1 ml einer löslichen Nickelsalz Lösung zu 1 g des das Additiv-enthaltenden Trägers wird der Träger in der Nickelsalzlösung getaucht, um einen Nickel-enthaltenden Träger zu erhalten. In einem Verhältnis von 0,7 bis 1 ml einer Eisensalzlösung zu 1 g des Nickel-enthaltenden Trägers
wird der Nickel-enthaltende Träger in der Eisensalz-Lösung getaucht, um anschließend getrocknet und kalziniert zu werden, um einen Katalysator zu erhalten, der 2,5 bis 10 Gew.- % Nickeloxid, 2,5 bis 10 Gew.-% Eisenoxid, 0,01 bis 5 Gew.-% eines Additivs enthält, wobei das Additiv mindestens ein Element ist, ausgewählt aus Lanthan, Cer, Barium, und Magne- sium. Der so hergestellte Katalysator weist in der Tieftemperatur-Methanisierung eine stark erhöhte Aktivität auf, weist reduzierte Kosten auf und verbessert die Methanselektivität und die Stabilität. CN 104399482 A and CN 104399466 A disclose a natural ore loaded iron containing nickel catalyst for methanization and the production thereof. Nickel oxide makes up 2 to 15% by weight of the catalyst. Based on the redox capacity of the carrier and the resulting interaction between iron and the nickel loading and the measures for adjusting the nickel loading capacity, the calcination temperature of the carrier, the calcination temperature of the catalyst, the reduction temperature of the catalyst and the like made a bimetallic iron-nickel methanation catalyst. The catalyst thus prepared is characterized by a low nickel loading capacity, high activity, good stability, high strength and the like. The catalyst is useful in a process for C0 2 / CO methanation of coke oven gas, coal or biomass based synthesis gas and the like under various H / C ratios. CN 104209127 A relates to a bimetallic nickel / iron methanation catalyst and the preparation and use thereof. In a ratio of 0.7 to 1 ml of soluble salt solution to 1 g of alumina carrier, the alumina carrier is immersed in the prepared soluble salt solution. In a ratio of 0.7 to 1 ml of a soluble nickel salt solution to 1 g of the additive-containing carrier, the carrier is immersed in the nickel salt solution to obtain a nickel-containing carrier. In a ratio of 0.7 to 1 ml of an iron salt solution to 1 g of the nickel-containing carrier the nickel-containing carrier is dipped in the iron salt solution to be subsequently dried and calcined to obtain a catalyst containing 2.5 to 10% by weight of nickel oxide, 2.5 to 10% by weight of iron oxide, 0.01 to 5 wt .-% of an additive, wherein the additive is at least one element selected from lanthanum, cerium, barium, and magnesium. The catalyst thus prepared exhibits a greatly increased activity in cryogenic methanation, has reduced costs and improves methane selectivity and stability.
CN 102872874 A betrifft einen auf Nickel basierenden beladenen Katalysator, der zur Me- thanisierung in einer Suspension verwendet wird, ein Herstellungsverfahren und die Anwendung desselben. Der auf Nickel basierende beladene Katalysator besteht aus 10 bis 40 Gew.-% NiO, 56 bis 90 Gew.-% eines Trägers und 0 bis 4 Gew.-% eines Hilfsstoffs. Der auf Nickel basierende beladene Katalysator wird hergestellt durch die Schritte des Herstellens einer löslichen Salzlösung mit 0,5 bis 1 ,3 g/ml Nickelnitrat und des Hilfsstoffs; des nachei- nander Hinzugebens eines Katalysatorträgers und eines löslichen organischen Brennstoffs zur Salzlösung; des Imprägnierens für 6 bis 24 Stunden unter Rühren; des Erhitzens der Lösung, zur Konzentration, in einem Wasserbad bei einer Temperatur von 60 bis 90 °C, nach der Imprägnation oder Erhitzen zur direkten Entzündung der Lösung bei einer Temperatur von 300 bis 700 °C; des Isolierens des nach der Verbrennung verbleibenden Pul- vers, des Vermahlens und Granulierens des Pulvers und des Reduzierens für 2 bis 6 Stunden mit einem reduzierenden Gas in einem Festbettreaktor bei einer Temperatur von 500 bis 700 °C. CN 102872874 A relates to a nickel-based loaded catalyst used for the methylation in a suspension, a production process and the use thereof. The nickel-based loaded catalyst consists of 10 to 40% by weight of NiO, 56 to 90% by weight of a carrier and 0 to 4% by weight of an adjuvant. The nickel-based loaded catalyst is prepared by the steps of preparing a soluble salt solution with 0.5 to 1.3 g / ml nickel nitrate and the excipient; adding a catalyst carrier and a soluble organic fuel to the salt solution in tandem; impregnation for 6 to 24 hours with stirring; heating the solution, for concentration, in a water bath at a temperature of 60 to 90 ° C, after impregnation or heating to directly ignite the solution at a temperature of 300 to 700 ° C; isolating the post-combustion powder, grinding and granulating the powder, and reducing for 2 to 6 hours with a reducing gas in a fixed bed reactor at a temperature of 500 to 700 ° C.
CN 101537357 A betrifft einen aus synthetischem Gas hergestellten Methanisierungskata- lysator. Der Methanisierungskatalysator umfasst die folgenden Komponenten: 1 bis 20 % Eisenoxid, 1 bis 30 % Kobaltoxid, 1 bis 30 % Nickeloxid, 0 bis 10 % eines Seltenerdoxids, 0 bis 10 % Molybdänoxid und 50 bis 97 % Siliziumcarbid-Träger. Die Herstellung des Me- thanisierungskatalysators umfasst das Siliziumcarbid-Material, welches chemisch stabil und eine gute thermische Leitfähigkeit aufweist, als Katalysatorträger zur Herstellung eines Methanisierungskatalysators durch synthetisches Gas. CN 101537357 A relates to a methanation catalyst produced from synthetic gas. The methanation catalyst comprises the following components: 1 to 20% iron oxide, 1 to 30% cobalt oxide, 1 to 30% nickel oxide, 0 to 10% of a rare earth oxide, 0 to 10% molybdenum oxide, and 50 to 97% silicon carbide support. The preparation of the methanation catalyst comprises the silicon carbide material, which is chemically stable and has good thermal conductivity, as a catalyst support for producing a methanation catalyst by synthetic gas.
WO 2007025691 A1 betrifft ein Verfahren zur Hydrogenierung von Kohlenstoff-Oxiden umfassend das Kontaktieren einer Gasmischung enthaltend Kohlenstoffoxide und Wasserstoff mit einem Katalysator, umfassend eine bimetallische Eisen-Nickel- oder Eisen-Kobalt-Le- gierung als aktives Katalysatormaterial, aufgebracht auf einem oxidischen Träger. Der Träger weist vorzugsweise eine Oberfläche >20 m2/g auf.
CN 103706366 A beschreibt einen Katalysator umfassend 15 bis 55 % einer aktiven Komponente, 1 bis 6 % eines 1 . katalytischen Promotors, 3 bis 15 % eines 2. katalytischen Promotors und im Übrigen einen katalytischen Träger, wobei die aktive Komponente Nickeloxid ist, der katalytische Träger Al203 ist, der 1 . katalytische Promotor einer ist, ausge- wählt aus Lanthanoxid, Ceroxid oder Samariumoxid, der 2. katalytische Promotor mindestens einer ist aus Magnesiumoxid, Manganoxid, Eisenoxid und Zirkonoxid. Die Herstellungsmethode umfasst die Schritte: Auflösen eines Reduktionsmittels in Wasser, um eine reduzierende Lösung zu erhalten, Einmischen von Nickelnitrat, Aluminiumnitrat, dem 1 . Metallsalz und dem 2. Metallsalz in Wasser, um eine Rohmateriallösung zu erhalten und Hin- zugeben der reduzierenden Mischung zur Rohmateriallösung unter gleichmäßigen Rühren, um eine 1 . Lösung zu erhalten, Hinzugeben einer Alkali-Lösung zur 1 . Lösung unter starkem Rühren, um eine 2. Lösung zu erhalten, Übertragen in einen abgedichteten Reaktor und Durchführen einer Reaktion bei 100 bis 200 °C für 10 bis 15 Stunden, Kühlen auf Raumtemperatur, Filtrieren und Waschen bis zu einem pH-Wert von 6 bis 7, Trocknen bei 80 bis 120 °C für 4 bis 30 Stunden und Kalzinieren bei 300 bis 550 °C für 2 bis 12 Stunden, um einen Katalysator zu erhalten, in dem das Reduktionsmittel eines ist ausgewählt aus Formaldehyd, Hydrazin-Hydrat, Natriumhypophosphit und Ascorbinsäure, wobei das 1 . Metallsalz eines ist, ausgewählt aus Lanthannitrat, Cernitrat und Samariumnitrat, das 2. Metallsalz mindestens eines ist ausgewählt aus Magnesiumnitrat, Manganitrat, Eisennitrat und Zirkonnitrat, die Alkali-Lösung eine wässrige Lösung aus Natriumcarbonat, Natriumhydroxid, Kaliumcarbonat, Ammoniumcarbonat, Harnstoff oder NH3 * H20 ist. Der Katalysator kann mit einem Bindemittel (Calciumaluminat), einem Schmiermittel (Graphit) und Wasser vermischt werden und dann in Partikelform gepresst werden. Der Katalysator ist zur Metha- nisierung von Kohlegas bei hoher Temperatur und hohem Druck geeignet, um syntheti- sches Erdgas zu produzieren. WO 2007025691 A1 relates to a process for the hydrogenation of carbon oxides comprising contacting a gas mixture containing carbon oxides and hydrogen with a catalyst comprising a bimetallic iron-nickel or iron-cobalt alloy as an active catalyst material, applied to an oxidic support. The support preferably has a surface area> 20 m 2 / g. CN 103706366 A describes a catalyst comprising 15 to 55% of an active component, 1 to 6% of a 1. catalytic promoter, 3 to 15% of a second catalytic promoter and, moreover, a catalytic support, wherein the active component is nickel oxide, the catalytic support is Al 2 O 3 , the 1. catalytic promoter is one selected from lanthanum oxide, cerium oxide or samarium oxide, the second catalytic promoter is at least one of magnesium oxide, manganese oxide, iron oxide and zirconium oxide. The production method comprises the steps of dissolving a reducing agent in water to obtain a reducing solution, mixing in nickel nitrate, aluminum nitrate, the 1. Metal salt and the 2nd metal salt in water to obtain a raw material solution and adding the reducing mixture to the raw material solution with uniform stirring to obtain a 1. To obtain solution, adding an alkali solution to the 1st Solution with vigorous stirring to obtain a 2nd solution, transfer to a sealed reactor and conduct a reaction at 100 to 200 ° C for 10 to 15 hours, cool to room temperature, filter and wash to pH 6 to 7, drying at 80 to 120 ° C for 4 to 30 hours and calcining at 300 to 550 ° C for 2 to 12 hours to obtain a catalyst in which the reducing agent is one selected from formaldehyde, hydrazine hydrate, sodium hypophosphite and Ascorbic acid, wherein the 1. A metal salt of at least one selected from magnesium nitrate, manganese nitrate, iron nitrate and zirconium nitrate, the alkali metal solution is an aqueous solution of sodium carbonate, sodium hydroxide, potassium carbonate, ammonium carbonate, urea or NH 3 * H 2 0 is. The catalyst may be mixed with a binder (calcium aluminate), a lubricant (graphite) and water and then pressed in particulate form. The catalyst is suitable for the methanation of coal gas at high temperature and high pressure to produce synthetic natural gas.
CN 104028270 A offenbart einen Methanisierungskatalysator umfassend 5 bis 60 Gew.-% einer katalytisch aktiven NiO-Komponente, basierend auf dem Gesamtgewicht des Katalysators und im Übrigen Al203, der auch 1 bis 25 Gew.-%, basierend auf dem Gesamtgewicht des Katalysators, an mitwirkender Komponente M umfassen kann, wobei die mitwirkende Komponente M ausgewählt ist aus einem oder mehreren Oxiden der Metalle Ce, Ca, Co, La, Sm, Zr, Ba, Mn, Fe, Mo, Ti und Cu. Das Dokument stellt auch ein Verfahren zur Herstellung des Methanisierungskatalysators zur Verfügung, welches das Mischen der Vorstufe der katalytisch aktiven Komponente, der Vorstufe der mitwirkenden Komponente M sowie eines Katalysatorträgers - gemäß dem entsprechend Anteil in der Methanisierungs- katalysatorzusammensetzung -, das Hinzugeben eines organischen Brennstoffes und das
gründliche Vermischen und Trocknen, um ein gelartiges Produkt zu formen, das Durchführen einer Verbrennungsreaktion, das Säubern und das Trocknen, um das endgültige Produkt zu erhalten, beinhaltet. CN 104028270 A discloses a methanation catalyst comprising 5 to 60 wt .-% of a catalytically active NiO component, based on the total weight of the catalyst and otherwise Al 2 0 3 , which also 1 to 25 wt .-%, based on the total weight of Catalyst, may participate in participating component M, wherein the co-acting component M is selected from one or more oxides of the metals Ce, Ca, Co, La, Sm, Zr, Ba, Mn, Fe, Mo, Ti and Cu. The document also provides a method of making the methanation catalyst which comprises mixing the precursor of the catalytically active component, the precursor of the co-acting component M and a catalyst support according to the proportion in the methanation catalyst composition, adding an organic fuel and the thoroughly mixing and drying to form a gel-like product, carrying out a combustion reaction, cleaning and drying to obtain the final product.
CN 101745401 offenbart einen geträgerten schwefelresistenten Methanisierungs-Katalysa- tor, welcher sich dadurch auszeichnet, dass er ein Hauptmetall M als aktive Komponente, ein 2. Metall M1 als Hilfsstoff und S als Trägermaterial beinhaltet, wobei das Gewichtsverhältnis zwischen M1 , M und S zwischen 0,01 bis 39 : 1 bis 30 : 0,01 bis 90 ist, M eines oder mehrere aus Mo, W und/oder V ist, das 2. Metall M1 eines oder mehrere aus Fe, Co, Ni, Cr, Mn, La, Y oder/und Ce ist und der Träger S Zr02, Al203, MgO oder Ti02 ist. Der geträ- gerte schwefelresistente Methanisierungskatalysator wird durch eine Sol-Gel- Methode dargestellt. CN 101745401 discloses a supported sulfur-resistant methanation catalyst which is characterized in that it comprises a main metal M as active component, a second metal M1 as auxiliary and S as support material, the weight ratio between M1, M and S being between 0 Where M is one or more of Mo, W and / or V, the second metal M1 is one or more of Fe, Co, Ni, Cr, Mn, La , Y and / or Ce and the support S Zr0 2 , Al 2 0 3 , MgO or Ti0 2 . The supported sulfur-resistant methanation catalyst is prepared by a sol-gel method.
Es ist Aufgabe der Erfindung einen Methanisierungskatalysator zur Methanisierung von Kohlenmonoxid und/oder Kohlendioxid bereitzustellen, der bei hoher Aktivität und Selekti- vität eine gegenüber Katalysatoren des Stands der Technik verbesserte Stabilität aufweist. It is the object of the invention to provide a methanation catalyst for the methanation of carbon monoxide and / or carbon dioxide which, with high activity and selectivity, has an improved stability compared to catalysts of the prior art.
Diese Aufgabe wird gelöst durch einen Katalysator zur Methanisierung von Kohlenmonoxid und/oder Kohlendioxid, umfassend Aluminiumoxid und eine Ni-Aktivmasse, welche Fe enthält, dadurch gekennzeichnet, dass das molare Ni/Fe-Verhältnis im Katalysator 4,0 bis 25,0, bevorzugt 5,0 bis 10,0 und besonders bevorzugt 5,0 bis 6,0 beträgt. This object is achieved by a catalyst for the methanation of carbon monoxide and / or carbon dioxide comprising aluminum oxide and a Ni active composition which contains Fe, characterized in that the molar Ni / Fe ratio in the catalyst is 4.0 to 25.0, preferably 5.0 to 10.0, and more preferably 5.0 to 6.0.
Mit der Stabilität des Katalysators im Sinne der Anmeldung ist die Eigenschaft des Katalysators gemeint, unter Reaktionsbedingungen möglichst wenig zu desaktivieren und die hohe Selektivität/Aktivität möglichst beizubehalten. The stability of the catalyst in the sense of the application means the property of the catalyst to deactivate as little as possible under reaction conditions and to maintain the high selectivity / activity as far as possible.
Bei dem Aluminiumoxid muss es sich nicht um stöchiometrisches AI2O3 handeln, vielmehr kann es sich hierbei auch um ein nicht-stöchiometrisches Aluminiumoxid handeln. The alumina need not be stoichiometric Al 2 O 3, but may be a non-stoichiometric alumina.
Auch kann das molare Ni/Fe-Verhältnis im Bereich von 4,5 bis 8,0 liegen, vorzugsweise im Bereich von 5,0 bis 7,0, ganz besonders bevorzugt im Bereich 5,3 bis 5,5. Also, the molar Ni / Fe ratio may be in the range of 4.5 to 8.0, preferably in the range of 5.0 to 7.0, most preferably in the range of 5.3 to 5.5.
Der Promotor Fe kann vollständig oder teilweise in der Ni-Aktivmasse enthalten sein. Der Katalysator kann neben Fe weitere Promotoren enthalten, er kann aber auch ausschließlich den Promotor Fe enthalten. Die Oxidationsstufen von AI, Ni sowie der Promotoren können je nach Behandlung des Katalysators variieren. AI, Ni und die Promotoren liegen typischerweise als Metallkationen (z.B. Al3+, Ni2+, Fe2+, Fe3+) vor. Nach der Kalzinierung, z.B. an Luft, können hohe Oxidationsstufen bzw. die maximalen Oxidationsstufen erreicht werden. Wird
der Katalysator bei Temperaturen oberhalb Raumtemperatur reduziert, z.B. unter Reaktionsbedingungen mit Wasserstoff, können AI, Ni und die Promotoren niedrigere Oxidations- stufen annehmen oder teilweise oder ganz in der Oxidationsstufe 0 auftreten. Der Ladungsausgleich zu den Metallkationen erfolgt durch negativ geladene Sauerstoffatome (02~). The promoter Fe may be contained completely or partially in the Ni active material. The catalyst may contain other promoters in addition to Fe, but it may also contain exclusively the promoter Fe. The oxidation states of Al, Ni and the promoters can vary depending on the treatment of the catalyst. Al, Ni and the promoters are typically present as metal cations (eg, Al 3+, Ni 2+, Fe 2+, Fe 3+). After calcination, eg in air, high oxidation states or the maximum oxidation states can be achieved. Becomes the catalyst is reduced at temperatures above room temperature, for example under reaction conditions with hydrogen, AI, Ni and the promoters can assume lower oxidation states or occur partially or completely in the oxidation state 0. The charge balance to the metal cations is carried out by negatively charged oxygen atoms (0 2 ~ ).
Der erfindungsgemäße Katalysator kann weitere Komponenten, neben Aluminiumoxid (AlOx mit x <1 ,5) Ni, und Fe (sowie die zum Ladungsausgleich notwendigen Sauerstoffanio- nen) enthalten, er kann jedoch auch ausschließlich aus Aluminiumoxid, Ni und Fe bestehen. Auch kann die Ni-Aktivmasse neben Fe weitere Promotoren enthalten, sie kann aber auch ausschließlich den Promotor Fe enthalten. Letzteres hat den Vorteil, dass dann die Aktivmasse bzw. der Katalysator aus vergleichsweise preiswerten und wenig toxischen Elementen besteht. Vorzugsweise enthält der Katalysator keines der Elemente ausgewählt aus Ta, In, Cu, Ce, Cr, Bi, Mn, P, B, Sb, Sn, Si, Ti, Zr, Co, Rh, Ru, Ag, Ir, Pd und Pt. Vorzugsweise enthält der Katalysator kein Edelmetall. Vorzugsweise enthält der Katalysator nicht Mn. The catalyst according to the invention may contain other components besides aluminum oxide (AlO x with x <1.5) Ni and Fe (as well as the oxygen anions necessary for charge equalization), but it may also consist exclusively of aluminum oxide, Ni and Fe. Also, the Ni active material in addition to Fe may contain further promoters, but it may also contain only the promoter Fe. The latter has the advantage that then the active material or the catalyst consists of comparatively inexpensive and less toxic elements. Preferably, the catalyst does not contain any of the elements selected from Ta, In, Cu, Ce, Cr, Bi, Mn, P, B, Sb, Sn, Si, Ti, Zr, Co, Rh, Ru, Ag, Ir, Pd and Pt , Preferably, the catalyst does not contain a noble metal. Preferably, the catalyst does not contain Mn.
Das atomare Al/Ni-Verhältnis kann zwischen 0,5 und 1 ,5 sein, bevorzugterweise zwischen 0,8 und 1 ,2, besonders bevorzugt ist das Al/Ni-Verhältnis annähernd 1 . The atomic Al / Ni ratio may be between 0.5 and 1.5, preferably between 0.8 and 1.2, more preferably the Al / Ni ratio is approximately 1.
Die erfindungsgemäßen Katalysatoren können vorteilhafterweise in der Ni-Aktivmasse Kristallite mit einem Durchmesser unter 20 nm, bevorzugt unter 10 nm, aufweisen. Die Ni- Aktivmasse kann auch ganz oder zu wesentlichen Teilen aus Kristalliten mit einem Durchmesser unter 20 nm, bevorzugt unter 10 nm bestehen. Die Ni-Aktivmasse liegt vorzugsweise in einem metallischen Zustand vor. Die C02-Aufnahmekapazität der Katalysatoren bei 35°C kann größer 150 μηιοΙ/g sein und liegt vorzugsweise im Bereich zwischen 150 bis 250 μηιοΙ/g, besonders bevorzugt, zwischen 180 bis 210 μηιοΙ/g. The catalysts according to the invention can advantageously have crystallites in the Ni active composition with a diameter of less than 20 nm, preferably less than 10 nm. The Ni active material may also consist entirely or substantially of crystallites with a diameter of less than 20 nm, preferably less than 10 nm. The Ni active material is preferably in a metallic state. The C0 2 absorption capacity of the catalysts at 35 ° C may be greater than 150 μηιοΙ / g and is preferably in the range between 150 to 250 μηιοΙ / g, more preferably, between 180 to 210 μηιοΙ / g.
Die BET-Oberfläche (SBET) des erfindungsgemäßen Katalysators kann größer als 100 m2/g sein, vorzugsweise größer als 200 m2/g, oder im Bereich zwischen 200 und The BET surface area (SBET) of the catalyst according to the invention may be greater than 100 m 2 / g, preferably greater than 200 m 2 / g, or in the range between 200 and
400 m2/g, vorzugsweise im Bereich zwischen 200 und 300 m2/g und insbesondere im Bereich zwischen 200 und 250 m2/g. 400 m 2 / g, preferably in the range between 200 and 300 m 2 / g and in particular in the range between 200 and 250 m 2 / g.
Die spezifische Metalloberfläche (Swiet) des erfindungsgemäßen Katalysators ist vorzugs- weise größer als 5 m2/g, vorzugsweise größer als 10 m2/g, oder im Bereich zwischen 5 und 25 m2/g, vorzugsweise im Bereich zwischen 10 und 20 m2/g, oder im Bereich zwischen 9 und 12 m2/g.
Weiterhin betrifft die Erfindung ein Verfahren zur Herstellung eines Methanisierungskata- lysators, umfassend die Schritte: The specific metal surface area (Swiet) of the catalyst according to the invention is preferably greater than 5 m 2 / g, preferably greater than 10 m 2 / g, or in the range between 5 and 25 m 2 / g, preferably in the range between 10 and 20 m 2 / g, or in the range between 9 and 12 m 2 / g. Furthermore, the invention relates to a process for the preparation of a methanation catalyst, comprising the steps:
a) Kopräzipitation aus einer Lösung, die AI, Ni und Fe in gelöster Form enthält, um einen Niederschlag zu erhalten, a) co-precipitation from a solution containing Al, Ni and Fe in dissolved form to obtain a precipitate,
b) Isolieren des Niederschlags aus Schritt a), b) isolating the precipitate from step a),
c) Trocknen des isolierten Niederschlags aus Schritt b) und c) drying the isolated precipitate from step b) and
d) Kalzinieren des getrockneten Niederschlags aus Schritt c). Bevorzugt ist hierbei, dass die Lösung aus Schritt a) eine wässrige Lösung ist und AI, Ni und Fe in der wässrigen Lösung gelöst als ionische Verbindungen vorliegen. d) calcining the dried precipitate from step c). It is preferred here that the solution from step a) is an aqueous solution and Al, Ni and Fe are present dissolved in the aqueous solution as ionic compounds.
AI liegt bevorzugterweise gelöst als Aluminiumnitrat, Aluminiumtrichlorid oder Aluminiumsulfat vor. Ni liegt bevorzugter Weise gelöst als Nickelnitrat, Nickeldichlorid, Nickelsulfat, Nickelacetat oder Nickelcarbonat vor. Fe liegt bevorzugterweise in der Oxidationsstufe II oder III vor und ist als Eisennitrat, Eisenbi- oder trichlorid, Eisenacetat, Eisensulfat oder Eisenhydroxid gelöst. Al is preferably dissolved as aluminum nitrate, aluminum trichloride or aluminum sulfate. Ni is preferably dissolved as nickel nitrate, nickel dichloride, nickel sulfate, nickel acetate or nickel carbonate. Fe is preferably in the oxidation state II or III and is dissolved as iron nitrate, iron or trichloride, iron acetate, iron sulfate or iron hydroxide.
Bevorzugterweise, liegen AI, Ni und Fe in gelöster Form, als ionische Verbindungen in der wässrigen Lösung vor und weisen dasselbe Anion auf, welches zum Beispiel Nitrat sein kann. Preferably, Al, Ni and Fe are in dissolved form as ionic compounds in the aqueous solution and have the same anion, which may be, for example, nitrate.
Die Kopräzipitation erfolgt durch Hinzugeben der Lösung, die AI, Ni und Fe enthält, zu einer vorgelegten basischen Lösung oder durch Zugabe einer basischen Lösung zu der vorge- legten Lösung die AI, Ni und Fe enthält. Alternativ wird die Lösung, die AI, Ni und Fe enthält und die basische Lösung gleichzeitig in ein Gefäß gegeben, welche bereits ein Lösungsmittel wie Wasser enthalten kann und wird darin vermischt. Die basische Lösung weist einen pH größer 7, vorzugsweise im Bereich von 8 bis 10 auf und enthält bevorzugterweise ein Alkali-Hydroxid und/oder ein Alkali-Carbonat. Zum Beispiel ist die basische Lösung eine wässrige Lösung aus Natriumhydroxid und Natriumcarbonat. Die Kopräzipitation erfolgt vorzugsweise unter Temperierung, sodass die Temperatur der Lösung annähernd Raumtemperatur oder zum Beispiel 30 °C beträgt. The coprecipitation is carried out by adding the solution containing Al, Ni and Fe to a basic solution or by adding a basic solution to the proposed solution containing Al, Ni and Fe. Alternatively, the solution containing Al, Ni and Fe and the basic solution are simultaneously added to a vessel which may already contain a solvent such as water and is mixed therein. The basic solution has a pH greater than 7, preferably in the range of 8 to 10, and preferably contains an alkali hydroxide and / or an alkali carbonate. For example, the basic solution is an aqueous solution of sodium hydroxide and sodium carbonate. The coprecipitation is preferably carried out under temperature control, so that the temperature of the solution is approximately room temperature or, for example, 30 ° C.
Nach der Fällung durch die Kopräzipitation wird vorzugsweise der Niederschlag in der Lö- sung für mindestens 30 Minuten, bevorzugterweise länger als 1 Stunde, stärker bevorzugt
länger als 12 Stunden gealtert. Die Alterung erfolgt vorzugsweise dadurch, dass der Niederschlag bei annähernd Raumtemperatur in der Lösung (Mutterlauge) unter Rühren belassen wird. Der durch die Kopräzipitation erhaltene Niederschlag wird isoliert, zum Beispiel indem eine Filterung durchgeführt wird. Die Filterung kann in geeigneter Weise zum Beispiel durch eine Filterpresse erfolgen. After precipitation by coprecipitation, the precipitate in the solution is preferably more preferably for at least 30 minutes, preferably longer than 1 hour aged for more than 12 hours. The aging is preferably carried out by stirring the precipitate at approximately room temperature in the solution (mother liquor). The precipitate obtained by the coprecipitation is isolated, for example by filtering. The filtering can be done in a suitable manner, for example by a filter press.
Der isolierte Niederschlag wird vorzugsweise gewaschen, zum Beispiel mit destilliertem Wasser, bis ein neutraler pH-Wert erreicht wird. The isolated precipitate is preferably washed, for example with distilled water, until a neutral pH is reached.
Im Folgenden kann der isolierte Niederschlag getrocknet werden, zum Beispiel bei erhöhter Temperatur an Luft. Bevorzugterweise erfolgt die Trocknung bei einer Temperatur zwischen 70 °C und 90 °C für einen Zeitraum länger als 4 Stunden, vorzugsweise länger als 12 Stun- den. In the following, the isolated precipitate can be dried, for example at elevated temperature in air. Preferably, the drying takes place at a temperature between 70 ° C and 90 ° C for a period longer than 4 hours, preferably longer than 12 hours.
Der isolierte Niederschlag wird kalziniert, dies kann an Luft bei einer Temperatur zwischen 300 °C bis 600 °C erfolgen, bevorzugterweise 400 °C bis 500 °C und in einem Zeitraum von 3 bis 10 Stunden, bevorzugterweise 5 bis 7 Stunden. The isolated precipitate is calcined, this can be done in air at a temperature between 300 ° C to 600 ° C, preferably 400 ° C to 500 ° C and in a period of 3 to 10 hours, preferably 5 to 7 hours.
Der erfindungsgemäße Katalysator soll insbesondere in der Methanisierung von Kohlenmonoxid und/oder Kohlendioxid Verwendung finden. Die Methanisierung von Kohlendioxid lässt sich durch die folgende Reaktionsgleichung darstellen: 4H2 + C02 -> CH4 + 2H20 The catalyst according to the invention is intended to be used in particular in the methanation of carbon monoxide and / or carbon dioxide. The methanation of carbon dioxide can be represented by the following reaction equation: 4H 2 + C0 2 -> CH 4 + 2H 2 0
Die Methanisierung von Kohlenmonoxid lässt sich durch die folgende Reaktionsgleichung darstellen: The methanation of carbon monoxide can be represented by the following reaction equation:
3H2 + CO -> CH4 + H20 3H 2 + CO -> CH 4 + H 2 O
Bei dem Verfahren zur Durchführung der Methanisierung wird das Reaktionsgas, welches Kohlendioxid und/oder Kohlenmonoxid oder ein Gemisch aus beidem enthält, bei einer Temperatur oberhalb von 200 °C mit dem Katalysator in Kontakt gebracht. Die Figuren zeigen das katalytische Verhalten der eisendotierten Katalysatoren Fe2, Fe4, Fe7 und Fe10 jeweils vor und nach Alterung.
Figur 1 : Katalytische Testergebnisse zu Fe2 (Beispiel). In the method for carrying out the methanation, the reaction gas containing carbon dioxide and / or carbon monoxide or a mixture of both is contacted with the catalyst at a temperature higher than 200 ° C. The figures show the catalytic behavior of the iron-doped catalysts Fe2, Fe4, Fe7 and Fe10 before and after aging. Figure 1: Catalytic test results for Fe2 (example).
Figur 2: Katalytische Testergebnisse zu Fe4 (Beispiel). Figure 2: Catalytic test results for Fe4 (example).
Figur 3: Katalytische Testergebnisse zu Fe7 (Beispiel). FIG. 3: Catalytic test results for Fe7 (example).
Figur 4: Katalytische Testergebnisse zu Fe10 (Vergleichsbeispiel). Figur 5: Normierte WTY(CH4) als Funktion der Alterungsdauer für Fe7ll im Vergleich zu Nill bei einer Alterungstemperatur von 450 °C. FIG. 4: Catalytic test results for Fe10 (comparative example). FIG. 5: Normalized WTY (CH4) as a function of the aging time for Fe711 in comparison to Nill at an aging temperature of 450 ° C.
Figur 6: Normierte WTY(CH4) als Funktion der Alterungsdauer für Fe7ll im Vergleich zu Nill bei einer Alterungstemperatur von 350 °C. FIG. 6: Normalized WTY (CH4) as a function of the aging time for Fe711 in comparison to Nill at an aging temperature of 350 ° C.
Methoden methods
Elementaranalyse Elemental analysis
Die Bestimmung der Zusammensetzung der kalzinierten Katalysatoren erfolgte durch optische Emissionsspektroskopie mittels induktiv gekoppeltem Plasma (ICP-OES). 50 mg an Katalysator wurden in 50 ml 1 molarer Phosphorsäure (VWR, p.A.) bei 60°C gelöst. Um gebildeten Braunstein zu lösen, wurden zur Lösung 50 mg Na2S03 (Sigma Aldrich, p.A.) zugegeben. Nach Abkühlung wurden die Lösungen 1 /10 verdünnt und mittels 0,1 μηι Filtern (Pall) gefiltert. Die Kalibrierlösungen wurden zu 1 , 10 und 50 mg I-1 (Merck) angesetzt. Die Bestimmung der Metallkonzentrationen wurde mittels eines Agilent 700 ICP-OES durchgeführt. The determination of the composition of the calcined catalysts was carried out by means of inductively coupled plasma optical emission spectroscopy (ICP-OES). 50 mg of catalyst were dissolved in 50 ml of 1 molar phosphoric acid (VWR, pA) at 60 ° C. To dissolve any brownstone formed, 50 mg Na 2 S0 3 (Sigma Aldrich, pA) was added to the solution. After cooling, the solutions were diluted 1/10 and filtered by 0.1 μηι filters (Pall). The calibration solutions were prepared at 1, 10 and 50 mg I -1 (Merck). Determination of metal concentrations was performed using an Agilent 700 ICP-OES.
Bestimmung der spezifischen Oberfläche Die Bestimmung der spezifischen Oberflächen der Katalysatoren (SBET) wurde mittels N2-BET Analyse an einer NOVA 4000e (Quantachrome) durchgeführt. Hierzu wurden 100 mg Katalysator für 3 Stunden bei 120 °C entgast und anschließend Adsorptions- und Desorptionsiso- therme im p/p0-Bereich von 0,007 bis 1 aufgenommen. Zur Bestimmung der BET-Oberfläche wurden die Datenpunkte im p/p0-Bereich von 0,007 bis 0,28 herangezogen. Chemisorption Specific Surface Determination The specific surface area of the catalysts (SBET) was determined by N 2 -BET analysis on a NOVA 4000e (Quantachrome). For this purpose, 100 mg of catalyst were degassed for 3 hours at 120 ° C and then absorbed adsorption and Desorptionsiso- therme in the p / p 0 range of 0.007 to 1. To determine the BET surface area, the data points in the p / p 0 range of 0.007 to 0.28 were used. chemisorption
Chemisorptionsexperimente wurden an einer Autosorb 1 C (Quantachrome) vorgenommen. Vor der Messung wurden 100 mg Katalysator bei 500 °C in 10% H2 in N2 für 6 Stunden aktiviert. Die Heizrampe betrug 2 Kmin-1.
Die Bestimmung der Metalloberfläche (SMET) erfolgte nach DIN 66136-2 (Ver. 2007-01 ) und wurde mittels H2-Chemisorption bei 35°C durchgeführt. Hierfür wurden 20 Adsorptionspunkte äquidistant von 40 mmHg bis 800 mmHg aufgenommen. Die Equilibrierzeit für die Adsorption betrug 2 min, die des thermischen Gleichgewichts 10 min. Zur Bestimmung der Metalloberflä- che wurde eine Metallatom/H-Stöchiometrie von 1 angesetzt. Für die CC Chemisorptionsmes- sungen zur Bestimmung der C02-Aufnahmekapazitäten (U(C02)) wurde bei ansonsten unveränderten Parametern die Equilibrierzeit für die Adsorption auf 10 min gesetzt. Vor Aufnahme der Chemisorptionsdaten wurde eine etwaige kinetische Hemmung der C02-Chemisorption unter diesen Bedingungen experimentell ausgeschlossen. Metalloberflächen und CC Aufnahme- kapazitäten wurden gemäß der Extrapolationsmethode auf einen Druck von 0 mmHg extrapoliert. Chemisorption experiments were performed on an Autosorb 1C (Quantachrome). Before the measurement, 100 mg of catalyst were activated at 500 ° C in 10% H 2 in N 2 for 6 hours. The heating ramp was 2 Kmin -1 . The determination of the metal surface (SMET) was carried out according to DIN 66136-2 (Ver., 2007-01) and was carried out by means of H 2 chemisorption at 35 ° C. For this purpose, 20 adsorption points were recorded equidistant from 40 mmHg to 800 mmHg. The equilibration time for the adsorption was 2 min, the thermal equilibrium 10 min. To determine the metal surface, a metal atom / H stoichiometry of 1 was used. For the CC chemisorption measurements to determine the CO 2 uptake capacities (U (C0 2 )), the equilibration time for the adsorption was set to 10 min with otherwise unchanged parameters. Before the absorption of the chemisorption data, any kinetic inhibition of CO 2 chemisorption under these conditions was experimentally excluded. Metal surfaces and CC uptake capacities were extrapolated to a pressure of 0 mmHg according to the extrapolation method.
In-situ-Röntgenpulverdiffraktometrie In situ X-ray powder
/n-s/fu-Röntgenpulverdiffraktometrie-Messungen (in-situ XRD) von reduzierten und desaktivier- ten Katalysatorproben wurden mit einem STOE Stadi P Diffraktometer unter Verwendung von Cu-Ka-Strahlung, einem Ge(1 1 1 ) Monochromator und einem Dectris MYTHEN 1 K Detektor durchgeführt. Hierfür wurden unter Ar-Atmosphäre etwa 3 mg Katalysatorprobe in Glaskapillaren mit einem Durchmesser von 0,5 mm überführt. Die Kapillare wurde anschließend abgeschmolzen. Die XRD-Daten wurden für 2Θ = 5-90 5 mit 0,5 5 pro Schritt und 1 ,7 Schritten min 1 aufgezeichnet. Die Bestimmung der mittleren Kristallitgrößen der Metallpartikeln wurde nach der Scherrer-Gleichung anhand des Ni(Fe)-Reflexes bei 2Θ = 51 .3-51 .7 durchgeführt. X-ray powder diffraction (in-situ XRD) measurements of reduced and deactivated catalyst samples were performed with a STOE Stadi P diffractometer using Cu-Ka radiation, a Ge (1 1 1) monochromator, and a Dectris MYTHEN 1 K detector performed. For this, about 3 mg of catalyst sample were transferred into glass capillaries with a diameter of 0.5 mm under Ar atmosphere. The capillary was then melted off. The XRD data were recorded for 2Θ = 5-90 5 with 0.5 5 per step and 1, 7 steps min 1 . The determination of the average crystallite sizes of the metal particles was carried out according to the Scherrer equation using the Ni (Fe) reflection at 2Θ = 51 .3-51 .7.
Synthese synthesis
Die Katalysatoren wurden durch Kopräzipitation hergestellt und das atomare Verhältnis von Nickel und Aluminium auf 1 eingestellt. Zur Untersuchung der Wirkung von Eisen auf das Katalysatorverhalten wurde während der Katalysatorsynthese Eisen(lll)-nitrat zur Salzlösung aus Nickel- und Aluminiumnitrat zugegeben. Zur Untersuchung der Wirkung von Mangan auf das Katalysatorverhalten wurde während der Katalysatorsynthese Mangan(ll)-nitrat zur Salzlösung aus Nickel- und Aluminiumnitrat zugegeben. Die Reinheit aller verwendeter Chemikalien war p.a. Wasser wurde durch ein Millipore-Filtersystem aufgereinigt und der Reinheitsgrad mittels Leitfähigkeitsmessungen verifiziert. Die Synthese erfolgte in einem doppelwandigen, 3 I fassenden Rührkessel. Der mit Wasser gefüllte Doppelmantel ermöglichte über einen Thermostaten die Temperierung des Syntheseansatzes auf 30 °C, zwei Strömungsbrecher sorgten für
eine verbesserte Vermischung. Zum Rühren kam ein KPG-Rührer mit 150 Umdrehungen min-The catalysts were prepared by coprecipitation and the atomic ratio of nickel and aluminum was adjusted to 1. To study the effect of iron on catalyst behavior, iron (III) nitrate was added to the salt solution of nickel and aluminum nitrate during catalyst synthesis. To study the effect of manganese on catalyst behavior, manganese (II) nitrate was added to the salt solution of nickel and aluminum nitrate during catalyst synthesis. The purity of all chemicals used was pa Water was purified by a Millipore filter system and the degree of purity verified by conductivity measurements. The synthesis was carried out in a double-walled, 3 l stirred tank. The water-filled double jacket allowed the temperature of the synthesis approach to 30 ° C via a thermostat, two baffles provided for an improved mixing. For stirring, a KPG stirrer with 150 revolutions min.
1 zum Einsatz. Für die Synthese wurde im Rührkessel 1 I H20 vorgelegt und auf pH = 9±0,1 eingestellt. Die Dosierung der Mischung der gelösten Nitrate erfolgte mit 2,5 ml min-1. Zeitgleich diente die kontrollierte Zugabe des Fällungsreagenz zur Aufrechterhaltung des pH-Werts. Als Ausgangsstoffe kamen einmolare Lösungen der jeweiligen Nitrate zum Einsatz (Ni(N03)2 * 6H20, AI(N03)3 * 9H20, Fe(N03)3 * 9H20 und Mn(N03)2 * 4H20). Diese wurden, wie in Tabelle 1 for use. For the synthesis, 1H 2 0 was placed in the stirred tank and adjusted to pH = 9 ± 0.1. The dosage of the mixture of dissolved nitrates was 2.5 ml min -1 . At the same time, the controlled addition of the precipitating reagent was used to maintain the pH. As starting materials molar solutions of the respective nitrates were used (Ni (N0 3) 2 * 6H 2 0, AI (N0 3) 3 * 9H 2 0, Fe (N0 3) 3 * 9H 2 0 and Mn (N0 3) 2 * 4H 2 0). These became, as in table
2 dargestellt, zu einem Gesamtvolumen von 120 ml min-1 gemischt, bevor das Zutropfen in den Reaktor erfolgte. Als Fällungsreagenz diente eine volumengleiche Mischung aus den Lösungen 0.5M NaOH und 0.5 M Na2C03, zu deren Dosierung ein Titrator verwendet wurde. Unter stän- digem Rühren wurde die Suspension über Nacht in der Mutterlauge gealtert, der Niederschlag anschließend abfiltriert und so lange mit H20 gewaschen, bis das Filtrat einen neutralen pH- Wert aufwies. Nach einer Trocknung bei 80 °C im Trockenschrank über Nacht wurde der getrocknete Niederschlag (Prekursor) mit einer Aufheizrate von 5 K min-1 auf 450 °C erhitzt und für 6 Stunde unter synthetischer Luft kalziniert. Aktivitäts- und Stabilitätsmessung 2, to a total volume of 120 ml min -1 before dropping into the reactor. The precipitation reagent was a mixture of 0.5M NaOH and 0.5 M Na 2 C0 3 solutions of equal volume, for the metering of which a titrator was used. With constant stirring, the suspension was aged overnight in the mother liquor, the precipitate was then filtered off and washed with H 2 0 until the filtrate had a neutral pH. After drying at 80 ° C in a drying oven overnight, the dried precipitate (precursor) was heated at a heating rate of 5 K min -1 to 450 ° C and calcined for 6 hours under synthetic air. Activity and stability measurement
Um verschiedene Katalysatoren in ihrer Aktivität bezüglich der C02-Methanisierung vergleichen zu können, wurde ein Testprogramm entwickelt, welches eine Aussage zu deren Aktivität und Stabilität liefert. Die Ergebnisse dieses Testprogramms werden in den Figuren 1 bis 4 gezeigt. Dazu wurden 25 mg Katalysator in der Siebfraktion 150 - 200 μηι mit der neunfachen Menge an SiC verdünnt und in den Reaktor eingebaut. Die nacheinander in der Reihenfolge Reduktion, Einlaufen, S-Kurve 1 , Alterung und S-Kurve 2 durchgeführten Messschritte, sind im Detail in Tabelle 1 aufgeführt. In order to be able to compare different catalysts in terms of their activity in terms of C0 2 methanation, a test program was developed which provides information on their activity and stability. The results of this test program are shown in FIGS. 1 to 4. For this purpose, 25 mg of catalyst in the sieve fraction 150-200 μηι were diluted with nine times the amount of SiC and incorporated into the reactor. The measurement steps carried out successively in the order of reduction, shrinkage, S-curve 1, aging and S-curve 2 are listed in detail in Table 1.
Tabelle 1 : Parameter der Messschritte zur Ermittlung des Aktivitäts- und Stabilitätsprofils Table 1: Parameters of the measurement steps for determining the activity and stability profile
Zur Bestimmung der Temperatur-C02-Umsatz-Kurven, wurde die Temperatur im angegebenen Bereich schrittweise um 25 °C erhöht und jeweils die Aktivität bestimmt. Ein Vergleich der beiden S-Kurven vor und nach 32 Stunden Alterung bei 500 °C lässt einen Einblick auf die Stabilität der Systeme hinsichtlich hoher Temperaturen zu. Als Maß für die Aktivität wurde repräsentativ die Temperatur T75,i bestimmt, welche nötig ist, um während des Messschrittes S-Kurve 1 einen C02-Umsatz von 75% zu erreichen. Hierzu wurde die Temperatur im angegebenen Bereich schrittweise um 25 °C erhöht. Je niedriger T75,i ist, desto höher ist daher die Aktivität des Katalysators. To determine the temperature-C0 2 -Umsatz curves, the temperature in the specified range was gradually increased by 25 ° C and each determines the activity. A comparison of the two S-curves before and after 32 hours of aging at 500 ° C gives an insight into the stability of the systems in terms of high temperatures. As a measure of the activity, the temperature T 7 5, i was determined, which is necessary in order to achieve a C0 2 conversion of 75% during the measuring step S-curve 1. For this purpose, the temperature in the specified range was gradually increased by 25 ° C. Therefore, the lower T 7 5, i, the higher the activity of the catalyst.
Als Maß für die Aktivität nach der Alterung wurde repräsentativ die Temperatur T75,2 bestimmt, welche nötig ist, um während des Messschrittes S-Kurve 2 einen C02-Umsatz von 75% zu erreichen. Hierzu wurde die Temperatur im angegebenen Bereich schrittweise um 25 °C erhöht. Je niedriger T75,2 ist, desto höher ist daher die Aktivität des Katalysators nach der Alterung. As a measure of the activity after aging, the temperature T 7 5.2, which is necessary in order to achieve a C0 2 conversion of 75% during the measuring step S-curve 2, was determined representatively. For this purpose, the temperature in the specified range was gradually increased by 25 ° C. The lower T 7 is 5.2, therefore, the higher the activity of the catalyst after aging.
Berechnet man die Differenz der T75,i und T75,2 aus den beiden Umsatz-Temperatur-Charakte- ristika, so erhält man ein Maß für die Stabilität des Katalysators. Auch hier gilt, je niedriger die Differenz, desto stabiler der Katalysator. Zur besseren Vergleichbarkeit wurden alle bestimmten Aktivitäten und Stabilitäten auf die des nicht promotierten Nickel-Aluminiumoxid-Katalysators (Ni) normiert. Solche Ni/AIOx-Katalysatorsysteme sind Stand der Technik, sodass sich dieser Katalysator als Ausgangssystem eignet. Die Normierung ergibt sich aus: Normierte Aktivität = *»/^) Calculating the difference of T 75 , i and T 75 , 2 from the two conversion temperature characteristics, one obtains a measure of the stability of the catalyst. Again, the lower the difference, the more stable the catalyst. For better comparability, all specific activities and stabilities were normalized to those of the un-promoted nickel-alumina (Ni) catalyst. Such Ni / AIO x catalyst systems are known in the art, so this catalyst is suitable as the starting system. The normalization results from: normalized activity = * »/ ^ )
T7S 1(dot. Kat.) T 7S 1 (dot cat.)
T75 2 (Ni/AlOx) T 75 2 (Ni / AlO x )
Normierte Stabilität = T?s (dot. Kat.) Normalized stability = T? S (dot cat.)
T7 S 1 (dot. Kat) T 7 S 1 (dot cat)
Die Ergebnisse in Figur 1 bis 4 zeigen, dass die Promotierung eines Ni/AIOx-Katalysators mit Eisen, bei einem Ni/Fe-Verhältnis im Katalysator von 4,0 bis 25,0, zu einer signifikanten Erhöhung der Katalysatorstabilität führt. In den Figuren 5 und 6 wurde jeweils die normierte WTY(CH4) als Funktion der Alterungsdauer für Nill im Vergleich zu Fe7ll, aufgenommen. Die Messung fand jeweils unter differentiellen Bedingungen bei 230 °C, 4 bar, 600 NIJ(gkat h), H2/C02/Ar = 4/1 /75 statt, die Alterung erfolgte bei 450 °C (Figur 5) und 350 °C (Figur 6) bei jeweils 8 bar, 18 NIJ(gkat h), H2/C02/Ar = 4/1/5. Unter normierter WTY(CH4) (WTY =„weight time yield" auch„Massen-Zeit-Ausbeute") wird der gebildete Massenstrom an Methan pro Katalysatormasse und Zeit, normiert auf die initiale
WTY(CH4) bei t = Oh verstanden. Diese Größe kann als Maß für die Katalysatoraktivität herangezogen werden. The results in FIGS. 1 to 4 show that the promotion of a Ni / AlO x catalyst with iron, with a Ni / Fe ratio in the catalyst of 4.0 to 25.0, leads to a significant increase in the catalyst stability. In Figures 5 and 6, respectively, the normalized WTY (CH4) was recorded as a function of the aging time for Nill compared to Fe711. The measurement took place under differential conditions at 230 ° C., 4 bar, 600 NIJ (g ka th), H 2 / CO 2 / Ar = 4/1/75, the aging took place at 450 ° C. (FIG. 5) and 350 ° C (Figure 6) at 8 bar, 18 NIJ (g cat h), H 2 / C0 2 / Ar = 4/1/5. Under normalized WTY (CH4) (WTY = "weight time yield" also "mass-time yield"), the mass flow of methane formed per catalyst mass and time, normalized to the initial WTY (CH 4 ) at t = Oh understood. This size can be used as a measure of the catalyst activity.
50 mg des kalzinierten Katalysators wurden mit 450 mg Fe-freien SiC (ESK) gemischt und in einen mit Quartzglas-beschichteten Rohrreaktor (Innendurchmesser 4mm) gegeben. Das Ka- talysatorbett wurde mit Quarzwollestopfen fixiert und in der isothermen Zone eines Ofens positioniert. Die Katalysatortemperatur würde über ein Thermoelement im Katalysatorbett gemessen. Der Katalysator wurde mit einer Aufheizrate von 2 K min-1 in 5 % H2 in Ar mit 50 NL min- 1 auf 485 5C erhitzt und dort für 5 h reduziert. 50 mg of the calcined catalyst was mixed with 450 mg Fe-free SiC (ESK) and placed in a quartz glass-coated tube reactor (4 mm ID). The catalyst bed was fixed with quartz wool plugs and positioned in the isothermal zone of a furnace. The catalyst temperature would be measured via a thermocouple in the catalyst bed. The catalyst was contacted with a heating rate of 2 K min-1 in 5% H2 in Ar with 50 min- NL 1 to 485 5 C. and reduced there for 5 h.
Nach Abkühlen auf 230 °C wurde die initiale Katalysatoraktivität unter differentiellen Reaktions- bedingungen bei 4 bar und 600 NL gka 1 lr1 (H2/C02/Ar = 4/1/75, GHSV = 800.000 hr1) gemessen. Zur Alterung wurde der Katalysator mit einer Aufheizrate von 5 K min 1 erhitzt und bei der Alterungstemperatur (350 °C bzw. 450 °C) bei 8 bar und 18 NL gka 1 h 1 gehalten (H2/C02/Ar = 4/1/5, GHSV = 24.000 hr1). Die Alterungszeit betrug 2 h in der anfänglichen Des- aktivierungsbehandlung und 4 h in allen weiteren Behandlungen. Nach jedem Alterungsschritt wurde das Katalysatorbett auf 230 °C abgekühlt, bevor die Katalysatoraktivität unter den oben genannten Bedingungen erneut bestimmt wurde, um die Katalysatordesaktivierung im kinetischen Regime unter Bedingungen frei von Produkt- oder Gleichgewichtslimitierungen zu verfolgen. Diese Zyklen wurden wiederholt, um Katalysatoren zu erhalten, die für 0, 6, 40 und 72 h gealtert waren. Die gealterten Katalysatoren wurden unter Ar-Atmosphäre in eine Glovebox überführt, von der aus weitere Charakterisierungsstudien vorbereitet wurden.
After cooling to 230 ° C., the initial catalyst activity was measured under differential reaction conditions at 4 bar and 600 NL g ka 1 Ir 1 (H 2 / CO 2 / Ar = 4/1/75, GHSV = 800,000 hr 1 ). For aging, the catalyst was heated at a heating rate of 5 K min 1 and maintained at the aging temperature (350 ° C and 450 ° C) at 8 bar and 18 NL g ka 1 h 1 (H 2 / C0 2 / Ar = 4 / 1/5, GHSV = 24,000 hr 1 ). The aging time was 2 h in the initial deactivation treatment and 4 h in all further treatments. After each aging step, the catalyst bed was cooled to 230 ° C before the catalyst activity was re-determined under the above conditions to follow the catalyst deactivation in the kinetic regime under conditions free of product or equilibrium limitations. These cycles were repeated to obtain catalysts aged for 0, 6, 40 and 72 hours. The aged catalysts were transferred under Ar atmosphere to a glovebox, from which further characterization studies were prepared.
Beispiele Examples
Tabelle 2: In der Kopräzipitation eingesetzte einmolare Metallsalz-Lösungen
Table 2: Molar metal salt solutions used in co-precipitation
Tabelle 3: Zusammensetzung der kalzinierten Katalysatoren
Tabelle 4: Charakterisierungsdaten der Katalysatoren Table 3: Composition of the calcined catalysts Table 4: Characterization data of the catalysts
a normiert auf Masse des kalzinierten Katalysators b normiert auf Masse des kalzinierten Katalysators a normalized to mass of the calcined catalyst b normalized to mass of the calcined catalyst
Tabelle 5: Ergebnisse der katalytischen Testreaktion Table 5: Results of the catalytic test reaction
Tabelle 6: Charakterisierungsdaten bei verschiedenen Alterungszeiten Table 6: Characterization data at different aging times
a normiert auf Masse des kalzinierten Katalysators a normalized to the mass of the calcined catalyst
b normiert auf Masse des reduzierten Katalysators b normalized to mass of the reduced catalyst
c bestimmt mittels XRD, Ni(Fe)-Reflex bei 2Θ = 51 .3-51 .7 0
c determined by XRD, Ni (Fe) reflection at 2Θ = 51 .3-51 .7 0
Claims
1 . Katalysator zur Methanisierung von Kohlenmonoxid und/oder Kohlendioxid, umfassend Aluminiumoxid, eine Ni-Aktivmasse, sowie Fe, dadurch gekennzeichnet, dass das molare Ni/Fe-Verhältnis im Katalysator 4,0 bis 25,0, bevorzugt 5,0 bis 10,0 und besonders bevorzugt 5,0 bis 6,0 beträgt. 1 . A catalyst for the methanation of carbon monoxide and / or carbon dioxide, comprising aluminum oxide, a Ni active composition, and Fe, characterized in that the molar Ni / Fe ratio in the catalyst is 4.0 to 25.0, preferably 5.0 to 10.0 and more preferably 5.0 to 6.0.
2. Katalysator nach Anspruch 1 , dadurch gekennzeichnet, dass die Ni-Aktivmasse Kristallite mit einem Durchmesser unter 20 nm, bevorzugt unter 10 nm, aufweist. 2. A catalyst according to claim 1, characterized in that the Ni active material crystallites having a diameter of less than 20 nm, preferably less than 10 nm.
3. Katalysator nach einem der vorhergehenden Ansprüche, gekennzeichnet durch eine C02-Aufnahmekapazität bei 35°C von größer 200 μηιοΙ, vorzugsweise 200 bis 300 μηιοΙ pro Gramm Katalysator. 3. Catalyst according to one of the preceding claims, characterized by a C0 2 -aufnahmekapazität at 35 ° C of greater than 200 μηιοΙ, preferably 200 to 300 μηιοΙ per gram of catalyst.
4. Verwendung eines Katalysators nach einem der vorhergehenden Ansprüche, zur Methanisierung von Kohlenmonoxid und/oder Kohlendioxid mit gasförmigen Wasserstoff. 4. Use of a catalyst according to one of the preceding claims, for the methanation of carbon monoxide and / or carbon dioxide with gaseous hydrogen.
5. Verfahren zur Herstellung eines Katalysators nach Anspruch 1 , umfassend die Schritte: 5. A process for the preparation of a catalyst according to claim 1, comprising the steps:
a) Kopräzipitation aus einer Lösung, die AI, Ni und Fe in gelöster Form enthält, um einen Niederschlag zu erhalten, a) co-precipitation from a solution containing Al, Ni and Fe in dissolved form to obtain a precipitate,
b) Isolieren des Niederschlags aus Schritt a), b) isolating the precipitate from step a),
c) Trocknen des isolierten Niederschlags aus Schritt b) und c) drying the isolated precipitate from step b) and
d) Kalzinieren des getrockneten Niederschlags aus Schritt c). d) calcining the dried precipitate from step c).
6. Verfahren nach Anspruch 5, dadurch gekennzeichnet, dass die Lösung aus Schritt a) eine wässrige Lösung ist. 6. The method according to claim 5, characterized in that the solution from step a) is an aqueous solution.
7. Verfahren nach Anspruch 5 oder 6, dadurch gekennzeichnet, dass der Niederschlag in der Lösung für mindestens 30 Minuten gealtert wird. 7. The method according to claim 5 or 6, characterized in that the precipitate is aged in the solution for at least 30 minutes.
8. Verfahren nach Anspruch 5 bis 7, dadurch gekennzeichnet, dass der isolierte Nieder- schlag aus Schritt b) gewaschen wird. 8. The method according to claim 5 to 7, characterized in that the isolated precipitate from step b) is washed.
9. Verfahren nach Anspruch 5 bis 8, dadurch gekennzeichnet, dass die AI, Ni und Fe in gelöster Form, als ionische Verbindungen in der Lösung vorliegen und diese ionischen Verbindungen dasselbe Anion haben. 9. The method according to claim 5 to 8, characterized in that the Al, Ni and Fe are present in dissolved form, as ionic compounds in the solution and these ionic compounds have the same anion.
10. Verfahren nach Anspruch 9, dadurch gekennzeichnet, dass das Anion Nitrat, Sulfat, ein Halogenid, Chlorid, oder Acetat ist.
10. The method according to claim 9, characterized in that the anion is nitrate, sulfate, a halide, chloride, or acetate.
1 1 . Verfahren nach einem der Ansprüche 5 bis 10, dadurch gekennzeichnet, dass Fe in der Lösung aus Schritt a) in der Oxidationsstufe II oder III vorliegt. 1 1. Method according to one of claims 5 to 10, characterized in that Fe is present in the solution of step a) in the oxidation state II or III.
12. Verfahren nach Anspruch 5, dadurch gekennzeichnet, dass das Kalzinieren des getrockneten Niederschlags bei einer Temperatur von 300 bis 600 °C an Luft erfolgt. 12. The method according to claim 5, characterized in that the calcination of the dried precipitate takes place at a temperature of 300 to 600 ° C in air.
13. Verfahren zur Methanisierung von Kohlendioxid und/oder Kohlenmonoxid bei dem ein Gas enthaltend Kohlendioxid und/oder Kohlenmonoxid mit einem Katalysator nach Anspruch 1 in Kontakt gebracht wird. 13. A process for the methanation of carbon dioxide and / or carbon monoxide in which a gas containing carbon dioxide and / or carbon monoxide is brought into contact with a catalyst according to claim 1.
14. Verfahren nach Anspruch 13, bei dem das Gas mit dem Katalysator bei einer Temperatur oberhalb von 200 °C in Kontakt gebracht wird.
14. The method of claim 13, wherein the gas is contacted with the catalyst at a temperature above 200 ° C in contact.
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