WO2012018520A2 - Methods for deoxygenating biomass-derived pyrolysis oils - Google Patents
Methods for deoxygenating biomass-derived pyrolysis oils Download PDFInfo
- Publication number
- WO2012018520A2 WO2012018520A2 PCT/US2011/044498 US2011044498W WO2012018520A2 WO 2012018520 A2 WO2012018520 A2 WO 2012018520A2 US 2011044498 W US2011044498 W US 2011044498W WO 2012018520 A2 WO2012018520 A2 WO 2012018520A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- derived pyrolysis
- catalyst
- pyrolysis oil
- biomass
- support
- Prior art date
Links
- 239000003921 oil Substances 0.000 title claims abstract description 209
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 188
- 239000002028 Biomass Substances 0.000 title claims abstract description 172
- 238000000034 method Methods 0.000 title claims abstract description 51
- 230000003635 deoxygenating effect Effects 0.000 title claims abstract description 13
- 239000003054 catalyst Substances 0.000 claims abstract description 97
- 229910044991 metal oxide Inorganic materials 0.000 claims abstract description 37
- 150000004706 metal oxides Chemical class 0.000 claims abstract description 37
- 229910000510 noble metal Inorganic materials 0.000 claims abstract description 28
- 230000007935 neutral effect Effects 0.000 claims abstract description 21
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000000203 mixture Substances 0.000 claims abstract description 19
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 claims abstract description 15
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims abstract description 13
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 7
- URLJKFSTXLNXLG-UHFFFAOYSA-N niobium(5+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[O-2].[O-2].[Nb+5].[Nb+5] URLJKFSTXLNXLG-UHFFFAOYSA-N 0.000 claims abstract description 6
- 229910052814 silicon oxide Inorganic materials 0.000 claims abstract description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 33
- 229910052750 molybdenum Inorganic materials 0.000 claims description 19
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 16
- 239000011733 molybdenum Substances 0.000 claims description 16
- 229910052759 nickel Inorganic materials 0.000 claims description 15
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 11
- 229910017052 cobalt Inorganic materials 0.000 claims description 11
- 239000010941 cobalt Substances 0.000 claims description 11
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 11
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 claims description 11
- 229910052721 tungsten Inorganic materials 0.000 claims description 11
- 239000010937 tungsten Substances 0.000 claims description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 9
- 239000010931 gold Substances 0.000 claims description 6
- 239000010948 rhodium Substances 0.000 claims description 6
- 229910000484 niobium oxide Inorganic materials 0.000 claims description 5
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 claims description 5
- 229910052763 palladium Inorganic materials 0.000 claims description 4
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 claims description 3
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims description 3
- 229910052737 gold Inorganic materials 0.000 claims description 3
- 229910052703 rhodium Inorganic materials 0.000 claims description 3
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 claims description 3
- 229910052707 ruthenium Inorganic materials 0.000 claims description 3
- 239000010955 niobium Substances 0.000 claims 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 23
- 239000001301 oxygen Substances 0.000 abstract description 23
- 229910052760 oxygen Inorganic materials 0.000 abstract description 23
- 229910052751 metal Inorganic materials 0.000 description 83
- 239000002184 metal Substances 0.000 description 83
- 239000007787 solid Substances 0.000 description 57
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 55
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 52
- 230000032050 esterification Effects 0.000 description 36
- 238000005886 esterification reaction Methods 0.000 description 36
- 229920005989 resin Polymers 0.000 description 36
- 239000011347 resin Substances 0.000 description 36
- 150000002739 metals Chemical class 0.000 description 30
- 239000003456 ion exchange resin Substances 0.000 description 27
- 229920003303 ion-exchange polymer Polymers 0.000 description 27
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 24
- 229930195733 hydrocarbon Natural products 0.000 description 18
- 150000002430 hydrocarbons Chemical class 0.000 description 18
- 229920001467 poly(styrenesulfonates) Polymers 0.000 description 18
- 238000005342 ion exchange Methods 0.000 description 15
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 14
- 239000002253 acid Substances 0.000 description 13
- 239000007789 gas Substances 0.000 description 13
- 229920001429 chelating resin Polymers 0.000 description 12
- 239000000243 solution Substances 0.000 description 12
- ZGEGCLOFRBLKSE-UHFFFAOYSA-N 1-Heptene Chemical compound CCCCCC=C ZGEGCLOFRBLKSE-UHFFFAOYSA-N 0.000 description 11
- 230000003197 catalytic effect Effects 0.000 description 11
- 238000006392 deoxygenation reaction Methods 0.000 description 9
- 238000001914 filtration Methods 0.000 description 9
- 239000000463 material Substances 0.000 description 9
- 239000001257 hydrogen Substances 0.000 description 8
- 229910052739 hydrogen Inorganic materials 0.000 description 8
- 230000001603 reducing effect Effects 0.000 description 8
- 238000009835 boiling Methods 0.000 description 7
- 238000004821 distillation Methods 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- 239000011148 porous material Substances 0.000 description 7
- 239000010457 zeolite Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 150000002148 esters Chemical class 0.000 description 6
- 239000002808 molecular sieve Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 6
- 239000011973 solid acid Substances 0.000 description 6
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 5
- 229910021536 Zeolite Inorganic materials 0.000 description 5
- 239000002551 biofuel Substances 0.000 description 5
- 150000001735 carboxylic acids Chemical class 0.000 description 5
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 5
- -1 hydrogen ions Chemical class 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 4
- 230000002378 acidificating effect Effects 0.000 description 4
- 238000005194 fractionation Methods 0.000 description 4
- 150000002500 ions Chemical class 0.000 description 4
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- 150000007513 acids Chemical class 0.000 description 3
- 229910001038 basic metal oxide Inorganic materials 0.000 description 3
- 238000004587 chromatography analysis Methods 0.000 description 3
- 239000000706 filtrate Substances 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 229910021645 metal ion Inorganic materials 0.000 description 3
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 150000002894 organic compounds Chemical class 0.000 description 3
- 238000010587 phase diagram Methods 0.000 description 3
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 3
- 229920000642 polymer Polymers 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- XNWFRZJHXBZDAG-UHFFFAOYSA-N 2-METHOXYETHANOL Chemical compound COCCO XNWFRZJHXBZDAG-UHFFFAOYSA-N 0.000 description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000002154 agricultural waste Substances 0.000 description 2
- 150000001299 aldehydes Chemical class 0.000 description 2
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 2
- 150000001342 alkaline earth metals Chemical group 0.000 description 2
- 238000001479 atomic absorption spectroscopy Methods 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 150000001732 carboxylic acid derivatives Chemical class 0.000 description 2
- 150000001896 cresols Chemical class 0.000 description 2
- 230000001419 dependent effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 2
- FKRCODPIKNYEAC-UHFFFAOYSA-N ethyl propionate Chemical compound CCOC(=O)CC FKRCODPIKNYEAC-UHFFFAOYSA-N 0.000 description 2
- 239000012065 filter cake Substances 0.000 description 2
- 235000019253 formic acid Nutrition 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 239000007791 liquid phase Substances 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
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 2
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 150000002989 phenols Chemical class 0.000 description 2
- 238000011085 pressure filtration Methods 0.000 description 2
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 238000004448 titration Methods 0.000 description 2
- 239000012808 vapor phase Substances 0.000 description 2
- 229910001928 zirconium oxide Inorganic materials 0.000 description 2
- HNAGHMKIPMKKBB-UHFFFAOYSA-N 1-benzylpyrrolidine-3-carboxamide Chemical compound C1C(C(=O)N)CCN1CC1=CC=CC=C1 HNAGHMKIPMKKBB-UHFFFAOYSA-N 0.000 description 1
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 241000209504 Poaceae Species 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 1
- YZCKVEUIGOORGS-IGMARMGPSA-N Protium Chemical compound [1H] YZCKVEUIGOORGS-IGMARMGPSA-N 0.000 description 1
- 229910006069 SO3H Inorganic materials 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 238000002441 X-ray diffraction Methods 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 125000003158 alcohol group Chemical group 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000011260 aqueous acid Substances 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 229910052788 barium Inorganic materials 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical group [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 239000010953 base metal Substances 0.000 description 1
- OBNCKNCVKJNDBV-UHFFFAOYSA-N butanoic acid ethyl ester Natural products CCCC(=O)OCC OBNCKNCVKJNDBV-UHFFFAOYSA-N 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000007233 catalytic pyrolysis Methods 0.000 description 1
- 239000003729 cation exchange resin Substances 0.000 description 1
- 229940023913 cation exchange resins Drugs 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 229920001577 copolymer Polymers 0.000 description 1
- 238000010908 decantation Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- WBJINCZRORDGAQ-UHFFFAOYSA-N formic acid ethyl ester Natural products CCOC=O WBJINCZRORDGAQ-UHFFFAOYSA-N 0.000 description 1
- 125000000524 functional group Chemical group 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 229910052741 iridium Inorganic materials 0.000 description 1
- GKOZUEZYRPOHIO-UHFFFAOYSA-N iridium atom Chemical compound [Ir] GKOZUEZYRPOHIO-UHFFFAOYSA-N 0.000 description 1
- 150000002576 ketones Chemical group 0.000 description 1
- 229910052747 lanthanoid Inorganic materials 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052755 nonmetal Inorganic materials 0.000 description 1
- 150000002843 nonmetals Chemical class 0.000 description 1
- 235000020986 nuts and seeds Nutrition 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 235000019260 propionic acid Nutrition 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000010517 secondary reaction Methods 0.000 description 1
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 description 1
- 229910010271 silicon carbide Inorganic materials 0.000 description 1
- 239000008247 solid mixture Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000008961 swelling Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 238000003828 vacuum filtration Methods 0.000 description 1
- 238000007158 vacuum pyrolysis Methods 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
- 239000002916 wood waste Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Definitions
- the present invention generally relates to methods for producing biofuels, and more particularly relates to methods for deoxygenating biomass-derived pyrolysis oils.
- Fast pyrolysis is a process during which organic carbonaceous biomass feedstock, i.e., "biomass", such as wood waste, agricultural waste, etc., is rapidly heated to between 300°C to 900°C in the absence of air using a pyrolysis reactor. Under these conditions, solid and gaseous pyrolysis products are produced. A condensable portion (vapors) of the gaseous pyrolysis products is condensed into biomass-derived pyrolysis oil.
- Biomass-derived pyrolysis oil can be burned directly as fuel for certain boiler and furnace applications, and can also serve as a potential feedstock in catalytic processes for the production of fuels in petroleum refineries. Biomass-derived pyrolysis oil has the potential to replace up to 60% of transportation fuels, thereby reducing the dependency on conventional petroleum and reducing its environmental impact.
- biomass-derived pyrolysis oil is a complex, highly oxygenated organic liquid having properties that currently limit its utilization as a biofuel.
- biomass-derived pyrolysis oil has high acidity and a low energy density attributable in large part to oxygenated hydrocarbons in the oil, which undergo secondary reactions during storage.
- Oxygenated hydrocarbons as used herein are organic compounds containing hydrogen, carbon, and oxygen. Such oxygenated hydrocarbons in the biomass- derived pyrolysis oil include carboxylic acids, phenols, cresols, aldehydes, etc.
- biomass-derived pyrolysis oil comprises 30% by weight oxygen from these oxygenated hydrocarbons.
- Conversion of biomass-derived pyrolysis oil into biofuels and chemicals requires full or partial deoxygenation of the biomass-derived pyrolysis oil. Such deoxygenation may proceed via two main routes, namely the elimination of either water or C0 2 .
- deoxygenating biomass-derived pyrolysis oil leads to rapid plugging or fouling in a hydroprocessing reactor caused by the formation of solids from the biomass- derived pyrolysis oil. Particulates in the oil settle on the processing catalysts causing catalytic bed fouling thereby reducing activity of the catalyst and causing build up in the hydroprocessing reactor. It is believed that this plugging is caused by an acid catalyzed polymerization of the biomass-derived pyrolysis oil that creates either a glassy brown polymer or powdery brown char, which limit run duration and processibility of the biomass-derived pyrolysis oil.
- Methods are provided for deoxygenating treated biomass-derived pyrolysis oil.
- the method comprises exposing the treated biomass-derived pyrolysis oil to a catalyst having a neutral catalyst support.
- Methods are provided for deoxygenating treated biomass-derived pyrolysis oil in accordance with yet another exemplary embodiment of the present invention.
- the method comprises the steps of providing a catalyst comprising a metal on a carbon support, a non- alumina metal oxide support, a theta alumina support, or a combination thereof.
- the treated biomass-derived pyrolysis oil is introduced into a hydroprocessing reactor in the presence of the catalyst under hydroprocessing conditions to produce low oxygen biomass-derived pyrolysis oil.
- Methods are provided for deoxygenating treated biomass-derived pyrolysis oil in accordance with yet another exemplary embodiment of the present invention.
- the method comprises the steps of providing a catalyst comprising a metal on a carbon support, a non- alumina metal oxide support, or a support comprising a combinations thereof.
- the treated biomass-derived pyrolysis oil is exposed to the catalyst at hydroprocessing conditions sufficient to at least partially deoxygenate the treated biomass-derived pyrolysis oil.
- the non-alumina metal oxide support is selected from the group consisting of a titanium oxide support, a silicon oxide support, a zirconia oxide support, and a niobium oxide support.
- FIG. 1 is a flow diagram of a method for deoxygenating treated biomass-derived pyrolysis oils, according to exemplary embodiments of the present invention
- FIG. 2 is a schematic diagram of the method of FIG. 1 , according to exemplary embodiments of the present invention.
- FIG. 3 is a phase diagram for pure ethanol
- FIG. 4 is a table of exemplary metals of exemplary deoxygenation catalysts having a neutral catalyst support.
- FIG. 5 is a table of exemplary neutral catalyst supports for the metals of FIG. 4.
- Various exemplary embodiments of the present invention are directed to methods for deoxygenating biomass-derived pyrolysis oils by exposing treated biomass-derived pyrolysis oil to a catalyst having a neutral catalyst support, as hereinafter described.
- the treated biomass-derived pyrolysis oil is introduced into a hydroprocessing reactor in the presence of the catalyst under hydroprocessing conditions to produce low oxygen biomass-derived pyrolysis oil. Solids formation that typically occurs during deoxygenation or other hydroprocessing is decreased resulting in less plugging of the catalyst bed, increased hydroprocessing run times, and improved processibility of the biomass-derived pyrolysis oil.
- the deoxygenated oil produced according to exemplary embodiments of the present invention is generally described herein as a "low oxygen biomass-derived pyrolysis oil", this term generally includes any oil produced having a lower oxygen concentration than conventional biomass-derived pyrolysis oil.
- the term “low oxygen biomass-derived pyrolysis oil” includes oil having no oxygen, i.e., a biomass-derived pyrolysis oil in which all the oxygenated hydrocarbons have been converted into hydrocarbons (i.e., a "hydrocarbon product").
- the low oxygen biomass-derived pyrolysis oil comprises from 0 to 5 wt.% oxygen.
- Hydrocarbons as used herein are organic compounds that contain principally only hydrogen and carbon, i.e., oxygen-free.
- Oxygenated hydrocarbons as used herein are organic compounds containing hydrogen, carbon, and oxygen.
- exemplary oxygenated hydrocarbons in biomass-derived pyrolysis oil include alcohols such as phenols and cresols, carboxylic acids, aldehydes, etc.
- a method 10 for deoxygenating biomass-derived pyrolysis oils begins by providing treated biomass-derived pyrolysis oil (step 200).
- treated biomass-derived pyrolysis oil comprises esterified biomass-derived pyrolysis oil having a solids content less than 0.10%, preferably less than 0.01 %; a total metals content of less than 100 ppm, preferably less than 20 ppm; and a water content of less than 20 weight percent (wt.%), preferably less than 15 wt.% (hereinafter "target levels").
- Esterification reduces the carboxylic total acid number (TAN) to less than 40 mg KOH/g biomass-derived pyrolysis oil (also a "target level") in the treated biomass-derived pyrolysis oil.
- the treated biomass-derived pyrolysis oil has not been subjected to an esterification process but has a solids content, a total metals content, and a water content, or at least one thereof, at the target levels.
- Conventional as-produced biomass-derived pyrolysis oil typically contains 1000 to 2000 ppm total metals, 20-33 wt.% water with high acidity (TAN > 150), and a solids content of 0.1 wt.% to 5 wt.%.
- TAN > 150 high acidity
- the conventional biomass-derived oil may be used as the "treated biomass-derived pyrolysis oil”.
- Conventional biomass-derived pyrolysis oil may also be selectively treated as hereinafter described to reduce only those levels not at the target level(s).
- the starting conventional biomass-derived pyrolysis oil is available from, for example, Ensyn
- Biomass-derived pyrolysis oil is provided from a source such as a feed tank or other source operative to provide such biomass-derived pyrolysis oil.
- Biomass-derived pyrolysis oil may be produced, for example, from pyrolysis of biomass in a pyrolysis reactor. Virtually any form of biomass can be used for pyrolysis to produce biomass- derived pyrolysis oil.
- Biomass-derived pyrolysis oil may be derived from biomass material such as wood, agricultural waste, nuts and seeds, algae, grasses, forestry residues, or the like.
- biomass-derived pyrolysis oil may be obtained by different modes of pyrolysis, such as fast pyrolysis, vacuum pyrolysis, catalytic pyrolysis, and slow pyrolysis (also known as carbonization) or the like.
- Biomass-derived pyrolysis oil composition is somewhat dependent on feedstock and processing variables.
- the biomass-derived pyrolysis oil 15 may be, for example, filtered in a filtration apparatus 20 to substantially remove particulate solids therefrom to form low solids biomass-derived pyrolysis oil 25, as hereinafter defined.
- the biomass-derived pyrolysis oil may be contacted in the filtration apparatus with one or more filters (and filter media) for a selected period of time to produce a filtrate comprised of filtered biomass-derived pyrolysis oil and a filter cake.
- the filters may be used sequentially for treating the same volume of oil.
- the biomass-derived pyrolysis oil may be filtered using one or more of vacuum, gravity, or pressure filtration.
- the filtrate is removed from the filter cake and the filtrate is recovered.
- pressurized gas such as nitrogen, air, or the like may be supplied on the input side of the filter to accelerate filtration. Pressures from 1 atmosphere (atm) absolute pressure to 8 atm absolute pressure may be used. The period of time required for filtration is dependent on volume and viscosity of the oil being filtered, the amount and particle size of solids to be removed, the filter media (composition and pore size), and filtration pressure and temperature.
- negative pressure i.e., a vacuum
- 0.10 atm absolute pressure to 0.95 atm absolute pressure may be supplied on the output side of the filter. No pressure is used for gravity filtration.
- Low solids biomass-derived pyrolysis oil as used herein means a biomass-derived pyrolysis oil having the target solids level of less than 0.10%, preferably less than 0.01 %, solids.
- biomass-derived pyrolysis oil may be a low solids biomass-derived pyrolysis oil if the solids content therein is already at the target solids level.
- low solids includes zero solids. Solids content in biomass-derived pyrolysis oil may be measured as described in the Annex to ASTM D7544-09 "Standard Specification for Pyrolysis Liquid Biofuel", or by other known methods.
- the low solids biomass-derived pyrolysis oil 25 undergoes a metal reduction process, for example ion-exchange on an ion-exchange resin 30, to reduce the total metal concentration therein to the target level.
- the low solids biomass-derived pyrolysis oil is contacted with the ion-exchange resin.
- the low solids biomass-derived pyrolysis oil that contacts the ion-exchange resin undergoes ion exchange such that metal ions are captured by the ion-exchange resin. More specifically, the ion- exchange resin contains sulfonic acid at its active sites.
- the metals preferentially migrate out of the oil to the active sites on the ion-exchange resin.
- the metals in the biomass-derived pyrolysis oil are replaced by hydrogen ions.
- the ion-exchange can be accomplished by either a batch method or a continuous column method.
- the ion-exchange resin and biomass-derived pyrolysis oil are contacted by mixing the resin and oil in a resin vessel, batch tank, or the like.
- a given weight of ion-exchange resin is added to a known volume of low solids biomass-derived pyrolysis oil, as hereinafter described.
- the amount of ion-exchange resin added to the fixed amount of oil is typically an excess of resin (based on theoretical resin capacity, as defined below).
- the optimum resin to oil ratio is determined experimentally and is impacted by temperature and exposure time.
- the resin/oil mixture is agitated for 0.5 hours to 24 hours, preferably 0.5 to 4 hrs (hereinafter "the exposure time") at a temperature of 10°C to 120°C, preferably from 20°C to 60°C.
- Samples of the ion- exchanged oil may be collected and analyzed for metal content, as hereinafter described.
- the ion-exchange resin and the low solids biomass-derived pyrolysis oil are contacted by passing the biomass-derived pyrolysis oil through a column (of one or more "beds") containing the ion-exchange resin.
- the resin temperature may be from 10°C to 120°C, preferably from 20°C to 60°C.
- the biomass- derived pyrolysis oil is passed through the column by positive pressure flow or by gravity flow.
- the absolute pressure is from greater than 0 KPa to 13790 KPa (0 to 2000 psi), preferably from greater than 0 KPa to 689.5 KPa (greater than 0 psi to 100 psi), and most preferably from 13.8 KPa to 206.8 KPa (2 psi to 30 psi).
- the biomass-derived pyrolysis oil passes downward through the column and is allowed to slowly elute gravimetrically.
- the low solids biomass-derived pyrolysis oil is passed over the ion-exchange resin at a Liquid Hourly Space Velocity (LHSV) of 0.1 -20 hr " ', preferably 1 - 10 hr " ' .
- LHSV Liquid Hourly Space Velocity
- the concentration of the selected metal ions in the treated oil is reduced significantly.
- metal concentrations in biomass-derived pyrolysis oil may be measured by Atomic Absorption Spectroscopy (AAS), Inductively-Coupled Plasma- Atomic Absorption Spectroscopy (ICP-AAS), or other known methods.
- AAS Atomic Absorption Spectroscopy
- ICP-AAS Inductively-Coupled Plasma- Atomic Absorption Spectroscopy
- MWj is the molecular weight of metal in g/mol
- Vj is the valency (charge) of metal i in solution
- D r is the ion-exchange resin density in g/mL.
- TC r is the theoretical capacity of resin r.
- Theoretical capacity (TC,) is often expressed in terms of milliequivalents ions/gram resin.
- V oil V r /(VC r *Dfced))
- Von is the volume of low solids biomass-derived pyrolysis oil in liters
- Dfeed is the feed oil (the starting biomass-derived pyrolysis oil) density (in kilograms/liter);
- V r is the resin volume in milliliters
- V VC r is the volume capacity of acidic ion-exchange resin to a given mass of metal- containing biomass-derived pyrolysis oil as determined above and expressed in mL resin/kg of biomass-derived pyrolysis oil.
- the V 0 ji/V r processed is also known as the number of bed volumes (BV) of oil processed.
- BV bed volumes
- volume capacity (VC r ) of the acidic ion-exchange resin preferably 1 to 5 VCr.
- Resin efficiency also referred to as ion-exchange efficiency (IX e ff )
- IX e ff ion-exchange efficiency
- IXeff ( ⁇ C(Cif-Cip)*V i /MW i * 1000*Mf)))/ (TC r *M r ),
- Q f and Q p are the concentration of metal i expressed in terms of grams of metal i per gram of oil in the feed (biomass-derived pyrolysis oil) and product (low metal biomass derived pyrolysis oil), respectively
- M f is the mass of feed oil in grams
- MWj is the molecular weight of metal i in g/mol
- V is the valency (charge) of metal i in solution
- TC is the theoretical capacity of resin r
- M is the mass in grams of resin r utilized. If it is assumed that a single metal ion neutralizes one resin exchange site regardless of ion charge, then the valance of the individual ions (Vj) is assigned as 1 for all metals. A higher exchange efficiency is typically desired.
- Theoretical resin capacity multiplied by the ion exchange efficiency provides the actual capacity, which is the amount of ion-exchange resin needed to actually deionize a given amount of biomass-derived pyrolysis oil.
- Suitable ion-exchange resins useful in this process are strongly acidic cation- exchange resins.
- the resin is used in the protonated form, i.e., all of the active groups are -SO 3 H.
- Neutralized sulfonic acid resins, in which some or all of the protons have been exchanged by a cation such as lithium, sodium, potassium, magnesium, and calcium are also suitable.
- resins are supplied with an alternate counterion (i.e., sodium, Na+)
- the acid form may be generated prior to use by treatment with aqueous acid (such as hydrochloric, nitric, or sulfuric acid, etc.) This is commonly known in the art as ion-exchange resin activation.
- the resin comprises sulfonated copolymers of styrene.
- Preferred sulfonic acid resins are macroreticular resins. As used herein,
- “macroreticular resins” are made of two continuous phases-a continuous pore phase and a continuous gel polymeric phase.
- the continuous gel polymeric phase is structurally composed of small spherical microgel particles agglomerated together to form clusters, which, in turn, form interconnecting pores.
- the surface area arises from the exposed surface of the microgel clusters.
- Macroreticular ion exchange resins can be made with different surface areas ranging from 7 to 1500 m 2 /g, and average pore diameters ranging from 5 to 10000 nm.
- Gel-type resins may also be used.
- gel-type resins are generally translucent. There are no permanent pore structures for the gel-type resins. The pores are generally considered to be molecular-scale micropores. The pore structures are determined by the distance between the polymer chains and crosslinks which vary with the crosslink level of the polymer, the polarity of the solvent, and the operating conditions.
- Macroreticular resins are preferable for continuous column ion-exchange applications where resin swelling/shrinking should be minimized, while gel-type resins are preferred for batch ion-exchange applications, but either type may be used in either application.
- exemplary suitable acidic ion-exchange resins include those manufactured by Dow Chemical Co., Midland, MI (USA) under the tradenames/trademarks DOWEX®
- DOWEX® MSC- 1 DOWEX® HGR NG (H), DOWE® DR-G8, DOWEX® 88,
- DOWEX® MONOSPHERE 88 DOWEX® MONOSPHERE C-600 B, DOWEX® MONOSPHERE M-31 , DOWEX® MONOSPHERE DR-2030, DOWEX® M-31 , DOWEX® G-26 (H), DOWEX® 50W-X4, DOWEX® 50W-X8, DOWEX® 66, those manufactured by Rohm and Haas, Philadelphia, PA (USA) under the
- a low solids, low metal biomass-derived pyrolysis oil 35 is then removed from the used ion-exchange resin (hereinafter "spent ion-exchange resin")-
- the low solids, low metal biomass-derived pyrolysis oil may be removed by filtration, decantation, or other known method.
- the low solids, low metal biomass-derived pyrolysis oil is removed from the spent ion- exchange resin when the low solids, low metal biomass-derived pyrolysis oil elutes from the column gravimetrically or under positive pressure.
- low metal biomass derived pyrolysis oil has the target level of total metals of less than 100 ppm, preferably less than 20 ppm.
- Conventional biomass-derived pyrolysis oil may be low metal biomass-derived pyrolysis oil if the total metals content therein is already at the target total metals level.
- low metals includes zero metals. While particular ion-exchange methods have been described, other methods of reducing the total metal content to the target level may be used in accordance with exemplary embodiments of the present invention.
- the low solids, low metal biomass-derived pyrolysis oil 35 may be subjected to an azeotropic, vacuum, gas-assisted, or atmospheric distillation process in a first fractionator 40 such as a distillation apparatus to reduce the water content therein.
- Azeotropic, vacuum, and gas-assisted distillation processes permit the removal of water 45 from biomass-derived pyrolysis oil without having to heat the oil to at least 100°C (the boiling point of water at one atmosphere) to remove the water, i.e., such processes allow atmospheric distillation at lower temperatures.
- the use of lower temperatures to remove the water from the oil substantially prevents solidification (phase separation) of the oil that is experienced at elevated temperatures (typically 150°C).
- Vacuum distillation is performed at lower than atmospheric pressure to lower the boiling point of the water in the biomass-derived pyrolysis oil so that water therein may be removed by heating the biomass-derived pyrolysis oil at least to the lower boiling point of water at that reduced pressure.
- the boiling point of water at that pressure may be determined by consulting temperature/pressure charts that are available from, for example, the National Bureau of Standards (NBS)/National Research Council (NRC). Vacuum may be applied by a vacuum pump, aspirator, or the like.
- the biomass-derived pyrolysis oil is heated to 65°C at a vacuum of 0.05 to 0.95 atm (absolute pressure) until the desired amount of water is removed to reach the target level.
- Gas-assisted distillation uses a standard distillation column with an inert gas such as nitrogen, air, argon, helium, hydrogen or other gas passing into and over the low metal, water-containing biomass-derived pyrolysis oil while heating the low metal biomass- derived pyrolysis oil to a selected temperature of 30°C to 90°C, preferably 70°C at a flow rate of 0.1 to 100 liters (L) gas/L oil/minute, preferably 0.5 to 4 L gas/L oil/min.
- Gas- assisted distillation functionally reduces the vapor pressure of the oil, thus resulting in more water in vapor phase so that it can be removed from the low metal biomass-derived pyrolysis oil at less than 100°C.
- the rate at which the water is removed is limited by the vapor pressure of water at the selected temperature, the gas flow rate, and the liquid volume to be distilled.
- the gas flow rate (controlled by a mass flow controller or valve) and selected temperature may be varied depending on the desired rate of water removal.
- the wt.% water in the starting and treated biomass-derived pyrolysis oil may be measured, for example, by the Karl Fischer Reagent Titration Method (ASTM D 1364) as known to one skilled in the art.
- the treated biomass-derived pyrolysis oil contains less than 20 weight percent water (the "target level").
- biomass-derived pyrolysis oil While particular methods for reducing the water content in biomass-derived pyrolysis oil have been described, other methods of reducing water in biomass-derived pyrolysis oil known to those skilled in the art may be used. It is also noted that while ion- exchange prior to water removal has been described, metal removal (including ion- exchange) following water removal may also be performed. As a result of fractionation, a "low solids, low metal, low water biomass-derived pyrolysis oil" 50 having the target level of water of less than 20 weight percent (wt.%), preferably less than 15 wt.% is produced. As noted previously, conventional biomass-derived pyrolysis oil may be low water biomass-derived pyrolysis oil if the water content therein is already at the target water level. As used herein, "low water” includes zero water.
- the low solids, low metal, low water biomass-derived pyrolysis oil is esterified. Esterification is, however, optional as noted previously. Esterification increases catalyst longevity by reacting components that are believed to participate in reactions that cause fouling of the catalyst.
- the low solids, low metal, low water biomass-derived pyrolysis oil is esterified in the presence of supercritical alcohol 60 to form esterified biomass-derived pyrolysis oil 70.
- the low solids, low metal, low water biomass-derived pyrolysis oil 50 is diluted with the alcohol 60 to form a solution 53.
- the alcohol 60 employed for esterification includes, but is not limited to aliphatic alcohols, such as methanol, ethanol, propanol, and butanol.
- Diluting can be achieved by placing a predetermined volume of the treated acid- containing biomass-derived pyrolysis oil in a container, such as a tank, vessel or the like, and adding the ethanol to the container to form the solution.
- a container such as a tank, vessel or the like
- an amount of ethanol is added to the low solids, low metal, low water biomass-derived pyrolysis oil such that the solution 53 includes at least 15% alcohol by weight. In other embodiments, more or less alcohol is added to the solution.
- the solution 53 is esterified at a temperature and a pressure that are at supercritical or just below critical limitations of the alcohol.
- esterification can be performed at a temperature in a range from of 180°C to 290°C at a pressure of at least 4.4 MPa to 8.00 MPa (640 psig to 1 160 psig).
- the particular temperatures and/or pressures employed are selected based on the alcohol included in the solution 53.
- the solution is esterified for a residence time in a range of 0.5 hour to 3 hours.
- esterification occurs for a longer or shorter time period.
- Esterification preferably occurs in the absence of gas.
- an inert gas such as nitrogen, can be employed to evacuate the atmosphere in which esterification occurs, and a vacuum seal may be formed after the atmosphere is substantially completely evacuated.
- FIG. 3 is a phase diagram for pure ethanol.
- the phase diagram includes an x-axis 302 representing temperature as measured in °C and a y-axis 304 representing pressure as measured in megaPascals (MPa).
- Line 306 includes a triple point 308 from which another line 310 extends to thereby indicate a phase change threshold between the solid, liquid, and vapor phases of ethanol.
- Line 306 further includes a critical point 312 at which the liquid and gaseous phase of ethanol become substantially identical.
- the critical point 312 for ethanol is at 243°C and 6.38 MPa (925 psi). As shown in FIG. 3, points along line 306 beyond the critical point 312 correspond to supercritical conditions.
- Other aliphatic alcohols employed during esterification have critical points that are different from that of ethanol.
- the critical point of methanol is at 240°C and 7.95 MPa (1 153 psi).
- the critical point of propanol is at 268.6°C and 5.16 MPa (749 psi), and the critical point of butanol is at 289.8°C and 4.42 MPa (641 psi).
- the reactor may be an upflow tubular reactor with or without a fixed catalyst bed.
- the preferred reactor comprises the upflow tubular reactor, downflow reactors can be employed in some embodiments.
- Suitable types of reactors include, but are not limited to fluidized bed systems, batch reactors, continuously stirred reactors, and the like. No matter the particular type of reactor employed, the esterification catalyst composition can be simply placed within the reactor or on the catalyst bed for reaction with the solution.
- esterification is performed in the absence of an esterification catalyst composition.
- esterification is performed in the presence of an esterification catalyst composition.
- an "esterification catalyst composition” is defined as solid composition comprising at least an active phase.
- the esterification catalyst composition is selected to reduce the total acid number of the acid-containing biomass-derived pyrolysis oil and may be referred to herein as an "esterification catalyst.”
- suitable esterification catalyst compositions comprise solid acid catalysts, solid base catalysts or catalytic metals dispersed on a solid support such as those typically employed for hydroprocessing.
- Exemplary solid acid esterification catalysts include, but are not limited to, molecular sieves, metal oxides, and sulfated metal oxides.
- Suitable molecular sieves include, but are not limited to zeolites and MCM 41.
- the zeolite can be selected from BEA -type zeolites, zeolite X, zeolite Y, zeolite ZSM 5, and zeolite ZSM 12.
- Metal oxides useful as solid acid esterification catalysts include those selected from Group IV metal oxides and Group V metal oxides.
- Group IV metal oxides include, but are not limited to titanium oxide (Ti0 2 ) and zirconium oxide ( ⁇ 2 ).
- Group V metal oxides include niobium oxide (Nb 2 0 5 ). In other embodiments, other Group IV and V metal oxides and mixtures thereof can alternatively be employed.
- Sulfated metal oxides used as solid acid esterification catalysts include sulfated zirconia. The aforementioned solid acid esterification catalysts are intended for use as standalone catalysts. Hence, the solid acid esterification catalyst is not employed with a support material.
- the solid base esterification catalysts include, but are not limited to basic metal oxides and alkaline-earth metal exchanged molecular sieves.
- Suitable basic metal oxides employed as solid base catalysts include, but are not limited to calcium oxide (CaO), magnesium oxide (MgO), and other basic metal oxides.
- Exemplary alkaline-earth metal exchanged molecular sieves suitable for inclusion as esterification catalyst compositions include, but are not limited to, barium exchanged molecular sieves, calcium exchanged molecular sieves, and the like.
- the aforementioned solid base esterification catalysts are intended for use as standalone catalysts. Hence, the solid base catalyst is not employed with a support material.
- the esterification catalyst composition may comprise one or more metal dispersed on a metal oxide support.
- the metal may be dispersed on the support as the oxide, sulfide or as the metal (zero valent state).
- supported catalyst compositions which may be used are those employed for hydroprocessing.
- the catalytic metals can comprise one or more noble metals or non-noble metals.
- the noble metal may be present in an amount from 0.1 wt.% to 1.5 wt.% of the catalyst composition.
- wt.% means the weight of the catalytic metal (as the metal) divided by the total weight of the catalytic composition (catalytic metal weight plus weight of the support).
- Suitable noble metals include, but are not limited to gold (Au), platinum (Pt), rhodium (Rh), ruthenium (Ru), palladium (Pd), and iridium (Ir).
- the non-noble metal can be selected from nickel (Ni), cobalt (Co), molybdenum (Mo), tungsten (W), and combinations thereof.
- Ni nickel
- Co cobalt
- Mo molybdenum
- W tungsten
- metals such as Ni/Mo, Co/Mo, Ni/Co/Mo, Ni/W, and combinations thereof, may be employed.
- the catalytic metals are Ni/Mo, the metals may be present in an amount from 0.5 wt.% to 3.5 wt.% of nickel, and 5 wt % to 20 wt.% of molybdenum.
- the metals may be present from 0.5 wt.% to 3.5 wt.% of cobalt and 5 wt.% to 20 wt.% of molybdenum. If Ni/Co/Mo are the catalytic metals, the metals may be present from 0.1 wt.% to 1.5 wt.% of nickel, 0.5 wt.% to 3.5wt.% of cobalt, and 5 wt.% to 20 wt.% of molybdenum. For the case of Ni/W, the metal concentration comprises 0.5 wt.% to 3.5 wt.% of nickel, and 5 wt.% to 20 wt.% of tungsten.
- the support materials include metal oxide support materials, including, but not limited to a Group rV metal oxide, a Group V metal oxide, and a Group IIIA metal oxide.
- the metal oxide support material can be selected from a group consisting essentially of titanium oxide (Ti0 2 ), zirconium oxide (Zr0 2 ), niobium oxide (Nb 2 0 5 ), quartz, silicon carbide, aluminum oxide (A1 2 0 3 ), and silicon oxide (Si0 2 ).
- the catalyst material comprises a sulfated metal oxide.
- the sulfated metal oxide comprises sulfated zirconia.
- the sulfated metal oxide can support a metal, in an embodiment.
- the metal is a noble metal. In such case, the noble metal comprises palladium.
- esterified biomass-derived pyrolysis oil i.e., a low acid biomass-derived pyrolysis oil.
- light carboxylic acids e.g., acids having C1-C4
- volatile esters have a boiling point below or equal to the normal boiling point of the ethanol.
- 80% to 95% of the light carboxylic acids are converted, thereby reducing the TAN of the biomass- derived pyrolysis oil by 5% by weight.
- Exemplary equations of the reactions that may occur within the biomass-derived pyrolysis oil are provided below. Formic Acid + Ethanol ⁇ Water + Ethyl Formate
- the esterified biomass- derived pyrolysis oil 70 may undergo fractionation in a second fractionator 65 to remove ethanol.
- the removed ethanol can be recycled and returned to the reactor for use as the supercritical alcohol 60 in later esterification steps.
- the remaining low acid biomass- derived pyrolysis oil, now comprising volatile esters forms the treated biomass-derived pyrolysis oil 90.
- Fractionation can be achieved in the second fractionator 65 by providing a temperature gradient along a fractionation column, where a minimum temperature of the temperature gradient is set just above the boiling point of ethanol.
- a fraction of the low acid biomass-derived pyrolysis oil (e.g., the ethanol) is collected at a location along the temperature gradient, distilled and directed to a separate container. While TAN reduction using esterification with an esterification catalyst and supercritical ethanol has been described, the total acid number (inclusive of the carboxylic acid number) may be further reduced by other methods known in the art, including but not limited to other esterification methods.
- treated biomass-derived pyrolysis oil preferably comprises the esterified low solids, low metal, low water biomass-derived pyrolysis oil
- treated biomass-derived pyrolysis oil also includes non-esterified and esterified biomass-derived pyrolysis oil that is one or more of low solids, low metal, and low water, i.e., the solids content, the metal content, and the water content may not all be at the target levels.
- conventional biomass-derived pyrolysis oil may already have a solids content, a total metals content, and a water content at the desired target levels, in which case the conventional biomass-derived pyrolysis oil may be considered the low solids, low metals, low water biomass-derived pyrolysis oil.
- the conventional biomass-derived pyrolysis oil may also be selectively treated to reduce only those levels not at the target level(s). It is also to be understood that while a particular sequence of steps has been described, such steps may be performed in a different sequence.
- method 10 continues with exposing the treated biomass-derived pyrolysis oil 90 to a catalyst having a neutral catalyst support in a hydroprocessing reactor 105 (step 300).
- a neutral catalyst support is defined as one that shows less than 15% total conversion of 1-heptene in a catalytic test reactor as follows: 0.25 g of solid support material (ground and sieved to 40/60 mesh) is loaded in a tubular reactor and heated under flowing hydrogen (1 atmosphere, upflow) to 550°C for 60 minutes.
- the reactor is cooled to 425°C, hydrogen flow rate is set at 1 slm (standard liter per minute) and then 1 -heptene is introduced to the catalyst bed (by injection into or saturation of the hydrogen stream) at a rate of 0.085 g/min.
- Conversion of 1-heptene is defined by 100*(l -X(heptene)) where X is the mol fraction 1-heptene in the hydrocarbon product as determined by gas chromatographic analysis of the reactor effluent stream.
- gas chromatographic analysis as known in the art are suitable, and other analytical methods known in the art may be substituted for gas chromatographic analysis as long as a mole fraction of n-heptene in the product may be calculated.
- Exemplary neutral catalyst materials comprise carbon, a non-alumina metal oxide, a theta alumina, or mixtures thereof.
- the non-alumina metal oxide support comprises a titanium oxide (Ti0 2 ) support, a silicon oxide support, a zirconia oxide (Zr0 2 ) support, a niobium oxide (Nb 2 0 5 ) support, or a support comprising mixtures of the non- alumina metal oxides.
- the non-alumina metal oxide support may be mixed with one or more additional components to improve the physical stability and/or phase stability of the metal oxide. Components that improve physical stability include, but are not limited to, carbon, other metal oxides, and clays as known in the art.
- phase stability includes, but are not limited to, base metals, transition metals, non-metals, lanthanide metals, and combinations thereof.
- Theta alumina refers to alumina having a crystallinity as measured by X-ray diffraction corresponding to that characterized in the Joint Committee on Powder Diffraction Standards number 23-1009.
- Catalysts having a neutral catalyst support comprise a metal.
- the metal can be a noble metal, or a Group VIII non-noble metal and a Group VIB non-noble metal.
- the noble metal comprises rhodium (Rh), palladium (Pd), gold (Au), and ruthenium (Ru), or combinations thereof.
- the noble metal comprises 0.1 to 5 weight percent of the catalyst having the neutral catalyst support.
- the effective amount of the catalyst is expressed as a catalyst to oil ratio of 0.1 to 10 weight of catalyst per hourly weight feed rate of treated biomass-derived pyrolysis oil.
- the Group VIII non-noble metal comprises cobalt, nickel, or both.
- the Group VIB non-noble metal comprises molybdenum or tungsten.
- the Group VIB and Group VIII non-noble metals are optionally sulfided.
- the molar ratio of Group VIB non-noble metals to Group VIII non-noble metals ranges from 10: 1 to 1 : 10.
- the weight percent of nickel and cobalt comprises from 0.1 to 5 weight percent of the total weight of the catalyst, the cobalt calculated as an oxide and the weight percent of the molybdenum and of the tungsten in the catalyst comprises from 5 to 20 weight percent of the total weight of the catalyst, the molybdenum calculated as an oxide.
- the term "calculated as an oxide” means that the metal is calculated as a metal oxide. When metals are initially incorporated onto the neutral catalyst support, they may be present as the metal oxide, rather than in the metallic state. Therefore, as used herein, if the metal is "calculated as an oxide", that means the catalyst has x% metal oxide. The actual amount of the metal will be somewhat lower depending on the stoichiometry of the specific oxide. The oxide is removed during deoxygenation. Exemplary metals for the catalysts are listed in the FIG. 3 table, with the corresponding neutral catalyst supports listed in FIG. 4. The weight % metals identified in the cells of the table of FIG. 3 are arranged from low to high, with the preferred wt.% shown between the low and high values.
- the treated biomass-derived pyrolysis oil is exposed to the catalyst having a neutral catalyst support under hydroprocessing conditions to produce the low oxygen biomass-derived pyrolysis oil by converting at least a portion of the oxygenated hydrocarbons in the treated biomass-derived pyrolysis oil into hydrocarbons.
- Such deoxygenation requires a source of hydrogen gas 1 10 which removes the oxygen as water 1 15, thereby producing low oxygen biomass-derived pyrolysis oil 120.
- substantially all of the oxygenated hydrocarbons are converted into hydrocarbons.
- the minimum amount of hydrogen gas needed to convert substantially all of the oxygenated hydrocarbons in the treated biomass-derived pyrolysis oil comprises 1-2 equivalents of hydrogen gas per one equivalent of non-water oxygen.
- the non-water oxygen in the treated biomass-derived pyrolysis oil is derived from the functional groups of the oxygenated hydrocarbons in the treated biomass-derived pyrolysis oil. For example, one equivalent of an alcohol functional group and a ketone functional group requires 1 equivalent of hydrogen gas for deoxygenation whereas one equivalent of an ester functional group requires 2 equivalents of hydrogen gas, and 1 equivalent of a carboxylic acid functional group requires 1.5 equivalents of hydrogen gas.
- the minimum amount of hydrogen gas to substantially deoxygenate the treated biomass-derived pyrolysis oil is equal to 1 to 3 molar equivalents of the non-water oxygen in the treated biomass-derived pyrolysis oil.
- the amount of non- water oxygen A- B wherein A is the total amount of oxygen in the treated biomass-derived pyrolysis oil as determined by combustion method, as known in the ait and B is the total amount of oxygen in the water in the treated biomass-derived pyrolysis oil.
- the total water content in the treated biomass-derived pyrolysis oil is first determined by the Karl Fischer Reagent Titration Method (ASTM D1364) as known to one skilled in the art. An excess of hydrogen gas may also be used. Suitable hydroprocessing conditions include a temperature of 100°C to 400°C, a pressure of 2758 kPa to 12410 kPa (400- 1800 psig), and a residence time in the hydroprocessing reactor of 0.2 hours to 20 hours. These hydroprocessing conditions are representative only, and may be varied as well known to one skilled in the art.
- the low oxygen biomass-derived pyrolysis oil 120 produced in accordance with exemplary embodiments of the present invention has significantly less oxygen and water, making it more suitable for use and processing as a biofuel.
- the plugging that occurs with conventional deoxygenation is substantially prevented, providing for longer run times and improved processibility of the biomass-derived pyrolysis oil.
Abstract
Description
Claims
Priority Applications (6)
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EP11814996.2A EP2598609A2 (en) | 2010-07-26 | 2011-07-19 | Methods for deoxygenating biomass-derived pyrolysis oils |
BR112012031522A BR112012031522A2 (en) | 2010-07-26 | 2011-07-19 | method for the deoxygenation of treated biomass-derived pyrolysis oil |
NZ603931A NZ603931A (en) | 2010-07-26 | 2011-07-19 | Methods for deoxygenating biomass-derived pyrolysis oils |
AU2011286351A AU2011286351B2 (en) | 2010-07-26 | 2011-07-19 | Methods for deoxygenating biomass-derived pyrolysis oils |
MX2012013781A MX2012013781A (en) | 2010-07-26 | 2011-07-19 | Methods for deoxygenating biomass-derived pyrolysis oils. |
CA2801250A CA2801250A1 (en) | 2010-07-26 | 2011-07-19 | Methods for deoxygenating biomass-derived pyrolysis oils |
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US12/843,625 US20120017495A1 (en) | 2010-07-26 | 2010-07-26 | Methods for deoxygenating biomass-derived pyrolysis oils |
US12/843,625 | 2010-07-26 |
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EP (1) | EP2598609A2 (en) |
AR (1) | AR083243A1 (en) |
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BR (1) | BR112012031522A2 (en) |
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Cited By (4)
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WO2012166402A2 (en) | 2011-06-01 | 2012-12-06 | Uop Llc | Methods and catalysts for deoxygenating biomass-derived pyrolysis oil |
US9163181B2 (en) | 2012-06-20 | 2015-10-20 | Uop Llc | Methods and apparatuses for deoxygenating biomass-derived pyrolysis oil |
US9670413B2 (en) | 2012-06-28 | 2017-06-06 | Ensyn Renewables, Inc. | Methods and apparatuses for thermally converting biomass |
US10400176B2 (en) | 2016-12-29 | 2019-09-03 | Ensyn Renewables, Inc. | Demetallization of liquid biomass |
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US8841495B2 (en) | 2011-04-18 | 2014-09-23 | Gas Technology Institute | Bubbling bed catalytic hydropyrolysis process utilizing larger catalyst particles and smaller biomass particles featuring an anti-slugging reactor |
US20130008772A1 (en) * | 2011-07-08 | 2013-01-10 | Fritz Peter M | Gasification process |
US9080109B2 (en) * | 2011-12-14 | 2015-07-14 | Uop Llc | Methods for deoxygenating biomass-derived pyrolysis oil |
US9068126B2 (en) * | 2011-12-14 | 2015-06-30 | Uop Llc | Methods for deoxygenating biomass-derived pyrolysis oil |
US9192931B2 (en) * | 2012-03-30 | 2015-11-24 | Uop Llc | Processes for washing a spent ion exchange bed and for treating biomass-derived pyrolysis oil, and apparatuses for treating biomass-derived pyrolysis oil |
CN103028408A (en) * | 2012-12-17 | 2013-04-10 | 常州大学 | Hydrodeoxygenation catalyst for organic oxygen-containing compound of oil product as well as preparation method and application thereof |
US20140221688A1 (en) * | 2013-02-07 | 2014-08-07 | Kior, Inc. | Organics recovery from the aqueous phase of biomass catalytic pyrolysis |
US20160257889A1 (en) * | 2015-03-05 | 2016-09-08 | Battelle Memorial Institute | Pre-processing Bio-oil Before Hydrotreatment |
EP4263031A1 (en) | 2020-12-17 | 2023-10-25 | Shell Internationale Research Maatschappij B.V. | Process for pre-treating renewable feedstocks |
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- 2011-07-19 MY MYPI2012005161A patent/MY159902A/en unknown
- 2011-07-19 MX MX2012013781A patent/MX2012013781A/en not_active Application Discontinuation
- 2011-07-19 EP EP11814996.2A patent/EP2598609A2/en not_active Withdrawn
- 2011-07-19 AU AU2011286351A patent/AU2011286351B2/en not_active Ceased
- 2011-07-19 BR BR112012031522A patent/BR112012031522A2/en not_active IP Right Cessation
- 2011-07-19 CA CA2801250A patent/CA2801250A1/en not_active Abandoned
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US20120017495A1 (en) | 2012-01-26 |
WO2012018520A3 (en) | 2012-05-10 |
AU2011286351B2 (en) | 2014-01-09 |
EP2598609A2 (en) | 2013-06-05 |
AU2011286351A1 (en) | 2012-12-20 |
AR083243A1 (en) | 2013-02-13 |
CA2801250A1 (en) | 2012-02-09 |
MX2012013781A (en) | 2012-12-17 |
MY159902A (en) | 2017-02-15 |
NZ603931A (en) | 2014-10-31 |
BR112012031522A2 (en) | 2016-12-06 |
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