WO2023200321A1 - Procédé de traitement d'huile de pyrolyse de déchets plastiques - Google Patents
Procédé de traitement d'huile de pyrolyse de déchets plastiques Download PDFInfo
- Publication number
- WO2023200321A1 WO2023200321A1 PCT/KR2023/095003 KR2023095003W WO2023200321A1 WO 2023200321 A1 WO2023200321 A1 WO 2023200321A1 KR 2023095003 W KR2023095003 W KR 2023095003W WO 2023200321 A1 WO2023200321 A1 WO 2023200321A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- oil
- temperature
- hydrotreating
- pyrolysis oil
- waste plastic
- Prior art date
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 83
- 239000002699 waste material Substances 0.000 title claims abstract description 79
- 239000004033 plastic Substances 0.000 title claims abstract description 76
- 229920003023 plastic Polymers 0.000 title claims abstract description 76
- 238000000034 method Methods 0.000 title claims abstract description 56
- 239000003054 catalyst Substances 0.000 claims abstract description 52
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 42
- 239000011593 sulfur Substances 0.000 claims abstract description 42
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 42
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000007789 gas Substances 0.000 claims abstract description 37
- 239000007788 liquid Substances 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 229910001868 water Inorganic materials 0.000 claims abstract description 22
- 238000005406 washing Methods 0.000 claims abstract description 12
- 238000002156 mixing Methods 0.000 claims abstract description 6
- 238000004064 recycling Methods 0.000 claims abstract description 6
- 239000012535 impurity Substances 0.000 claims description 39
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 38
- 239000000460 chlorine Substances 0.000 claims description 29
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 25
- 229910052801 chlorine Inorganic materials 0.000 claims description 25
- 229910052757 nitrogen Inorganic materials 0.000 claims description 19
- 230000015572 biosynthetic process Effects 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 150000003839 salts Chemical class 0.000 claims description 12
- 150000001336 alkenes Chemical class 0.000 claims description 10
- 238000004821 distillation Methods 0.000 claims description 9
- 239000012530 fluid Substances 0.000 claims description 6
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 2
- 239000003921 oil Substances 0.000 description 128
- 229910052751 metal Inorganic materials 0.000 description 16
- 239000002184 metal Substances 0.000 description 16
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 15
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 12
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 12
- 229910052750 molybdenum Inorganic materials 0.000 description 12
- 239000011733 molybdenum Substances 0.000 description 12
- 230000000694 effects Effects 0.000 description 11
- 229930195733 hydrocarbon Natural products 0.000 description 8
- 150000002430 hydrocarbons Chemical class 0.000 description 8
- 239000004215 Carbon black (E152) Substances 0.000 description 7
- 230000003197 catalytic effect Effects 0.000 description 7
- 150000001875 compounds Chemical class 0.000 description 7
- 239000002994 raw material Substances 0.000 description 7
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 5
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 5
- 229910021529 ammonia Inorganic materials 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 150000002894 organic compounds Chemical class 0.000 description 5
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 4
- 150000001805 chlorine compounds Chemical class 0.000 description 4
- 230000009849 deactivation Effects 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- 239000003350 kerosene Substances 0.000 description 4
- 150000002739 metals Chemical class 0.000 description 4
- CWQXQMHSOZUFJS-UHFFFAOYSA-N molybdenum disulfide Chemical compound S=[Mo]=S CWQXQMHSOZUFJS-UHFFFAOYSA-N 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 3
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 3
- 229910052759 nickel Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 239000010941 cobalt Substances 0.000 description 2
- 229910017052 cobalt Inorganic materials 0.000 description 2
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 230000006866 deterioration Effects 0.000 description 2
- 150000001993 dienes Chemical class 0.000 description 2
- QMMFVYPAHWMCMS-UHFFFAOYSA-N dimethyl monosulfide Natural products CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910052982 molybdenum disulfide Inorganic materials 0.000 description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 2
- 239000003209 petroleum derivative Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 2
- 229910052721 tungsten Inorganic materials 0.000 description 2
- 239000010937 tungsten Substances 0.000 description 2
- ZPFAVCIQZKRBGF-UHFFFAOYSA-N 1,3,2-dioxathiolane 2,2-dioxide Chemical compound O=S1(=O)OCCO1 ZPFAVCIQZKRBGF-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- BWGNESOTFCXPMA-UHFFFAOYSA-N Dihydrogen disulfide Chemical compound SS BWGNESOTFCXPMA-UHFFFAOYSA-N 0.000 description 1
- WQOXQRCZOLPYPM-UHFFFAOYSA-N Dimethyl disulfide Natural products CSSC WQOXQRCZOLPYPM-UHFFFAOYSA-N 0.000 description 1
- PLUBXMRUUVWRLT-UHFFFAOYSA-N Ethyl methanesulfonate Chemical compound CCOS(C)(=O)=O PLUBXMRUUVWRLT-UHFFFAOYSA-N 0.000 description 1
- 229910003294 NiMo Inorganic materials 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000002154 agricultural waste Substances 0.000 description 1
- ILRRQNADMUWWFW-UHFFFAOYSA-K aluminium phosphate Chemical compound O1[Al]2OP1(=O)O2 ILRRQNADMUWWFW-UHFFFAOYSA-K 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000012298 atmosphere Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000006298 dechlorination reaction Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 238000007429 general method Methods 0.000 description 1
- 229940015043 glyoxal Drugs 0.000 description 1
- 238000007602 hot air drying Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 150000002736 metal compounds Chemical class 0.000 description 1
- MBABOKRGFJTBAE-UHFFFAOYSA-N methyl methanesulfonate Chemical compound COS(C)(=O)=O MBABOKRGFJTBAE-UHFFFAOYSA-N 0.000 description 1
- JZMJDSHXVKJFKW-UHFFFAOYSA-M methyl sulfate(1-) Chemical compound COS([O-])(=O)=O JZMJDSHXVKJFKW-UHFFFAOYSA-M 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- -1 niobia Substances 0.000 description 1
- 239000012299 nitrogen atmosphere Substances 0.000 description 1
- 229910017464 nitrogen compound Inorganic materials 0.000 description 1
- 150000002830 nitrogen compounds Chemical class 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 229920001021 polysulfide Polymers 0.000 description 1
- 239000005077 polysulfide Substances 0.000 description 1
- 150000008117 polysulfides Polymers 0.000 description 1
- AUMOHRGUCCHLKI-UHFFFAOYSA-N prop-1-enyl 1-cyanoethanesulfonate Chemical compound C(#N)C(C)S(=O)(=O)OC=CC AUMOHRGUCCHLKI-UHFFFAOYSA-N 0.000 description 1
- CEOMSMHXJAWWED-UHFFFAOYSA-N prop-1-enyl prop-1-ene-1-sulfonate Chemical compound CC=COS(=O)(=O)C=CC CEOMSMHXJAWWED-UHFFFAOYSA-N 0.000 description 1
- DKORSYDQYFVQNS-UHFFFAOYSA-N propyl methanesulfonate Chemical compound CCCOS(C)(=O)=O DKORSYDQYFVQNS-UHFFFAOYSA-N 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- BDHFUVZGWQCTTF-UHFFFAOYSA-M sulfonate Chemical compound [O-]S(=O)=O BDHFUVZGWQCTTF-UHFFFAOYSA-M 0.000 description 1
- 229920003051 synthetic elastomer Polymers 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 229920001059 synthetic polymer Polymers 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 239000005061 synthetic rubber Substances 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 description 1
- 229920002554 vinyl polymer Polymers 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000010920 waste tyre Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/06—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/08—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by treating with water
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/72—Controlling or regulating
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
- C10G2300/1007—Used oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4081—Recycling aspects
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/42—Hydrogen of special source or of special composition
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
- C10G2300/708—Coking aspect, coke content and composition of deposits
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/80—Additives
Definitions
- the present disclosure relates to a method of treating waste plastic pyrolysis oil.
- Waste plastics which are produced using petroleum as a raw material, are not recyclable and are mostly disposed of as garbage. These wastes take a long time to degrade in nature, causing contamination of the soil and serious environmental pollution.
- waste plastics may be pyrolyzed and converted into usable oil, which is called waste plastic pyrolysis oil.
- pyrolysis oil obtained by pyrolyzing waste plastics may not be immediately used as a high-value-added fuel such as gasoline or diesel oil because it has a higher content of impurities such as chlorine, nitrogen, and metals compared to fractions produced from crude oil by a general method.
- a refinery process such as hydrotreating has been performed to remove the impurities.
- the waste plastic pyrolysis oil contains water, chlorine, and nitrogen, which causes problems such as equipment corrosion, a reduction in the activity of a catalyst, and deterioration of properties of a product during hydrotreating.
- ammonia and hydrogen chloride formed during hydrotreating react with each other to produce an ammonium chloride salt (NH 4 Cl), and the ammonium chloride salt causes corrosion of a subsequent Equipmemt, which causes a reduction in durability and a lot of process problems such as a reduction in process efficiency due to occurrence of a differential pressure.
- waste plastic pyrolysis oil has a high content of impurities such as metals, which affects the catalyst in the hydrotreating process, and accordingly, the activity of the catalyst is rapidly reduced, and thus the process may not be stably performed for a long period of time.
- An object of the present disclosure is to provide a method of treating waste plastic pyrolysis oil that may implement a stable operation for a long period of time without a reduction in the activity of a hydrotreating catalyst.
- Another object of the present disclosure is to provide a method of treating waste plastic pyrolysis oil that may implement a stable operation for a long period of time by suppressing or minimizing formation of an ammonium chloride salt (NH 4 Cl) throughout a process of treating waste plastic pyrolysis oil.
- NH 4 Cl ammonium chloride salt
- Still another object of the present disclosure is to provide a method of treating waste plastic pyrolysis oil by which high-quality high-value-added fuel having a significantly reduced content of impurities such as chlorine, nitrogen, oxygen, and metals may be obtained.
- a method of treating waste plastic pyrolysis oil includes: a first step of washing waste plastic pyrolysis oil with water and then removing moisture; a second step of mixing the waste plastic pyrolysis oil from which the moisture is removed and a sulfur source to prepare a mixed oil; a third step of hydrotreating the mixed oil with hydrogen gas in the presence of a hydrotreating catalyst; a fourth step of separating the hydrotreated mixed oil into a liquid stream and a gas stream to obtain liquid pyrolysis oil; and a fifth step of recovering hydrogen gas from the separated gas stream and recycling the recovered hydrogen gas to the third step.
- the waste plastic pyrolysis oil that is subjected to the first step may contain moisture in an amount of 300 to 2,000 ppm.
- the sulfur source in the second step may contain sulfur-containing oil.
- the sulfur source in the second step may be contained in an amount of less than 50 parts by weight based on 100 parts by weight of the waste plastic pyrolysis oil.
- the mixed oil in the second step may contain sulfur in an amount of 100 ppm or more.
- the third step may include a 3-1st step of hydrotreating the mixed oil at a first temperature in the presence of a hydrotreating catalyst to produce a fluid from which olefin, nitrogen, chlorine is removed; and a 3-2nd step of hydrotreating the fluid at a second temperature higher than the first temperature in the presence of a hydrotreating catalyst to produce refined oil from which impurities are removed.
- the first reaction temperature may be higher than 100°C and lower than 400°C
- the second reaction temperature may be higher than 300°C and lower than 450°C.
- a reaction pressure in the hydrotreating in each of the 3-1st step and the 3-2nd step may be more than 10 bar and less than 200 bar.
- liquid hourly space velocities (LHSVs) in the hydrotreating in the 3-1st step and the hydrotreating in the 3-2nd step may be 1:0.1 to 1:2.0.
- the hydrotreated mixed oil may be introduced into a high-temperature and high-pressure separator to separate the hydrotreated mixed oil into a liquid stream and a gas stream.
- the gas stream separated in the high-temperature and high-pressure separator may be sequentially introduced into a low-temperature and high-pressure separator and a low-temperature and low-pressure separator, and the liquid stream separated in the high-temperature and high-pressure separator may be introduced into a high-temperature and low-pressure separator.
- the gas stream separated in the high-temperature and high-pressure separator may be washed with water to suppress formation of a salt.
- the method may further include a step of performing distillation on the liquid pyrolysis oil separated in the fourth step, and in the distillation step, formation of a salt may be suppressed using a salt remover.
- the recovered hydrogen gas may be purified to remove impurities, and then the hydrogen gas from which the impurities are removed may be recycled to the third step.
- the method of treating waste plastic pyrolysis oil according to the present disclosure may implement a stable operation for a long period of time without a reduction in the activity of a hydrotreating catalyst.
- the method of treating waste plastic pyrolysis oil according to the present disclosure may implement a stable operation for a long period of time by suppressing or minimizing formation of an ammonium chloride salt (NH 4 Cl) throughout a process.
- an ammonium chloride salt NH 4 Cl
- high-quality high-value-added fuel having a significantly reduced content of impurities such as chlorine, nitrogen, oxygen, and metals may be obtained.
- hydrogen gas is recovered from the separated waste gas and the recovered hydrogen gas is reused, such that cost-effectiveness may be improved.
- a numerical range used in the present specification includes upper and lower limits and all values within these limits, all double limited values, and all possible combinations of the upper and lower limits in the numerical range defined in different forms. Unless otherwise specifically defined in the present specification, values out of the numerical ranges that may occur due to experimental errors or rounded values also fall within the defined numerical ranges.
- the present disclosure provides a method of treating waste plastic pyrolysis oil, the method including: a first step of washing waste plastic pyrolysis oil with water and then removing moisture; a second step of mixing the waste plastic pyrolysis oil from which the moisture is removed and a sulfur source to prepare a mixed oil; a third step of hydrotreating the mixed oil with hydrogen gas in the presence of a hydrotreating catalyst; a fourth step of separating the hydrotreated mixed oil into a liquid stream and a gas stream to obtain liquid pyrolysis oil; and a fifth step of recovering hydrogen gas from the separated gas stream and recycling the recovered hydrogen gas to the third step.
- the waste plastic pyrolysis oil may be a mixture of hydrocarbon oils produced by pyrolyzing waste plastics at a high temperature.
- the waste plastics may include solid or liquid waste related to synthetic polymer compounds such as a waste synthetic resin, a waste synthetic fiber, waste synthetic rubber, and waste vinyl.
- the waste plastics may be household waste plastics or industrial or agricultural waste plastics.
- the waste plastic pyrolysis oil may contain impurities such as a chlorine compound, a nitrogen compound, and a metal compound in addition to the hydrocarbon oil, and may contain an excessive amount of moisture. Both organic chlorine and inorganic chlorine may be present in the chlorine compound.
- a content of the chlorine compound in the waste plastic pyrolysis oil may be 50 ppm or more, and specifically, may be 300 ppm or more.
- An upper limit of the content of the chlorine compound is not particularly limited, and may be, for example, 3,000 ppm or less, and specifically, 1,500 ppm or less.
- the waste plastic pyrolysis oil may contain an excessive amount of moisture. Since waste plastics are usually collected or discarded in a state of containing moisture, pyrolysis oil produced from the waste plastics contains an excessive amount of moisture.
- a content of the moisture contained in the waste plastic pyrolysis oil may be 300 ppm or more, and specifically, 500 ppm or more.
- An upper limit of the content of the moisture is not particularly limited, and for example, may be 3,000 ppm or less.
- the waste plastic pyrolysis oil may contain 500 ppm or more of nitrogen, 100 ppm of chlorine, and 2,000 ppm or more of moisture, or may contain 20 vol% or more (based on 1 atm and 25°C) of olefins and 1 vol% or more (based on 1 atm and 25°C) of conjugated diolefins, but a content of the impurities is merely a specific example that may be included in the waste plastic pyrolysis oil, and a composition of the waste plastic pyrolysis oil is not limited thereto.
- the excessive amount of moisture and the impurities such as chlorine and nitrogen contained in the waste plastic pyrolysis oil may cause deactivation of the catalyst in a hydrogenation process or may cause problems such as equipment corrosion. Accordingly, the first step of washing the waste plastic pyrolysis oil with water and then removing the moisture is performed to simultaneously remove impurities and moisture contained in the pyrolysis oil, such that process stability and quality improvement of refined oil may be promoted.
- washing water is supplied to the waste plastic pyrolysis oil and the waste plastic pyrolysis oil is washed with water to discharge an aqueous solution containing chlorine and nitrogen, such that impurities including chlorine in the waste plastic pyrolysis oil may be removed.
- Moisture remaining in the waste plastic pyrolysis oil may be removed by performing a drying dehydration process such as hot air drying or by an oil-water separation, centrifugal separation, or distillation method.
- the first step may be performed at 30 to 250°C and 2 to 50 bar.
- the first step may be performed in an inert atmosphere, for example, a nitrogen atmosphere, and in a case where a water treatment process is performed under the above conditions, impurity removal efficiency may be improved.
- the waste plastic pyrolysis oil that is subjected to the first step may contain moisture in an amount of 300 to 2,000 ppm. Moisture present in the waste plastic pyrolysis oil may be effectively reduced through the first step.
- the waste plastic pyrolysis oil and the sulfur source are mixed to prepare the mixed oil in the second step, such that deactivation of the hydrotreating catalyst due to an insufficient sulfur source and a high-temperature operation during the reaction and the separation and refinery processes may be suppressed, and the activity of the catalyst may be maintained.
- the sulfur source refers to a sulfur source capable of continuously supplying a sulfur component during the refinery process.
- the hydrotreating catalyst may refer to a commonly used hydrotreating catalyst, but as described below, the hydrotreating catalyst may refer to a molybdenum-based hydrotreating catalyst, and specifically, a molybdenum-based sulfide hydrotreating catalyst, in terms of improving the activity of the catalyst by the sulfur source.
- the sulfur source may contain sulfur-containing oil.
- the sulfur-containing oil refers to oil composed of hydrocarbons containing sulfur obtained from crude oil as a raw material.
- the sulfur-containing oil is not particularly limited as long as it is an oil containing sulfur, and the sulfur-containing oil may be, for example, light gas oil, straight-run naphtha, vacuum naphtha, pyrolysis naphtha, straight-run kerosene, vacuum kerosene, pyrolysis kerosene, straight-run gas oil, vacuum gas oil, pyrolysis gas oil, sulfur-containing waste tire oil, and any mixture thereof.
- the sulfur-containing oil may be contained in an amount of less than 50 parts by weight based on 100 parts by weight of the waste plastic pyrolysis oil. Specifically, the sulfur-containing oil may be contained in an amount of less than 40 parts by weight.
- the sulfur source may contain a sulfur-containing organic compound instead of or together with sulfur-containing oil.
- the sulfur-containing organic compound may be one or two or more compounds selected from a disulfide-based compound, a sulfide-based compound, a sulfonate-based compound, and a sulfate-based compound.
- the sulfur-containing organic compound may include one or a mixture of two or more selected from disulfide, dimethyl disulfide, dimethyl sulfide, polysulfide, dimethyl sulfoxide (DMSO), methyl methanesulfonate, ethyl methanesulfonate, propyl methanesulfonate, propenyl propenesulfonate, propenyl cyanoethansulfonate, ethylene sulfate, bicyclo-glyoxal sulfate, and methyl sulfate.
- DMSO dimethyl sulfoxide
- the sulfur-containing organic compound may be contained in an amount of 0.001 to 50 parts by weight based on 100 parts by weight of the waste plastic pyrolysis oil.
- a content of sulfur component supplied is small, such that the effect of preventing deactivation of the hydrotreating catalyst may be insufficient.
- the third step of hydrotreating the mixed oil with the hydrogen gas in the presence of the hydrotreating catalyst refers to hydrogenation in which hydrogen gas is added to the hydrocarbon oil included in the mixed oil.
- the hydrotreating may refer to conventionally known hydrotreating including hydrodesulfurization, hydrocracking, hydrodechlorination, hydrodenitrogenation, and hydrodemetallization. Impurities including chlorine (Cl) and nitrogen (N), olefins, and other metal impurities may be removed by the hydrotreating.
- the third step may include a 3-1st step of hydrotreating the mixed oil at a first temperature in the presence of a hydrotreating catalyst to produce a fluid from which olefins are removed; and a 3-2nd step of hydrotreating the fluid at a second temperature higher than the first temperature in the presence of a hydrotreating catalyst to produce refined oil from which impurities are removed.
- the type of each component removed in the hydrotreating may be determined by a reaction temperature.
- the hydrotreating in the 3-1st step may be performed at a first temperature to mainly remove olefins, and the hydrotreating in the 3-2nd step may be performed at a second temperature higher than the first temperature to mainly remove impurities including chlorine and nitrogen.
- the hydrotreating in the 3-1st step and the hydrotreating in the 3-2nd step may be performed consecutively, but olefins are first removed in the 3-1st step, and then impurities including chlorine and nitrogen are removed in the 3-2nd step, such that it is possible to minimize formation and accumulation of materials that cause a differential pressure, such as oligomers, in the reactor.
- the first temperature may be higher than 100°C and lower than 400°C
- the second temperature may be higher than 300°C and lower than 450°C.
- a difference between the first temperature and the second temperature may be 50 to 350°C, and specifically, 50 to 280°C, but this is only an example, and the difference between the first temperature and the second temperature is not limited thereto.
- olefins may be intensively removed. Specifically, hydrogenation of the waste plastic pyrolysis oil is performed in the presence of a hydrotreating catalyst, and most of the olefins from the waste plastic pyrolysis oil are saturated to produce paraffins. In addition, some impurities such as chlorine are removed from the waste plastic pyrolysis oil, and other metal impurities are removed.
- the first temperature may be 100 to 400°C.
- the hydrotreating is performed in a range of the second temperature, impurities including chlorine and nitrogen may be removed.
- the second temperature is 300°C or lower, the impurities in the waste plastic pyrolysis oil may not be effectively removed, which may cause deterioration of product quality.
- the second temperature is 450°C or higher, a side reaction of thermal cracking excessively occurs, which may cause deactivation of the catalyst such as coking.
- the second temperature is 320 to 420°C, the activity of the catalyst may be maintained, which is preferable.
- a reaction pressure in the hydrotreating in each of the 3-1st step and the 3-2nd step may be more than 10 bar and less than 200 bar. Under a low pressure condition of 10 bar or less, impurities including chlorine and nitrogen may not be effectively removed. Under a high pressure condition of 200 bar or more, formation of an ammonium chloride salt (NH 4 Cl) is promoted. Specifically, the reaction pressure may be 30 bar to 180 bar.
- liquid hourly space velocities (LHSVs) in the hydrotreating in the 3-1st step and the hydrotreating in the 3-2nd step may be 1:0.1 to 1:2.0.
- LHSVs liquid hourly space velocities
- the hydrotreating catalyst various types of known catalysts may be used as long as they are catalysts for performing hydrogenation in which hydrogen is added to the hydrocarbon oil of the waste plastic pyrolysis oil.
- the hydrotreating catalyst may include one or two or more selected from a hydrodesulfurization catalyst, a hydrodenitrogenation catalyst, a hydrodechlorination catalyst, and a hydrodemetallization catalyst.
- a hydrodesulfurization catalyst a hydrodenitrogenation catalyst
- a hydrodechlorination catalyst a hydrodemetallization catalyst.
- Such a catalyst allows a demetallization reaction to be performed and allows a denitrification reaction or a dechlorination reaction to be performed at the same time according to conditions such as the temperature described above.
- the hydrotreating catalyst may contain an active metal having the hydrotreating catalytic ability, and preferably, an active metal may be supported on a support.
- any active metal may be used as long as it has a required catalytic ability, and for example, the active metal may include one or more selected from molybdenum and nickel.
- the support any support may be used as long as it has durability enough to support an active metal.
- the hydrotreating catalyst is a molybdenum-based hydrotreating catalyst, and specifically, a molybdenum-based sulfide hydrotreating catalyst, in terms of improving the activity of the catalyst by the sulfur source.
- the molybdenum-based hydrotreating catalyst may be a catalyst in which a molybdenum-based metal, or a metal including one or two or more selected from nickel, cobalt, and tungsten and a molybdenum-based metal are supported on a support.
- the molybdenum-based hydrotreating catalyst has high catalytic activity during hydrotreating, and the molybdenum-based hydrotreating catalysts may be used alone or, if necessary, in the form of a two-way catalyst combined with a metal such as nickel, cobalt, or tungsten.
- alumina, silica, silica-alumina, titanium oxide, a molecular sieve, zirconia, aluminum phosphate, carbon, niobia, or a mixture thereof may be used, but the present disclosure is not limited thereto.
- the molybdenum-based sulfide hydrotreating catalyst may contain, for example, molybdenum sulfide (MoS) or molybdenum disulfide (MoS 2 ), but is not limited thereto, and may include a known molybdenum-based sulfide hydrotreating catalyst.
- MoS molybdenum sulfide
- MoS 2 molybdenum disulfide
- the mixed oil hydrotreated in the third step may be separated into a liquid stream and a gas stream to obtain liquid pyrolysis oil.
- the hydrotreated mixed oil may be introduced into a high-temperature and high-pressure separator to separate the hydrotreated mixed oil into a liquid stream and a gas stream.
- a gas stream and a liquid stream separated from impurities may be obtained from the mixed oil through the high-temperature and high-pressure separator.
- a cooling process may be performed before the hydrotreated mixed oil is introduced into the high-temperature and high-pressure separator.
- the gas stream separated in the high-temperature and high-pressure separator may be sequentially introduced into a low-temperature and high-pressure separator and a low-temperature and low-pressure separator, and the liquid stream separated in the high-temperature and high-pressure separator may be introduced into a high-temperature and low-pressure separator.
- the gas stream separated in the high-temperature and high-pressure separator may be sequentially introduced into a low-temperature and high-pressure separator and a low-temperature and low-pressure separator to finally discharge and remove gas, and in this process, a part of the gas stream may be liquefied again and recovered as a liquid stream.
- the liquid stream separated in the high-temperature and high-pressure separator may be introduced into a high-temperature and low-pressure separator to finally recover a high-quality liquid stream.
- the gas stream separated in the high-temperature and high-pressure separator may be washed with water to suppress formation of a salt.
- the gas stream is washed with water, such that it is possible to prevent formation of an ammonium chloride salt (NH 4 Cl) by ammonia and hydrogen chloride.
- the water washing process may be performed at least twice.
- the fifth step is a step of recovering hydrogen gas from the separated gas stream and recycling the recovered hydrogen gas to the third step, and the gas stream may contain unreacted hydrogen gas, a trace of methane (CH 4 ) or ethane (C 2 H 6 ), and the like.
- the gas stream may contain hydrogen sulfide gas (H 2 S), hydrogen chloride (HCl), ammonia (NH 3 ), or water vapor (H 2 O) generated by reacting chlorine (Cl), nitrogen (N), sulfur (S), or oxygen (O) with hydrogen gas.
- Hydrogen gas is recovered from the gas stream and the recovered hydrogen gas is recycled to the third step, such that cost-effectiveness may be enhanced and reaction efficiency may be improved.
- the recovered hydrogen gas may be purified to remove impurities, and then the hydrogen gas from which the impurities are removed may be recycled to the third step.
- the recovered hydrogen gas may contain other impurities such as hydrogen chloride (HCl), and ammonia (NH 3 ). Therefore, a purification step is performed, such that the purity of the hydrogen gas may be improved by 90% or more and the hydrogen gas with improved purity may be recycled to the third step.
- the purification may be performed by washing the hydrogen gas with water, and the water washing process may be performed at least once.
- the method may further include a step of performing distillation on the liquid pyrolysis oil separated in the fourth step, and in the distillation step, formation of a salt may be suppressed using a salt remover.
- the liquid pyrolysis oil separated in the fourth step contains minimized impurities, and may contain less than 10 ppm of chlorine (Cl), less than 10 ppm of nitrogen (N), and less than 2,000 ppm of moisture.
- the liquid pyrolysis oil may contain less than 3 wt% of olefins, and may contain 0.5 wt% or less of conjugated diolefins.
- the pyrolysis oil is introduced into a fractionator to perform distillation, such that a petroleum product with minimized impurities may be finally recovered.
- the petroleum product may be recovered at different boiling points, for example, may be recovered as 5 to 35 wt% of Naphtha (bp 150°C or lower), 10 to 60 wt% of Kerosene (bp 150 to 265°C), 20 to 40 wt% of Light gas oil(bp 265 to 380°C), and 5 to 40 wt% of Atmospheric Residue (bp 380°C or higher), but is not limited thereto.
- the gas stream is washed with water using a salt remover, such that it is possible to prevent formation of an ammonium chloride salt (NH 4 Cl) by ammonia and hydrogen chloride.
- a salt remover a known salt remover capable of suppressing formation of an ammonium chloride salt (NH 4 Cl) may be used.
- Waste plastics were pyrolyzed to prepare 1,000 g of a waste plastic pyrolysis oil raw material. 560 ppm of chlorine, 1,080 ppm of nitrogen, and 2,200 ppm of moisture were contained in the waste plastic pyrolysis oil raw material.
- the waste plastic pyrolysis oil was washed with 200 g of washing water. Thereafter, the washed waste plastic pyrolysis oil was dried with hot air at 130°C and 5 bar to remove moisture, and then only oil was recovered.
- the prepared mixed oil and hydrogen gas were put into a reactor, and the reactor was operated, thereby hydrotreating the mixed oil.
- the mixed oil was hydrotreated with a reaction gas containing hydrogen gas (H 2 ) in the presence of a NiMo hydrotreating catalyst at 350°C and 60 bar.
- the hydrotreated mixed oil was separated into a liquid stream and a gas stream. Specifically, the hydrotreated mixed oil was put into a high-temperature and high-pressure separator to separate the hydrotreated mixed oil into a liquid stream and a gas stream so as to recover the liquid stream, thereby obtaining refined oil with minimized impurities. In addition, the hydrogen gas was recovered from the separated gas stream, and the recovered hydrogen gas was recycled to the hydrotreating reactor.
- Example 1 the waste plastic pyrolysis oil raw material was directly put into the reactor to perform hydrotreating. That is, the reaction was performed under the same conditions as those of Example 1, except that the water washing and moisture removal processes and the process of mixing with the sulfur-containing hydrocarbon oil were omitted.
- the catalytic activity retention time was measured and expressed in days based on the time point when the content of nitrogen in the refined oil exceeded 10 ppm by performing a Total Nitrogen & Sulfur (TNS element) analysis on the refined oil.
- TMS element Total Nitrogen & Sulfur
- Example 1 Comparative Example 1 Chlorine content (ppm) ⁇ 9 > 320 Moisture content (ppm) ⁇ 330 > 1,500 Catalytic activity retention time (day) > 18 4
- Example 1 as the method of treating waste plastic pyrolysis oil of the present disclosure was performed, it could be confirmed that the content of chlorine in the finally obtained waste plastic pyrolysis oil was removed to a level of a few ppm or less and high-quality refined oil with minimized impurities was obtained. In addition, it could be confirmed that the catalytic activity was continuously maintained for 18 days or longer.On the other hand, in Comparative Example 1, as the water washing and moisture removal processes and the process of mixing with the sulfur-containing hydrocarbon oil were omitted, it could be confirmed that the content of chlorine in the pyrolysis oil was 320 ppm and the catalytic activity retention time was significantly reduced to 4 days or shorter.
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Abstract
La présente invention concerne un procédé de traitement d'huile de pyrolyse de déchets plastiques, le procédé comprenant : une première étape de lavage d'huile de pyrolyse de déchets plastiques avec de l'eau puis d'élimination de l'humidité ; une deuxième étape de mélange de l'huile de pyrolyse de déchets plastiques de laquelle l'humidité est éliminée et une source de soufre pour préparer une huile mélangée ; une troisième étape d'hydrotraitement de l'huile mélangée avec de l'hydrogène gazeux en présence d'un catalyseur d'hydrotraitement ; une quatrième étape de séparation de l'huile mélangée hydrotraitée en un courant de liquide et un courant de gaz pour obtenir une huile de pyrolyse liquide ; et une cinquième étape de récupération d'hydrogène gazeux du courant de gaz séparé et de recyclage de l'hydrogène gazeux récupéré vers la troisième étape.
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KR10-2022-0044889 | 2022-04-12 | ||
KR1020220044889A KR20230146210A (ko) | 2022-04-12 | 2022-04-12 | 폐플라스틱 열분해유의 처리 방법 |
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Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2020239729A1 (fr) * | 2019-05-28 | 2020-12-03 | Neste Oyj | Purification hydrothermale améliorée par un alcali d'huiles de pyrolyse du plastique |
WO2021110395A1 (fr) * | 2019-12-02 | 2021-06-10 | IFP Energies Nouvelles | Procede de traitement d'huiles de pyrolyse de plastiques en vue de leur valorisation dans une unite de vapocraquage |
CN113348227A (zh) * | 2019-01-30 | 2021-09-03 | 格林菲尔德全球有限公司 | 一种生产合成喷气燃料的方法 |
WO2021204819A1 (fr) * | 2020-04-07 | 2021-10-14 | Total Research & Technology Feluy | Purification d'huile à base de déchets plastiques avec un premier piège et un premier hydrotraitement et un second piège et un second hydrotraitement |
EP3907267A1 (fr) * | 2020-05-08 | 2021-11-10 | Basf Se | Procédé de purification d'une huile de pyrolyse brute provenant de la pyrolyse de déchets plastiques |
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US4338186A (en) * | 1980-11-17 | 1982-07-06 | Suntech, Inc. | Shale oil process |
US7834226B2 (en) * | 2007-12-12 | 2010-11-16 | Chevron U.S.A. Inc. | System and method for producing transportation fuels from waste plastic and biomass |
US8329967B2 (en) * | 2008-04-06 | 2012-12-11 | Uop Llc | Production of blended fuel from renewable feedstocks |
WO2016142809A1 (fr) * | 2015-03-10 | 2016-09-15 | Sabic Global Technologies, B.V. | Procédé robuste intégré pour la conversion de déchets de matières plastiques en produits pétrochimiques finis |
GB201903080D0 (en) * | 2019-03-07 | 2019-04-24 | Oxford Sustainable Fuels Ltd | Process |
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2022
- 2022-04-12 KR KR1020220044889A patent/KR20230146210A/ko unknown
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2023
- 2023-02-08 WO PCT/KR2023/095003 patent/WO2023200321A1/fr unknown
- 2023-03-31 US US18/129,297 patent/US20230323221A1/en active Pending
- 2023-05-30 US US18/203,376 patent/US20230323222A1/en active Pending
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
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CN113348227A (zh) * | 2019-01-30 | 2021-09-03 | 格林菲尔德全球有限公司 | 一种生产合成喷气燃料的方法 |
WO2020239729A1 (fr) * | 2019-05-28 | 2020-12-03 | Neste Oyj | Purification hydrothermale améliorée par un alcali d'huiles de pyrolyse du plastique |
WO2021110395A1 (fr) * | 2019-12-02 | 2021-06-10 | IFP Energies Nouvelles | Procede de traitement d'huiles de pyrolyse de plastiques en vue de leur valorisation dans une unite de vapocraquage |
WO2021204819A1 (fr) * | 2020-04-07 | 2021-10-14 | Total Research & Technology Feluy | Purification d'huile à base de déchets plastiques avec un premier piège et un premier hydrotraitement et un second piège et un second hydrotraitement |
EP3907267A1 (fr) * | 2020-05-08 | 2021-11-10 | Basf Se | Procédé de purification d'une huile de pyrolyse brute provenant de la pyrolyse de déchets plastiques |
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US20230323221A1 (en) | 2023-10-12 |
KR20230146210A (ko) | 2023-10-19 |
US20230323222A1 (en) | 2023-10-12 |
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