CN114437775B - Method and system for producing aromatic hydrocarbon extraction raw material from waste plastic oil and/or waste tire oil - Google Patents
Method and system for producing aromatic hydrocarbon extraction raw material from waste plastic oil and/or waste tire oil Download PDFInfo
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- CN114437775B CN114437775B CN202011189181.9A CN202011189181A CN114437775B CN 114437775 B CN114437775 B CN 114437775B CN 202011189181 A CN202011189181 A CN 202011189181A CN 114437775 B CN114437775 B CN 114437775B
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- waste
- oil
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- 239000002699 waste material Substances 0.000 title claims abstract description 97
- 239000004033 plastic Substances 0.000 title claims abstract description 66
- 229920003023 plastic Polymers 0.000 title claims abstract description 66
- 238000000034 method Methods 0.000 title claims abstract description 52
- 239000002994 raw material Substances 0.000 title claims abstract description 30
- 239000010920 waste tyre Substances 0.000 title claims abstract description 29
- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 27
- 238000000605 extraction Methods 0.000 title claims abstract description 20
- 238000006243 chemical reaction Methods 0.000 claims abstract description 110
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 62
- 239000000463 material Substances 0.000 claims abstract description 62
- 239000012535 impurity Substances 0.000 claims abstract description 54
- 239000007791 liquid phase Substances 0.000 claims abstract description 42
- 239000003502 gasoline Substances 0.000 claims abstract description 22
- 239000003054 catalyst Substances 0.000 claims description 109
- 238000005984 hydrogenation reaction Methods 0.000 claims description 106
- 239000003921 oil Substances 0.000 claims description 106
- 229910052751 metal Inorganic materials 0.000 claims description 58
- 239000002184 metal Substances 0.000 claims description 50
- 239000001257 hydrogen Substances 0.000 claims description 31
- 229910052739 hydrogen Inorganic materials 0.000 claims description 31
- 239000003795 chemical substances by application Substances 0.000 claims description 27
- 230000000382 dechlorinating effect Effects 0.000 claims description 27
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 26
- 229910052710 silicon Inorganic materials 0.000 claims description 26
- 239000010703 silicon Substances 0.000 claims description 26
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 24
- 239000004215 Carbon black (E152) Substances 0.000 claims description 22
- 229930195733 hydrocarbon Natural products 0.000 claims description 22
- 150000002430 hydrocarbons Chemical class 0.000 claims description 22
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 18
- 239000000460 chlorine Substances 0.000 claims description 18
- 229910052801 chlorine Inorganic materials 0.000 claims description 18
- 229910052799 carbon Inorganic materials 0.000 claims description 16
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 14
- 229910044991 metal oxide Inorganic materials 0.000 claims description 14
- 150000004706 metal oxides Chemical class 0.000 claims description 14
- 229910052717 sulfur Inorganic materials 0.000 claims description 14
- 239000011593 sulfur Substances 0.000 claims description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- 239000012071 phase Substances 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 12
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- 238000004821 distillation Methods 0.000 claims description 10
- 238000004227 thermal cracking Methods 0.000 claims description 10
- 229910021536 Zeolite Inorganic materials 0.000 claims description 9
- 239000010457 zeolite Substances 0.000 claims description 9
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 8
- 150000002431 hydrogen Chemical class 0.000 claims description 7
- 239000010813 municipal solid waste Substances 0.000 claims description 7
- 238000012545 processing Methods 0.000 claims description 7
- 229920006395 saturated elastomer Polymers 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 229910000480 nickel oxide Inorganic materials 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 claims description 6
- 239000003223 protective agent Substances 0.000 claims description 6
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 claims description 5
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 claims description 5
- 229910052794 bromium Inorganic materials 0.000 claims description 5
- 239000004927 clay Substances 0.000 claims description 5
- 229910000428 cobalt oxide Inorganic materials 0.000 claims description 5
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical compound [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 claims description 5
- 238000004090 dissolution Methods 0.000 claims description 5
- 229910000476 molybdenum oxide Inorganic materials 0.000 claims description 5
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 5
- PQQKPALAQIIWST-UHFFFAOYSA-N oxomolybdenum Chemical compound [Mo]=O PQQKPALAQIIWST-UHFFFAOYSA-N 0.000 claims description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 4
- 239000011230 binding agent Substances 0.000 claims description 4
- 238000007233 catalytic pyrolysis Methods 0.000 claims description 4
- 229910052802 copper Inorganic materials 0.000 claims description 4
- 150000002736 metal compounds Chemical class 0.000 claims description 4
- QGLKJKCYBOYXKC-UHFFFAOYSA-N nonaoxidotritungsten Chemical compound O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1 QGLKJKCYBOYXKC-UHFFFAOYSA-N 0.000 claims description 4
- 229910001930 tungsten oxide Inorganic materials 0.000 claims description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 238000011049 filling Methods 0.000 claims description 3
- 238000009396 hybridization Methods 0.000 claims description 3
- 229910052814 silicon oxide Inorganic materials 0.000 claims description 3
- 244000043261 Hevea brasiliensis Species 0.000 claims description 2
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 2
- 238000012271 agricultural production Methods 0.000 claims description 2
- VIJYFGMFEVJQHU-UHFFFAOYSA-N aluminum oxosilicon(2+) oxygen(2-) Chemical compound [O-2].[Al+3].[Si+2]=O VIJYFGMFEVJQHU-UHFFFAOYSA-N 0.000 claims description 2
- 229910017052 cobalt Inorganic materials 0.000 claims description 2
- 239000010941 cobalt Substances 0.000 claims description 2
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 2
- 238000009776 industrial production Methods 0.000 claims description 2
- 229910052750 molybdenum Inorganic materials 0.000 claims description 2
- 239000011733 molybdenum Substances 0.000 claims description 2
- 229920003052 natural elastomer Polymers 0.000 claims description 2
- 229920001194 natural rubber Polymers 0.000 claims description 2
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 claims description 2
- 229920003051 synthetic elastomer Polymers 0.000 claims description 2
- 239000005061 synthetic rubber Substances 0.000 claims description 2
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 claims description 2
- 229910052721 tungsten Inorganic materials 0.000 claims description 2
- 239000010937 tungsten Substances 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 2
- 229910001928 zirconium oxide Inorganic materials 0.000 claims description 2
- 125000003118 aryl group Chemical group 0.000 abstract description 4
- 239000007795 chemical reaction product Substances 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 12
- 239000000203 mixture Substances 0.000 description 9
- 238000006298 dechlorination reaction Methods 0.000 description 7
- 239000002283 diesel fuel Substances 0.000 description 7
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 6
- 239000007789 gas Substances 0.000 description 5
- 150000001336 alkenes Chemical class 0.000 description 4
- -1 ethylene, propylene Chemical group 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 238000000197 pyrolysis Methods 0.000 description 4
- 238000007670 refining Methods 0.000 description 4
- 239000005995 Aluminium silicate Substances 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 description 3
- 235000012211 aluminium silicate Nutrition 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 3
- 239000000295 fuel oil Substances 0.000 description 3
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 241000219793 Trifolium Species 0.000 description 2
- 229910000323 aluminium silicate Inorganic materials 0.000 description 2
- HPTYUNKZVDYXLP-UHFFFAOYSA-N aluminum;trihydroxy(trihydroxysilyloxy)silane;hydrate Chemical compound O.[Al].[Al].O[Si](O)(O)O[Si](O)(O)O HPTYUNKZVDYXLP-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000003869 coulometry Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910052621 halloysite Inorganic materials 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229910052809 inorganic oxide Inorganic materials 0.000 description 2
- 239000011344 liquid material Substances 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 150000005673 monoalkenes Chemical class 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 229910052725 zinc Inorganic materials 0.000 description 2
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 1
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 1
- YKTSYUJCYHOUJP-UHFFFAOYSA-N [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] Chemical compound [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] YKTSYUJCYHOUJP-UHFFFAOYSA-N 0.000 description 1
- 229910000272 alkali metal oxide Inorganic materials 0.000 description 1
- 229910000287 alkaline earth metal oxide Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000000440 bentonite Substances 0.000 description 1
- 229910000278 bentonite Inorganic materials 0.000 description 1
- SVPXDRXYRYOSEX-UHFFFAOYSA-N bentoquatam Chemical compound O.O=[Si]=O.O=[Al]O[Al]=O SVPXDRXYRYOSEX-UHFFFAOYSA-N 0.000 description 1
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- GUJOJGAPFQRJSV-UHFFFAOYSA-N dialuminum;dioxosilane;oxygen(2-);hydrate Chemical compound O.[O-2].[O-2].[O-2].[Al+3].[Al+3].O=[Si]=O.O=[Si]=O.O=[Si]=O.O=[Si]=O GUJOJGAPFQRJSV-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 229910052900 illite Inorganic materials 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000002480 mineral oil Substances 0.000 description 1
- 235000010446 mineral oil Nutrition 0.000 description 1
- 229910052901 montmorillonite Inorganic materials 0.000 description 1
- VGIBGUSAECPPNB-UHFFFAOYSA-L nonaaluminum;magnesium;tripotassium;1,3-dioxido-2,4,5-trioxa-1,3-disilabicyclo[1.1.1]pentane;iron(2+);oxygen(2-);fluoride;hydroxide Chemical compound [OH-].[O-2].[O-2].[O-2].[O-2].[O-2].[F-].[Mg+2].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[K+].[K+].[K+].[Fe+2].O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2 VGIBGUSAECPPNB-UHFFFAOYSA-L 0.000 description 1
- 239000003027 oil sand Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000012805 post-processing Methods 0.000 description 1
- 238000000066 reactive distillation Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000003079 shale oil Substances 0.000 description 1
- 150000003377 silicon compounds Chemical class 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000004876 x-ray fluorescence Methods 0.000 description 1
Classifications
-
- 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
-
- 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
- C10G2300/40—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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/30—Aromatics
Abstract
The invention relates to a method and a system for producing an aromatic hydrocarbon extraction raw material from waste plastic oil and/or junked tire oil. The waste plastic oil and/or the waste tire oil are subjected to impurity removal reaction in an impurity removal unit, the obtained reaction effluent is separated to obtain a first fraction, a second fraction and a third fraction, the second fraction enters a hydrofining unit to react, the third fraction enters a catalytic cracking unit to react, the obtained catalytic cracking gasoline also enters the hydrofining unit to react, and the second liquid phase material obtained after the reaction product of the hydrofining unit is separated is an aromatic hydrocarbon extraction raw material. The invention can effectively remove impurities in the waste plastic oil and/or the waste tire oil, and can be combined with the catalytic cracking unit to provide qualified raw materials for the aromatic extraction device. The invention has low cost and long operation period.
Description
Technical Field
The invention relates to the technical field of hydrocarbon raw material treatment, in particular to a method and a system for producing an aromatic hydrocarbon extraction raw material from waste plastic oil and/or waste tire oil.
Background
With the continuous development of urban process in China, urban population rises year by year, the living standard of people is continuously improved, the yield of urban household garbage is continuously increased, and the current urban garbage treatment method mainly comprises landfill, incineration and the like. There are a series of subsequent environmental protection issues, whether incineration or landfill.
The chemical conversion method can convert the plastic garbage into industrial raw materials or fuel oil with utilization value, not only can eliminate environmental pollution, but also can realize sustainable development and utilization of resources, and is an effective way for treating white pollution. At present, the waste plastic oil refining industry has developed a situation of blooming throughout China, and some enterprises build pyrolysis demonstration devices with smaller scale, but the problem of high-value utilization of waste plastic pyrolysis products is still to be effectively solved.
The waste plastic oil, the waste tire oil and the traditional petroleum-based oil converted by various processes have large difference, and the high impurity content, especially the high silicon content, brings great trouble to the subsequent processing. At present, few researches are conducted on deep processing of waste plastic oil and waste tire oil, and much research focuses on the influence of chlorine impurities in the waste plastic oil on post-processing of the waste plastic oil, and the situation that other impurities such as silicon impurities and metal impurities are also contained in the waste plastic oil is not realized, and the serious influence of the impurities on the subsequent processing technology is not realized.
CN104611060a discloses a method for producing clean fuel oil from waste plastics and high aromatic components. After the high aromatic component is mixed with the waste plastic oil, the waste plastic oil passes through a thermal cracking reaction zone, and the thermal cracking reaction zone adopts a mode of combining gradual heating and constant temperature operation; and (3) the obtained pyrolysis gas enters a catalytic reaction zone to be contacted with a catalyst in the catalytic reaction zone for catalytic reaction, and the obtained reaction effluent enters gas-liquid separation to obtain a gas product and a liquid-phase oil product.
CN104726134a discloses a method for producing high-quality gasoline and diesel oil from chlorine-containing plastic oil. The method is characterized in that chlorine-containing plastic oil is injected into a high-temperature dechlorination tower filled with active aluminum oxide for high-temperature dechlorination, a small amount of NaOH aqueous solution is sprayed on the top of the high-temperature dechlorination tower, and the dechlorinated plastic oil enters a catalytic distillation tower filled with a molecular sieve/aluminum oxide catalyst for reaction and rectification; the plastic oil after catalytic distillation enters a hydrogenation refining tower through pressurization, the distillate oil after hydrogenation refining is distilled at a constant pressure, the distillate oil is cut into gasoline and diesel oil according to the distillation temperature, and the heavy oil at the bottom of the tower is mixed with the raw material chlorine-containing plastic oil for re-reaction. The dechlorination catalyst and the sulfide catalyst used in the invention are prepared by selecting proper methods according to the composition and the performance of the plastic oil.
CN102942951a discloses a method for preparing clean diesel oil by hydrogenation of plastic oil, which comprises the following steps: a. mixing the plastic oil and hydrogen, and entering a pre-hydrogenation reactor filled with a hydrogenation protecting catalyst for chemical reaction; b. the effluent of the pre-hydrogenation reactor enters a hot high-pressure separator for separation and gas stripping, and the effluent at the bottom of the hot high-pressure separator and the gas at the top of the cold high-pressure separator enter a main hydrogenation reactor for chemical reaction; c. the effluent of the main hydrogenation reactor enters a cold high-pressure separator for gas-liquid separation, the effluent at the bottom of the cold high-pressure separator enters a cold low-pressure separator for mixing with light oil extracted from the middle part of the cold high-pressure separator, and then enters a fractionating tower for separation, and clean diesel oil fractions with sulfur content less than 5 mug/g and cetane number higher than 50 can be extracted from the lateral line of the fractionating tower.
CN102226103a discloses a method for producing gasoline and diesel oil by using plastic oil. The process is characterized in that firstly, the plastic oil is distilled to obtain a fraction smaller than 300 ℃ and a fraction larger than 300 ℃, then the fraction smaller than 300 ℃ is hydrofined on a sulfide catalyst, the mono-olefin is removed through hydrogenation saturation reaction of mono-olefin, no peculiar smell is produced by desulfurizing, removing nitrogen and removing colloid, and the gasoline and diesel oil mixed oil with high quality is obtained through distillation. The distillate with the distillation temperature of more than 300 ℃ is subjected to reactive distillation and then hydrofining or mixing with plastic oil for re-reaction. The sulfide catalyst used in the invention is prepared by selecting a proper carrier according to the composition and the performance of the pyrolysis plastic oil through a liquid phase method.
The prior art mainly focuses on the dechlorination and refining processes of waste plastic oil, and is not aware that silicon compounds in the waste plastic oil can have serious toxic effects on the hydrogenation catalyst in the prior art and catalysts in other subsequent processes, so that the operation period of the subsequent processes is short, or industrial operation cannot be realized in fact.
Disclosure of Invention
The invention aims to solve the problem of short processing period when waste plastic oil and/or waste tire oil raw materials are processed in the prior art, and provides a method and a system for producing aromatic hydrocarbon extraction raw materials from waste plastic oil and/or waste tire oil.
The first aspect of the invention provides a method for producing an aromatic hydrocarbon extraction raw material from waste plastic oil and/or junked tire oil, comprising the following steps:
(1) The waste plastic oil and/or the waste tire oil raw materials enter a impurity removal reactor to be contacted with a waste hydrogenation catalyst in the presence of hydrogen, impurity removal reaction is carried out under impurity removal reaction conditions, and after gas-liquid separation is carried out on obtained reaction effluent, a first gas-phase material and a first liquid-phase material are obtained, wherein the silicon content of the obtained first liquid-phase material is less than 1 mug/g, and the metal content of the obtained first liquid-phase material is less than 5 mug/g;
fractionating the obtained first liquid phase material to obtain a first fraction, a second fraction and a third fraction, wherein the first fraction is C 5 And a hydrocarbon fraction of C 6 ～C 8 A hydrocarbon fraction, the third fraction being C 9 The above hydrocarbon fractions;
(2) A hydrofining unit, wherein the second fraction obtained in the step (1) enters a hydrofining reactor, contacts with a hydrofining catalyst in the presence of hydrogen, and performs hydrofining reaction under the condition of hydrofining reaction; and (3) carrying out gas-liquid separation on the obtained reaction effluent to obtain a second gas-phase material and a second liquid-phase material, wherein the obtained second liquid-phase material is an aromatic hydrocarbon extraction raw material.
In one embodiment of the present invention, the method further comprises step (3):
(3) The third fraction obtained in the step (1) enters a catalytic cracking unit, contacts with a catalytic cracking catalyst, reacts under the catalytic cracking reaction condition, and at least low-carbon olefin and catalytic cracking gasoline fraction are obtained after the reaction effluent is separated;
the obtained catalytic pyrolysis gasoline fraction is sent to a hydrofining unit in the step (2) to enter a hydrofining reactor.
In one embodiment of the invention, the waste plastic oil is hydrocarbon materials obtained by one or more conversion methods of thermal cracking, catalytic cracking and dissolution liquefaction of waste plastic; the distillation range of the waste plastic oil is 30-700 ℃, the silicon content is less than 10000 mug/g, the chlorine content is less than 10000 mug/g, and the metal content is less than 10000 mug/g. The composition of the waste plastic oil comprises olefin with volume fraction of 5-80%, preferably 5-60%, aromatic hydrocarbon with volume fraction of less than 90%, preferably 2-60%, and alkane with volume fraction of less than 90%, preferably 5-60%.
In the invention, the waste plastic is one or more of waste plastic in fresh household garbage, waste plastic in industrial and agricultural production and waste plastic in aged garbage, and the waste plastic is one or more selected from PE, PP, PS, PVC.
In one embodiment of the invention, the junked tire oil is a hydrocarbon material obtained by one or more conversion methods of thermal cracking, catalytic cracking and dissolution liquefaction of junked tires; the distillation range of the waste tire oil is 30-700 ℃, the silicon content is less than 10000 mug/g, the chlorine content is less than 10000 mug/g, and the metal content is less than 10000 mug/g. The composition of the waste tire oil comprises 5-80% of olefin, preferably 5-60% of aromatic hydrocarbon, less than 90% of aromatic hydrocarbon, preferably 2-60% of aromatic hydrocarbon, and less than 90% of alkane, preferably 5-60% of alkane.
In the invention, the junked tires are various junked tires prepared from natural rubber and/or synthetic rubber.
In the invention, the thermal cracking and thermal cracking reaction refers to a reaction that hydrocarbon molecules including waste plastics and junked tires are decomposed into smaller molecules under the condition of isolating air at high temperature. Depending on the reaction temperature, 600℃or less will be referred to as thermal cracking reaction, and 600℃or more will be referred to as thermal cracking reaction.
In the present invention, the catalytic cracking and catalytic cracking reaction refers to a reaction in which hydrocarbon molecules including waste plastics and junked tires are decomposed into smaller molecules under high temperature conditions and in the presence of a catalyst. Depending on the reaction products, the reaction using low-carbon olefins (ethylene, propylene, and butene) as the target products is called a catalytic cracking reaction, and the reaction using motor gasoline as the target products is called a catalytic cracking reaction.
In the present invention, the dissolution and liquefaction reaction means a reaction in which waste plastics and junked tires are converted from a solid state to a liquid state in the presence of solvent oil and/or an organic solvent.
In one embodiment of the invention, in the stripping unit, the stripping reactor is at least one fixed bed hydrogenation reactor and/or at least one moving bed hydrogenation reactor. And filling a waste hydrogenation catalyst in the fixed bed hydrogenation reactor and/or the moving bed reactor, and allowing waste plastic oil and/or waste tire oil to pass through at least one fixed bed hydrogenation reactor and/or at least one moving bed hydrogenation reactor for desilication, dechlorination, demetallization and other impurity removal reactions.
In one embodiment of the invention, the impurity removal reactor is more than two fixed bed hydrogenation reactors connected in parallel, each reactor is filled with a waste hydrogenation catalyst, the feed is subjected to impurity removal reaction through at least one fixed bed hydrogenation reactor, and when the waste hydrogenation catalyst in the fixed bed hydrogenation reactor is saturated with silicon or metal, the feed is switched to other fixed bed hydrogenation reactors.
In one embodiment of the invention, the spent hydrogenation catalyst in the dehazing reactor is considered to be saturated with silicon or with metal when the silicon content of the liquid phase material in the reaction effluent is greater than or equal to 1 μg/g or when the metal content is greater than or equal to 5 μg/g.
In one embodiment of the invention, the waste hydrogenation catalyst is one or more selected from the group consisting of a protecting agent used from the end of any fixed bed hydrogenation process device in the hydrocarbon oil processing field, a catalyst at the end of the fixed bed hydrogenation process device, a regenerated protecting agent and a regenerated catalyst.
In one embodiment of the invention, the equivalent diameter of the spent hydrogenation catalyst is from 0.5 to 16mm, preferably from 1 to 10mm. The shape of the waste hydrogenation catalyst is not limited, and for example, the shape of the waste hydrogenation catalyst comprises a sphere, and various different shapes such as strip clover, butterfly, raschig ring, honeycomb shape and the like.
In one embodiment of the invention, the waste hydrogenation catalyst comprises, based on the total weight of the waste hydrogenation catalyst, 0-50% by weight of hydrogenation active metal oxide, 0-50% by weight of carbon and 0-40% by weight of sulfur, wherein the hydrogenation active metal is selected from one or more of VIII group metals and VIB group metals.
In one embodiment of the invention, the waste hydrogenation catalyst comprises, based on the total weight of the waste hydrogenation catalyst, 0-50 wt% of molybdenum oxide and/or tungsten oxide, 0-40 wt% of nickel oxide and/or cobalt oxide, 0-30 wt% of carbon and 0-30 wt% of sulfur.
In one embodiment of the invention, the waste hydrogenation catalyst comprises 1-40 wt% of hydrogenation active metal oxide and 20 wt% or less of carbon based on the total weight of the waste hydrogenation catalyst, wherein the hydrogenation active metal is selected from one or more of VIII group metal and VIB group metal.
In one embodiment of the invention, a plurality of waste hydrogenation catalysts are filled in layers, the equivalent diameter of the waste hydrogenation catalysts is gradually reduced along the material flow direction, the pore diameter is gradually reduced, and the active metal content is gradually increased.
In one embodiment of the invention, the impurity removal reactor is also filled with a dechlorinating agent, and the filling volume ratio of the dechlorinating agent to the waste catalyst is 1-80: 20 to 99. The waste hydrogenation catalyst and the dechlorinating agent are uniformly mixed and filled or layered filled.
In one embodiment of the invention, the waste hydrogenation catalyst and the dechlorinating agent are filled in layers, and the dechlorinating agent is filled downstream of the waste hydrogenation catalyst according to the material flow direction.
In one embodiment of the present invention, the dechlorinating agent is one or more, and when the dechlorinating agent is a plurality of dechlorinating agents, the dechlorinating agents can be packed in a graded combination or a mixed packing.
In one embodiment of the invention, the hydrogenation reactor is at least one moving bed hydrogenation reactor, and the waste hydrogenation catalyst and the dechlorinating agent are filled in the moving bed hydrogenation reactor. The waste hydrogenation catalyst and the dechlorinating agent are mechanically mixed according to a certain proportion.
In one embodiment of the invention, the dechlorinating agent comprises at least one group IA metal compound and/or at least one group IIA metal compound, optionally one or more metal oxides selected from Cu, fe, zn, and a carrier and/or binder;
the carrier and/or the binder is selected from one or more of silicon oxide, aluminum oxide, silicon oxide-aluminum oxide, zirconium oxide and clay. The clay is one or more selected from kaolin, illite, montmorillonite and bentonite; the kaolin comprises halloysite.
In the invention, the optional one or more metal oxides selected from Cu, fe and Zn refer to one or more metal oxides selected from Cu, fe and Zn as optional components of the dechlorinating agent.
In the present invention, the dechlorinating agent is preferably a high-temperature dechlorinating agent and/or a medium-temperature dechlorinating agent. The invention has no limitation to high-temperature dechlorinating agent and medium-temperature dechlorinating agent, and the invention can be realized by conventional high-temperature dechlorinating agent and medium-temperature dechlorinating agent. Further preferred are high temperature dechlorinating agents and/or medium temperature dechlorinating agents having a large chlorine capacity.
In one embodiment of the invention, the stripping reaction conditions are: hydrogen partial pressure of 0.5-20.0 MPa, reaction temperature of 60-450 ℃ and volume space velocity of 0.1-30 h -1 Hydrogen oil volume ratio of 5-1000 Nm 3 /m 3 。
The preferred conditions for the stripping reaction are: hydrogen partial pressure of 1-12 MPa, reaction temperature of 100-400 ℃ and volume space velocity of 0.2-20 h -1 Hydrogen oil volume ratio of 10-800 Nm 3 /m 3 。
In the invention, after the gas-liquid separation of the reaction effluent obtained from the impurity removal reactor, a first gas-phase material and a first liquid-phase material are obtained, wherein the silicon content of the obtained first liquid-phase material is less than 1 mug/g, the metal content is less than 5 mug/g, and the chlorine content is less than 0.5 mug/g.
Fractionating the obtained first liquid phase material to obtain a first fraction, a second fraction and a third fraction, wherein the first fraction is C 5 And a hydrocarbon fraction of C 6 ～C 8 A hydrocarbon fraction of the hydrocarbon fraction,the third fraction is C 9 The above hydrocarbon fraction.
In the hydrofining unit of step (2) of the present invention, the second fraction obtained in the impurity removal unit of step (1), namely C 6 ～C 8 The hydrocarbon fraction enters a hydrofining reactor and contacts with a hydrofining catalyst under the condition of hydrofining reaction to carry out the reactions of hydrodesulfurization, hydrodenitrogenation, olefin hydrogenation saturation and the like.
In one embodiment of the present invention, the hydrofinishing reaction conditions are: hydrogen partial pressure of 0.5-20.0 MPa, reaction temperature of 60-450 ℃ and volume space velocity of 0.1-30 h -1 Hydrogen oil volume ratio of 5-1000 Nm 3 /m 3 ；
The preferred hydrofining reaction conditions are: hydrogen partial pressure of 1.0-12.0 MPa, reaction temperature of 100-420 ℃ and volume space velocity of 0.2-20 h -1 Hydrogen oil volume ratio of 10-800 Nm 3 /m 3 。
In one embodiment of the invention, the hydrofining catalyst comprises a hydrogenation metal active component and a carrier, wherein the content of the hydrogenation metal active component is 5-50 wt% based on the total weight of the hydrofining catalyst and calculated as oxide.
In a preferred case, the hydrogenation metal active component is at least one metal element selected from the group consisting of group VIB metal elements and at least one metal element selected from the group consisting of group VIII metal elements, wherein the group VIB metal elements are molybdenum and/or tungsten, and the group VIII metal elements are cobalt and/or nickel; the content of the group VIB metal element is 4 to 40 wt%, preferably 8 to 35 wt%, and the content of the group VIII metal element is 1 to 10 wt%, preferably 2 to 5 wt%, based on the total weight of the hydrofining catalyst, calculated as oxide.
And separating the reaction effluent obtained by the hydrofining reactor to obtain a second gas-phase material and a second liquid-phase material. In one embodiment of the invention, the obtained second liquid phase material has 20-90 mass% of aromatic hydrocarbon content, sulfur content <1 mug/g, nitrogen content <1 mug/g, silicon content <1 mug/g, chlorine content < 0.5 mug/g, total metal content <1 mug/g and bromine valence < 0.5gBr/100g, and is a high-quality aromatic hydrocarbon extraction raw material.
In one embodiment of the invention, the third fraction obtained in step (1) enters a catalytic cracking unit, contacts a catalytic cracking catalyst, and reacts under catalytic cracking reaction conditions.
In a preferred aspect, the catalytic cracking unit is aimed at producing high yields of lower olefins and aromatic hydrocarbon products.
In one embodiment of the present invention, the catalytic cracking unit is selected from one or more of DCC, CPP, HCC catalytic cracking process technologies.
In one embodiment of the invention, the reaction temperature of the catalytic cracking unit is 500-850 ℃, and the weight ratio of the catalyst to the oil is (1-50): 1, the mass ratio of water to oil is (0.01-1): 1, and the reaction pressure is 0.1-2 MPa.
In one embodiment of the present invention, the catalytic cracking catalyst is one or more of a metal oxide type catalytic cracking catalyst and a zeolite type catalytic cracking catalyst.
In one embodiment of the invention, the zeolite-type catalytic cracking catalyst comprises the following components: the zeolite-type catalytic cracking catalyst comprises 1 to 50 wt% zeolite, 5 to 99 wt% inorganic oxide, and 0 to 70 wt% clay, based on the dry weight of the zeolite-type catalytic cracking catalyst.
In a preferred case, the zeolite comprises 50 to 100 wt% of a large pore zeolite comprising at least one selected from REY, REHY, USY and high silicon Y and 0 to 50 wt% of a medium pore zeolite comprising ZSM-series zeolite and/or ZRP zeolite based on the dry weight of the zeolite; the inorganic oxide comprises silicon oxide and/or aluminum oxide; the clay comprises kaolin and/or halloysite.
In one embodiment of the invention, the feed to the catalytic cracking unit comprises an optional catalytic cracking feedstock that is a petroleum hydrocarbon oil selected from at least one of vacuum wax oil, coker wax oil, deasphalted oil, residuum, gasoline, and diesel oil, and/or a mineral oil selected from at least one of coal liquefaction oil, oil sand, and shale oil.
In one embodiment of the present invention, the metal oxide type catalytic cracking catalyst contains alumina and/or aluminosilicate, and one or more metal oxides selected from alkali metal oxides, alkaline earth metal oxides, and group VIII metal oxides.
In a preferred case, the aluminosilicate is selected from the group consisting of silica-alumina, amorphous aluminum silicate, molecular sieves.
Preferably, the metal oxide is selected from one or more of K, na, ca, fe, co, ni, mo oxides.
In one embodiment of the invention, the reaction effluent of the catalytic cracking unit is separated to obtain a catalytic cracking catalyst and a catalytic cracking product, and the catalytic cracking product is further separated to obtain low-carbon olefin comprising ethylene, propylene and butylene, a catalytic cracking gasoline fraction, a catalytic cracking diesel fraction and slurry oil; wherein the distillation range of the catalytic pyrolysis gasoline fraction is 30-180 ℃.
In one embodiment of the invention, the catalytically cracked gasoline fraction obtained from the catalytic cracking unit is recycled to the inlet of the hydrofining unit; the hydrofining reaction product is subjected to gas-liquid separation, and the obtained liquid phase material is subjected to fractionation to obtain a second liquid phase material meeting the feeding requirement of aromatic hydrocarbon, wherein the content of aromatic hydrocarbon in the second liquid phase material is 20-90 mass%, the content of sulfur is less than 1 mug/g, the content of nitrogen is less than 1 mug/g, the content of silicon is less than 1 mug/g, the content of chlorine is less than 0.5 mug/g, the total metal content is less than 1 mug/g, the bromine valence is less than 0.5gBr/100g, and the second liquid phase material is a high-quality aromatic hydrocarbon extraction raw material.
In another aspect, the invention provides a system for any of the above methods, comprising a depuration unit, a hydrofining unit;
the impurity removal unit is provided with an impurity removal reactor filled with waste hydrogenation catalyst, the impurity removal reactor is provided with at least one waste plastic oil and/or waste tire oil inlet, at least one first fraction outlet, at least one second fraction outlet and at least one third fraction outlet, and the waste hydrogenation catalyst is one or more selected from a protective agent used from any fixed bed hydrogenation process device to the end in the hydrocarbon oil processing field, a catalyst at the end and a regenerated protective agent and a regenerated catalyst;
the hydrofining unit is provided with a hydrofining reactor filled with hydrofining catalyst, the hydrofining unit is provided with a feeding inlet, at least one second gas-phase material outlet and at least one second liquid-phase material outlet, and a second fraction outlet of the impurity removing unit is communicated with the feeding inlet of the hydrofining unit.
In one embodiment of the invention, the system further comprises a catalytic cracking unit, wherein a feeding inlet of the catalytic cracking unit is communicated with a third fraction outlet of the impurity removal unit, and the catalytic cracking unit is provided with at least one low-carbon olefin outlet and at least one catalytic cracking gasoline fraction outlet; the catalytic pyrolysis gasoline fraction outlet is communicated with the feed inlet of the hydrofining unit.
In one embodiment of the invention, the de-hybridization reactor is at least one fixed bed hydrogenation reactor and/or at least one moving bed hydrogenation reactor.
In one embodiment of the invention, the impurity removal reactor is more than two fixed bed hydrogenation reactors connected in parallel, each fixed bed hydrogenation reactor is filled with waste hydrogenation catalyst, and each fixed bed hydrogenation reactor is provided with at least one feed inlet and at least one reaction effluent outlet.
The invention is characterized in that:
1. the invention can treat waste plastic oil and waste tyre oil converted by various processes, and provides high-quality aromatic hydrocarbon extraction raw materials for the aromatic hydrocarbon extraction process after the waste plastic oil and the waste tyre oil are treated by the impurity removal unit and the hydrofining unit and are organically combined with the catalytic cracking unit.
2. The invention effectively removes impurities, especially silicon impurities, chlorine impurities and metal impurities, in the waste plastic oil and the waste tire oil in the impurity removal unit, avoids the influence of the impurities on the hydrofining catalyst in the hydrofining unit, and prolongs the whole operation period.
3. The invention uses the waste hydrogenation catalyst, and has low cost and good impurity removal effect. In the preferred embodiment of the invention, a moving bed or two fixed bed reactors which are connected in parallel and alternately switched are adopted for pretreatment, so that the purposes of long-period deep desilication, demetallization and dechlorination are realized.
Drawings
FIG. 1 is a schematic diagram of one embodiment of the process for producing an aromatic extraction feedstock from waste plastic oil and/or scrap tire oil provided by the present invention.
Detailed Description
The invention will be further described with reference to the accompanying drawings, without thereby limiting the invention.
FIG. 1 is a schematic diagram of one embodiment of a method for producing an aromatic hydrocarbon extraction raw material from waste plastic oil and/or waste tire oil, wherein the method is shown in FIG. 1, after the waste plastic oil and/or waste tire oil from a pipeline 1 is boosted by a feed pump 2, the waste plastic oil and/or waste tire oil enters a heating furnace 4 from a pipeline 3 together with new hydrogen from a pipeline 17 and circulating hydrogen from a pipeline 16 to be heated, the heated hydrogen-mixed material enters a impurity removal unit through a pipeline 5, the impurity removal unit is provided with two parallel fixed bed hydrogenation reactors 8 and 9, a catalyst bed layer A is arranged in the fixed bed hydrogenation reactor 8, waste hydrogenation catalyst is filled in a grading manner, a catalyst bed layer B is arranged in the fixed bed hydrogenation reactor 9, and waste hydrogenation catalyst is filled in a grading manner. In one embodiment, the hydrogen mixed material enters a fixed bed hydrogenation reactor 8 through a pipeline 6, contacts with the waste hydrogenation catalyst filled in a grading way, and carries out the impurity removal reaction under the impurity removal reaction condition, and the fixed bed hydrogenation reactor 9 is used for standby. After the waste hydrogenation catalyst in the fixed bed hydrogenation reactor 8 is saturated with silicon or metal, the hydrogen mixed material enters the fixed bed hydrogenation reactor 9 through a pipeline 7 to react, the fixed bed hydrogenation reactor 8 is cut out of the reaction system, and then the waste hydrogenation catalyst in the catalyst bed A is replaced. The reaction effluent obtained by the impurity removal unit enters a high-pressure separator 12 through pipelines 10 and 11 for gas-liquid separation, the obtained first liquid phase material enters a fractionating tower 18 through a pipeline 14, and a first fraction, a second fraction and a third fraction are obtained after cutting and are respectively extracted through pipelines 19, 20 and 21; the resulting first gaseous material is fed via line 13 to recycle hydrogen compressor 15 for pressurization and then recycled via line 16 to the inlet of furnace 4.
The second fraction from line 20 and the catalytically cracked gasoline fraction from line 24 are mixed with fresh hydrogen from line 25 and recycle hydrogen from line 33, heated in furnace 26, and then enter hydrofining reactor 27 to contact hydrofining catalyst for reaction, the reaction effluent enters high pressure separator 29 via line 28 for gas-liquid separation, the second liquid phase material is withdrawn via line 30, and the second gas phase material is returned to the inlet of furnace 26 via line 33 after being boosted in recycle hydrogen compressor 32.
The third fraction from the pipeline 21 enters a catalytic cracking unit 22 to carry out catalytic cracking reaction, contacts with a catalytic cracking catalyst to carry out reaction under the condition of catalytic cracking reaction, and after the reaction effluent is separated, the obtained catalytic cracking gasoline fraction is sent to an inlet of a hydrofining unit through a pipeline 24; the catalytically cracked heavy fraction is withdrawn via line 23.
The invention is further illustrated by the following examples, which are not intended to limit the invention in any way.
In the examples, the silicon content in the hydrocarbon material was measured by the method of measuring single wavelength dispersive X-ray fluorescence (SH/T0993-2019) of the silicon content in gasoline and related products in the examples.
In the examples, the chlorine content in the liquid material was measured by coulometry, specifically by the method of "measuring the total chlorine content in crude oil by coulometry" (RIPP 64-90) in "petrochemical analysis method" (RIPP test method). The instrument used was a microcoulomb analyzer and the sample was a liquid material.
The dechlorinating agent used in the examples was an industrially practiced dechlorinating agent RDY-100, manufactured by Jinan Ruidong Utility Co.
The reforming prehydrogenation end catalyst D used in the examples was alumina, butterfly-shaped with equivalent diameter of 1.6mm and active composition comprising: 18% by weight of tungsten oxide, 2% by weight of nickel oxide, 0.04% by weight of cobalt oxide, 5.0% by weight of carbon and 6% by weight of sulfur;
the catalyst E used in the examples at the end of the hydrogenation of gasoline has the following active composition: molybdenum oxide to 10 weight percent, cobalt oxide to 3.5 weight percent, carbon to 8.0 weight percent and sulfur to 7.0 weight percent;
the end catalyst F for diesel hydrofining used in the examples has the carrier of alumina, butterfly shape and equivalent diameter of 1.6mm, and the active composition comprises: molybdenum oxide to 26 weight percent, nickel oxide to 4.0 weight percent, carbon to 20 weight percent and sulfur to 15 weight percent;
the end hydrogenation catalyst G used in the examples is a residuum hydrogenation protecting agent end catalyst, the carrier is alumina, raschig rings, equivalent diameter 6.0mm, the active composition includes: molybdenum oxide to 2 weight percent, nickel oxide to 0.5 weight percent, carbon to 40 weight percent and sulfur to 5 weight percent.
The hydrofining catalyst H used in the examples has the following active metal composition, wherein the carrier is alumina and clover with equivalent diameter of 1.6 mm: tungsten oxide to 19 weight percent, nickel oxide to 2.0 weight percent and cobalt oxide to 0.4 weight percent.
The properties of the raw materials are shown in Table 1, wherein the raw material I is a mixed raw material of waste plastic oil and waste tire oil, and the mixing ratio is 40:60 weight, J is scrap tire oil.
Examples 1 to 3
Waste plastic oil and/or waste tire oil raw materials enter a impurity removal reactor to contact with a waste hydrogenation catalyst in the presence of hydrogen, impurity removal reaction is carried out under impurity removal reaction conditions, obtained reaction effluent is separated to obtain a first gas-phase material and a first liquid-phase material, and the obtained first liquid-phase material is further separated to obtain a first fraction (C1-C5), a second fraction (C6-C8) and a third fraction (C9+).
The second fraction enters a hydrofining reactor to contact with a hydrofining catalyst, hydrofining reaction is carried out under the condition of hydrofining reaction, and a second gas-phase material and a second liquid-phase material are obtained after the reaction effluent is separated. The specific reaction conditions and product properties are shown in Table 2.
As shown in Table 2, the obtained second liquid phase material has low sulfur, low nitrogen and low bromine value, and is a high-quality aromatic hydrocarbon extraction raw material.
Examples 4 to 5
Waste plastic oil and/or waste tire oil raw materials enter a impurity removal reactor to contact with a waste hydrogenation catalyst in the presence of hydrogen, impurity removal reaction is carried out under impurity removal reaction conditions, obtained reaction effluent is separated to obtain a first gas-phase material and a first liquid-phase material, and the obtained first liquid-phase material is further separated to obtain a first fraction (C1-C5), a second fraction (C6-C8) and a third fraction (C9+).
The obtained second fraction enters a hydrofining reactor to contact with a hydrofining catalyst, hydrofining reaction is carried out under the condition of hydrofining reaction, and a second gas-phase material and a second liquid-phase material are obtained after the reaction effluent is separated. The specific reaction conditions and product properties are shown in Table 3.
The third fraction enters a catalytic cracking unit to react with a catalytic cracking catalyst, the reaction effluent is separated to obtain a product comprising low-carbon olefin and a catalytic cracking gasoline fraction, and the obtained catalytic cracking gasoline fraction is recycled to the inlet of the hydrofining reactor to react with the second fraction. The catalytic cracking catalyst is CRP and is produced by China petrochemical catalyst division. The catalytic cracking reaction temperature is 550 ℃, the reaction pressure is 0.11MPa, the catalyst-oil mass ratio is 9.0, the water-oil mass ratio is 0.2, and the airspeed is 4h -1 The catalyst regeneration temperature was 715 ℃.
As shown in Table 3, the obtained second liquid phase material has low sulfur, low nitrogen and low bromine value, and is a high-quality aromatic hydrocarbon extraction raw material.
TABLE 1
TABLE 2
TABLE 3 Table 3
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Example 6
In this example, two parallel fixed bed hydrogenation reactors 1 and 2 were set up, and the feedstock I was used as feed, and the catalyst loading conditions, the impurity removal reaction conditions and the reaction results were as shown in Table 4.
When the reactor 1 is operated for 2500 hours, the silicon content of the liquid phase material in the reaction effluent is more than 1 mug/g, and the reactor 2 is switched to carry out impurity removal reaction, and the silicon content of the liquid phase material is reduced to be less than 1 mug/g. The catalyst is replaced for the reactor 1, and thus the cycle achieves a long period of operation.
TABLE 4 Table 4
Example 7
The stripping unit in this example employs a moving bed reactor fed with feedstock J, catalyst loading conditions, stripping reaction conditions and reaction results are set forth in Table 5.
As can be seen from Table 5, by adopting the method of the present invention, the raw material J with higher impurity content is treated by adopting a moving bed in the impurity removal unit, the silicon content of the obtained first liquid phase material is less than 1 mug/g, the chlorine content is less than 0.5 mug/g, the metal content is less than 5 mug/g, and the dosage consumption is 3.2 kg/ton of oil.
TABLE 5
It should be noted that the above-mentioned embodiments of the present invention are merely examples, and are not intended to limit the present invention, and various modifications and variations of the present invention will be apparent to those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (23)
1. A method for producing aromatic hydrocarbon extraction raw materials from waste plastic oil and/or junked tire oil comprises the following steps:
(1) The waste plastic oil and/or the waste tire oil raw materials enter a impurity removal reactor to be contacted with a waste hydrogenation catalyst in the presence of hydrogen, impurity removal reaction is carried out under impurity removal reaction conditions, and after gas-liquid separation is carried out on obtained reaction effluent, a first gas-phase material and a first liquid-phase material are obtained, wherein the silicon content of the obtained first liquid-phase material is less than 1 mug/g, and the metal content of the obtained first liquid-phase material is less than 5 mug/g; the waste hydrogenation catalyst is a protective agent and a catalyst which are selected from the end of any fixed bed hydrogenation process device in the hydrocarbon oil processing field, wherein the waste hydrogenation catalyst comprises 0-50% by weight of hydrogenation active metal oxide, 5-50% by weight of carbon and 6-40% by weight of sulfur based on the total weight of the waste hydrogenation catalyst, and the hydrogenation active metal is selected from one or more of VIII group metal and VIB group metal; the impurity removal reaction conditions are as follows: hydrogen partial pressure of 0.5-20.0 MPa, reaction temperature of 60-450 ℃ and volume space velocity of 0.1-30 h -1 Hydrogen oil volume ratio of 5-1000 Nm 3 /m 3 ；
Fractionating the obtained first liquid phase material to obtain a first fraction, a second fraction and a third fraction, wherein the first fraction is C 5 And a hydrocarbon fraction of C 6 ～C 8 A hydrocarbon fraction, the third fraction being C 9 The above hydrocarbon fractions;
(2) A hydrofining unit, wherein the second fraction obtained in the step (1) enters a hydrofining reactor, contacts with a hydrofining catalyst in the presence of hydrogen, and performs hydrofining reaction under the condition of hydrofining reaction; and (3) carrying out gas-liquid separation on the obtained reaction effluent to obtain a second gas-phase material and a second liquid-phase material, wherein the obtained second liquid-phase material is an aromatic hydrocarbon extraction raw material.
2. The method according to claim 1, comprising the step (3):
(3) The third fraction obtained in the step (1) enters a catalytic cracking unit, contacts with a catalytic cracking catalyst, reacts under the catalytic cracking reaction condition, and at least low-carbon olefin and catalytic cracking gasoline fraction are obtained after the reaction effluent is separated;
the obtained catalytic pyrolysis gasoline fraction is sent to a hydrofining unit in the step (2) to enter a hydrofining reactor.
3. The method according to claim 1 or 2, wherein the waste plastic oil is a hydrocarbon material obtained by one or more conversion methods of thermal cracking, catalytic cracking, and dissolution liquefaction of waste plastic; the distillation range of the waste plastic oil is 30-700 ℃, the silicon content is less than 10000 mug/g, the chlorine content is less than 10000 mug/g, and the metal content is less than 10000 mug/g.
4. A method according to claim 3, wherein the waste plastics are one or more of fresh household garbage, industrial and agricultural production and aged garbage, and the waste plastics are one or more selected from PE, PP, PS, PVC.
5. The method according to claim 1 or 2, wherein the junked tire oil is a hydrocarbon material obtained by one or more conversion methods of thermal cracking, catalytic cracking, and dissolution liquefaction of junked tires; the distillation range of the waste tire oil is 30-700 ℃, the silicon content is less than 10000 mug/g, the chlorine content is less than 10000 mug/g, and the metal content is less than 10000 mug/g.
6. The method according to claim 5, wherein the scrap tires are various scrap tires made of natural rubber and/or synthetic rubber.
7. The process according to claim 1, characterized in that the de-hybridization reactor is at least one fixed bed hydrogenation reactor and/or at least one moving bed hydrogenation reactor.
8. The method according to claim 1, wherein the impurity removal reactor is more than two fixed bed hydrogenation reactors connected in parallel, each reactor is filled with a waste hydrogenation catalyst, the feed is subjected to impurity removal reaction through at least one fixed bed hydrogenation reactor, and when the waste hydrogenation catalyst in the fixed bed hydrogenation reactor is saturated with silicon or saturated with metal, the feed is switched to other fixed bed hydrogenation reactors.
9. The method of claim 8, wherein the waste hydrogenation catalyst in the de-hybridization reactor is considered to be saturated with silicon or saturated with metal when the silicon content of the first liquid phase feed is 1 μg/g or greater or when the metal content is 5 μg/g or greater.
10. The method according to claim 1, wherein the equivalent diameter of the spent hydrogenation catalyst is 0.5-16 mm.
11. The method according to claim 1, wherein the waste hydrogenation catalyst comprises, based on the total weight of the waste hydrogenation catalyst, 0-50 wt% of molybdenum oxide and/or tungsten oxide, 0-40 wt% of nickel oxide and/or cobalt oxide, 5-30 wt% of carbon, and 6-30 wt% of sulfur.
12. The method according to claim 1, wherein the waste hydrogenation catalyst comprises 1-40 wt% of hydrogenation active metal oxide and 5-20 wt% of carbon based on the total weight of the waste hydrogenation catalyst, and the hydrogenation active metal is selected from one or more of group VIII metal and group VIB metal.
13. The method according to claim 1, wherein the impurity removal reactor is further filled with a dechlorinating agent, and the filling volume ratio of the dechlorinating agent to the waste catalyst is 1-80: 20 to 99.
14. The method according to claim 13, wherein the dechlorinating agent comprises at least one group IA metal compound and/or at least one group IIA metal compound, optionally one or several metal oxides selected from Cu, fe, zn, and a carrier and/or a binder;
the carrier and/or the binder is selected from one or more of silicon oxide, aluminum oxide, silicon oxide-aluminum oxide, zirconium oxide and clay.
15. The process according to claim 1 or 13, wherein the chlorine content of the first liquid phase material of step (1) is less than 0.5 μg/g.
16. The method according to claim 1, wherein the stripping reaction conditions are: hydrogen partial pressure of 1-12 MPa, reaction temperature of 100-400 ℃ and volume space velocity of 0.2-20 h -1 Hydrogen oil volume ratio of 10-800 Nm 3 /m 3 。
17. The process of claim 1, wherein the hydrofinishing catalyst of step (2) comprises a hydrofinishing metal active component and a support, the hydrofinishing metal active component being present in an amount of from 5 to 50 wt% on an oxide basis based on the total weight of the hydrofinishing catalyst.
18. The process according to claim 17, characterized in that the hydrogenating metal active component is at least one metal element selected from the group consisting of group VIB metal elements and at least one metal element selected from the group VIII metal elements, the group VIB metal elements being molybdenum and/or tungsten and the group VIII metal elements being cobalt and/or nickel; the total weight of the hydrofining catalyst is taken as a reference, the content of the metal element of the VIB group is 4-40 wt% and the content of the metal element of the VIII group is 1-10 wt% based on oxide.
19. The process of claim 18 wherein the group VIB metal element is present in an amount of 8 to 35 wt.% and the group VIII metal element is present in an amount of 2 to 5 wt.% on an oxide basis based on the total weight of the hydrofinishing catalyst.
20. The process of claim 1, wherein the hydrofinishing reaction conditions of step (2) are: hydrogen partial pressure of 0.5-20.0 MPa, reaction temperature of 60-450 ℃ and volume space velocity of 0.1-30 h -1 Hydrogen oil volume ratio of 5-1000 Nm 3 /m 3 。
21. The method of claim 20, wherein the hydrofinishing reaction conditions are: hydrogen partial pressure of 1.0-12.0 MPa, reaction temperature of 100-420 ℃ and volume space velocity of 0.2-20 h -1 Hydrogen oil volume ratio of 10-800 Nm 3 /m 3 。
22. The process according to claim 1, wherein the second liquid-phase material obtained in the step (2) has an aromatic hydrocarbon content of 20 to 90 mass%, a sulfur content of < 1. Mu.g/g, a nitrogen content of < 1. Mu.g/g, a silicon content of < 1. Mu.g/g, a chlorine content of < 0.5. Mu.g/g, a total metal content of < 1. Mu.g/g, and a bromine number of < 0.5gBr/100g, and is an aromatic hydrocarbon extraction raw material.
23. The process according to claim 2, wherein the reaction conditions of the catalytic cracking unit are: the reaction temperature is 500-850 ℃, and the weight ratio of the catalyst to the oil is (1-50): 1, the mass ratio of water to oil is (0.01-1), 1, and the reaction pressure is 0.1-2 MPa; the catalytic cracking catalyst is one or more of metal oxide type catalytic cracking catalyst and zeolite type catalytic cracking catalyst.
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