CN116396775A - Equipment and method for preparing finished oil from waste oil - Google Patents
Equipment and method for preparing finished oil from waste oil Download PDFInfo
- Publication number
- CN116396775A CN116396775A CN202310498182.9A CN202310498182A CN116396775A CN 116396775 A CN116396775 A CN 116396775A CN 202310498182 A CN202310498182 A CN 202310498182A CN 116396775 A CN116396775 A CN 116396775A
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- oil
- tank
- condenser
- heater
- waste oil
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- 239000002699 waste material Substances 0.000 title claims abstract description 97
- 238000000034 method Methods 0.000 title claims abstract description 41
- 238000004821 distillation Methods 0.000 claims abstract description 52
- 238000006243 chemical reaction Methods 0.000 claims abstract description 45
- 239000004576 sand Substances 0.000 claims abstract description 21
- 230000003197 catalytic effect Effects 0.000 claims abstract description 13
- 238000011282 treatment Methods 0.000 claims abstract description 13
- 239000003921 oil Substances 0.000 claims description 209
- 150000002430 hydrocarbons Chemical class 0.000 claims description 62
- 229930195733 hydrocarbon Natural products 0.000 claims description 61
- 239000004215 Carbon black (E152) Substances 0.000 claims description 58
- 238000010438 heat treatment Methods 0.000 claims description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 47
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 36
- 239000010779 crude oil Substances 0.000 claims description 36
- 239000003502 gasoline Substances 0.000 claims description 27
- 238000003860 storage Methods 0.000 claims description 24
- 238000001704 evaporation Methods 0.000 claims description 11
- 238000005194 fractionation Methods 0.000 claims description 11
- 239000003054 catalyst Substances 0.000 claims description 10
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 8
- 238000004523 catalytic cracking Methods 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 6
- 239000010913 used oil Substances 0.000 claims description 5
- 239000008394 flocculating agent Substances 0.000 claims description 4
- 238000005189 flocculation Methods 0.000 claims description 4
- 230000016615 flocculation Effects 0.000 claims description 4
- 239000001488 sodium phosphate Substances 0.000 claims description 4
- RYFMWSXOAZQYPI-UHFFFAOYSA-K trisodium phosphate Chemical compound [Na+].[Na+].[Na+].[O-]P([O-])([O-])=O RYFMWSXOAZQYPI-UHFFFAOYSA-K 0.000 claims description 4
- 229910000406 trisodium phosphate Inorganic materials 0.000 claims description 4
- 235000019801 trisodium phosphate Nutrition 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 2
- 238000000638 solvent extraction Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 claims 1
- 238000002360 preparation method Methods 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 abstract description 2
- 230000009897 systematic effect Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 28
- 239000002283 diesel fuel Substances 0.000 description 25
- 230000000052 comparative effect Effects 0.000 description 15
- 238000011084 recovery Methods 0.000 description 13
- 239000000047 product Substances 0.000 description 11
- 150000007524 organic acids Chemical class 0.000 description 10
- 239000012141 concentrate Substances 0.000 description 8
- 239000007921 spray Substances 0.000 description 8
- 238000009833 condensation Methods 0.000 description 7
- 230000005494 condensation Effects 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 239000000872 buffer Substances 0.000 description 6
- 239000012535 impurity Substances 0.000 description 6
- 239000011555 saturated liquid Substances 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 238000001514 detection method Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- 229920006395 saturated elastomer Polymers 0.000 description 5
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 239000000654 additive Substances 0.000 description 4
- 230000000996 additive effect Effects 0.000 description 4
- 238000004040 coloring Methods 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- WMFOQBRAJBCJND-UHFFFAOYSA-M Lithium hydroxide Chemical compound [Li+].[OH-] WMFOQBRAJBCJND-UHFFFAOYSA-M 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 3
- 238000006303 photolysis reaction Methods 0.000 description 3
- 230000015843 photosynthesis, light reaction Effects 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 239000002199 base oil Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 150000003839 salts Chemical group 0.000 description 2
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 2
- 235000017557 sodium bicarbonate Nutrition 0.000 description 2
- 239000011949 solid catalyst Substances 0.000 description 2
- IVORCBKUUYGUOL-UHFFFAOYSA-N 1-ethynyl-2,4-dimethoxybenzene Chemical compound COC1=CC=C(C#C)C(OC)=C1 IVORCBKUUYGUOL-UHFFFAOYSA-N 0.000 description 1
- HNNQYHFROJDYHQ-UHFFFAOYSA-N 3-(4-ethylcyclohexyl)propanoic acid 3-(3-ethylcyclopentyl)propanoic acid Chemical compound CCC1CCC(CCC(O)=O)C1.CCC1CCC(CCC(O)=O)CC1 HNNQYHFROJDYHQ-UHFFFAOYSA-N 0.000 description 1
- WUPHOULIZUERAE-UHFFFAOYSA-N 3-(oxolan-2-yl)propanoic acid Chemical compound OC(=O)CCC1CCCO1 WUPHOULIZUERAE-UHFFFAOYSA-N 0.000 description 1
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- 229910021503 Cobalt(II) hydroxide Inorganic materials 0.000 description 1
- JJLJMEJHUUYSSY-UHFFFAOYSA-L Copper hydroxide Chemical compound [OH-].[OH-].[Cu+2] JJLJMEJHUUYSSY-UHFFFAOYSA-L 0.000 description 1
- 239000005750 Copper hydroxide Substances 0.000 description 1
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 1
- 239000005083 Zinc sulfide Substances 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- 229910000323 aluminium silicate Inorganic materials 0.000 description 1
- 239000000908 ammonium hydroxide Substances 0.000 description 1
- 239000010426 asphalt Substances 0.000 description 1
- 208000027697 autoimmune lymphoproliferative syndrome due to CTLA4 haploinsuffiency Diseases 0.000 description 1
- RQPZNWPYLFFXCP-UHFFFAOYSA-L barium dihydroxide Chemical compound [OH-].[OH-].[Ba+2] RQPZNWPYLFFXCP-UHFFFAOYSA-L 0.000 description 1
- 229910001863 barium hydroxide Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052980 cadmium sulfide Inorganic materials 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- VQWFNAGFNGABOH-UHFFFAOYSA-K chromium(iii) hydroxide Chemical compound [OH-].[OH-].[OH-].[Cr+3] VQWFNAGFNGABOH-UHFFFAOYSA-K 0.000 description 1
- ASKVAEGIVYSGNY-UHFFFAOYSA-L cobalt(ii) hydroxide Chemical compound [OH-].[OH-].[Co+2] ASKVAEGIVYSGNY-UHFFFAOYSA-L 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 229910001956 copper hydroxide Inorganic materials 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 150000004691 decahydrates Chemical class 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 150000004665 fatty acids Chemical class 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000003311 flocculating effect Effects 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 150000004688 heptahydrates Chemical class 0.000 description 1
- 229910052741 iridium Inorganic materials 0.000 description 1
- GKOZUEZYRPOHIO-UHFFFAOYSA-N iridium atom Chemical compound [Ir] GKOZUEZYRPOHIO-UHFFFAOYSA-N 0.000 description 1
- 235000014413 iron hydroxide Nutrition 0.000 description 1
- NCNCGGDMXMBVIA-UHFFFAOYSA-L iron(ii) hydroxide Chemical compound [OH-].[OH-].[Fe+2] NCNCGGDMXMBVIA-UHFFFAOYSA-L 0.000 description 1
- 229910021514 lead(II) hydroxide Inorganic materials 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000004682 monohydrates Chemical class 0.000 description 1
- 239000010705 motor oil Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- BFDHFSHZJLFAMC-UHFFFAOYSA-L nickel(ii) hydroxide Chemical compound [OH-].[OH-].[Ni+2] BFDHFSHZJLFAMC-UHFFFAOYSA-L 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 229910052762 osmium Inorganic materials 0.000 description 1
- SYQBFIAQOQZEGI-UHFFFAOYSA-N osmium atom Chemical compound [Os] SYQBFIAQOQZEGI-UHFFFAOYSA-N 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- IYDGMDWEHDFVQI-UHFFFAOYSA-N phosphoric acid;trioxotungsten Chemical compound O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.OP(O)(O)=O IYDGMDWEHDFVQI-UHFFFAOYSA-N 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 239000011736 potassium bicarbonate Substances 0.000 description 1
- 229910000028 potassium bicarbonate Inorganic materials 0.000 description 1
- 235000015497 potassium bicarbonate Nutrition 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 235000011181 potassium carbonates Nutrition 0.000 description 1
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 description 1
- CHWRSCGUEQEHOH-UHFFFAOYSA-N potassium oxide Chemical compound [O-2].[K+].[K+] CHWRSCGUEQEHOH-UHFFFAOYSA-N 0.000 description 1
- 229910001950 potassium oxide Inorganic materials 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 239000010948 rhodium Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000000344 soap Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
- 229910001948 sodium oxide Inorganic materials 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
- UGZADUVQMDAIAO-UHFFFAOYSA-L zinc hydroxide Chemical compound [OH-].[OH-].[Zn+2] UGZADUVQMDAIAO-UHFFFAOYSA-L 0.000 description 1
- 229910021511 zinc hydroxide Inorganic materials 0.000 description 1
- 229940007718 zinc hydroxide Drugs 0.000 description 1
- 229910052984 zinc sulfide Inorganic materials 0.000 description 1
- DRDVZXDWVBGGMH-UHFFFAOYSA-N zinc;sulfide Chemical compound [S-2].[Zn+2] DRDVZXDWVBGGMH-UHFFFAOYSA-N 0.000 description 1
Images
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
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
-
- 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
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/006—Distillation of hydrocarbon oils of waste oils other than lubricating oils, e.g. PCB's containing 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
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/04—Dewatering
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model relates to a waste oil preparation finished oil's equipment and method relates to waste oil processing technology field, and equipment includes continuous pretreatment tank, preliminary distillation tower, reation kettle, catalytic tower, fractionating tower and decoloration sand jar in proper order, and the preliminary distillation tower is connected in the lower extreme of pretreatment tank, is equipped with the heater on the reation kettle, is equipped with the condenser between fractionating tower and the decoloration sand jar, and the condenser is including communicating in the top condenser at fractionating tower top and communicating in the bottom condenser at fractionating tower bottom. The equipment that this application adopted is orderly connected in proper order, divides the different reactions according to the region in the waste oil treatment process, makes the process of waste oil treatment more systematic and the operation of high efficiency stable.
Description
Technical Field
The application relates to the technical field of waste oil processing, in particular to equipment and a method for preparing finished oil from waste oil.
Background
Waste oil refers to oil contaminated with physical or chemical impurities through use, which is derived from petroleum or synthetic oil, and mainly includes pyrolysis oil and waste engine oil. In the fields of large-scale machines such as automobiles, ships, airplanes, trains and the like, waste oil exceeding tens of millions of tons can be produced annually, so that the huge waste oil not only pollutes the environment, but also wastes valuable resources for recycling. Therefore, the waste oil is refined into the finished oil (the finished oil mainly refers to base oil and diesel oil), so that the problem of environmental pollution can be effectively solved, and the method can be a new way for saving energy and developing recycling economy.
At present, the treatment method of waste oil is mainly to collect, store and then settle, wherein the upper layer is oily substance and the lower layer is insoluble substance after settling, and the oily substance on the upper layer is finished oil; or simply pre-treating the waste oil, and then carrying out flash evaporation and condensation, and obtaining the finished oil after condensation. However, the quality of the oil product produced by the above-mentioned treatment method is poor and the recovery rate is low, and the present application has been made in view of this.
Disclosure of Invention
In order to solve the problems of poor quality and low recovery rate of finished oil in the existing waste oil treatment method, the application provides equipment and a method for preparing the finished oil from the waste oil.
The application adopts the following technical scheme:
in a first aspect, the apparatus for preparing finished oil from waste oil comprises a pretreatment tank, a primary distillation tower, a reaction kettle, a catalytic tower, a fractionating tower and a decolorizing sand tank which are sequentially connected, wherein the primary distillation tower is connected to the lower end of the pretreatment tank, a heater is arranged on the reaction kettle, a condenser is arranged between the fractionating tower and the decolorizing sand tank, and the condenser comprises a top condenser communicated with the top of the fractionating tower and a bottom condenser communicated with the bottom of the fractionating tower.
Optionally, one side of the primary distillation tower is provided with a circulating heater for heating the primary distillation tower, the lower end of the primary distillation tower is connected with a concentrate tank, and the concentrate tank is respectively connected to the circulating heater and the reaction kettle.
Preferably, the top of the primary distillation tower is connected with a light hydrocarbon condenser, the bottom of the light hydrocarbon condenser is connected with an oil-water separator, and the oil-water separator is respectively connected with a light hydrocarbon storage tank and a water tank.
Preferably, the heater comprises an electromagnetic heater and a pipeline heater which are arranged on the reaction kettle.
In a second aspect, a method for preparing a finished oil from used oil comprises: conveying the waste oil into a pretreatment tank for pretreatment;
conveying the pretreated waste oil into a primary distillation tower, and distilling and dehydrating and light hydrocarbon at 160-200 ℃ to prepare crude oil;
crude oil is conveyed to a reaction kettle to be heated to 380-420 ℃ in a partitioning way, and long-chain hydrocarbon components and oil residues are obtained through evaporation;
conveying the long-chain hydrocarbon component into a catalytic tower, and adding a catalyst into the long-chain hydrocarbon component for catalytic cracking to obtain a short-chain hydrocarbon component;
and conveying the short-chain hydrocarbon component to a fractionating tower for fractionation to obtain light component oil and heavy component oil, wherein the light component oil is condensed by a top condenser and then conveyed to a decoloring sand tank for decoloring to obtain gasoline, and the heavy component oil is condensed by a bottom condenser and then conveyed to the decoloring sand tank for decoloring to obtain diesel.
Preferably, the pretreatment comprises: conveying the waste oil into a pretreatment tank and heating to 80-120 ℃;
and adding a flocculating agent into the waste oil in the heating process to perform flocculation deacidification.
Preferably, the flocculant is selected from any one of concentrated sulfuric acid, trisodium phosphate and sodium hydroxide;
further, preferably, the flocculant is a sodium hydroxide solution with a mass of 0.5% -1%.
By adopting the technology, the flocculant can be added to effectively remove the organic acid in the waste oil, so that the quality of the waste oil is improved. The organic acid content in the diesel oil prepared from the deacidified waste oil is very small, and the quality of the diesel oil is improved.
Preferably, the heater comprises an electromagnetic heater and a pipeline heater which are arranged on the reaction kettle;
the step of heating comprises the following steps: firstly, heating the reaction kettle to 350-380 ℃ by using an electromagnetic heater and a pipeline heater;
and then the reaction kettle is heated to 380-420 ℃ by an electromagnetic heater.
By adopting the above technique, there is a difference in distillation ranges between the components due to the complexity of the components in the waste oil. And the components with different distillation ranges can be heated and decomposed respectively by adopting sectional heating, so that the loss of oil is reduced, and the resource is saved.
Preferably, the top of the primary distillation tower is connected with a light hydrocarbon condenser, the bottom of the light hydrocarbon condenser is connected with an oil-water separator, and the oil-water separator is respectively connected with a light hydrocarbon storage tank and a water tank;
the method further comprises the steps of: the removed water and light hydrocarbon enter a light hydrocarbon condenser along the upper end of the primary distillation tower to be cooled into a water-oil mixture;
the water-oil mixture flows into an oil-water separator for separation, wherein water flows into a water tank for storage, and oil flows into a light hydrocarbon storage tank for storage.
Through adopting above-mentioned technique, retrieve light dydrocarbon and the water of desorption, the water and the light dydrocarbon of retrieving can reuse, can reduce the wasting of resources, can realize resource cyclic utilization again, therefore this application prepares the process of finished oil more green.
Preferably, one side of the primary distillation tower is provided with a circulating heater for heating the primary distillation tower, the lower end of the primary distillation tower is connected with a concentrated solution tank, and the concentrated solution tank is respectively connected to the circulating heater and the reaction kettle;
the process of crude oil delivery to the reaction vessel includes: firstly, crude oil is conveyed into a concentrated liquid tank for diversion;
wherein, a part of crude oil flows into the reaction kettle, and another part of crude oil flows into the circulating heater, and the circulating heater utilizes crude oil to circularly heat the primary distillation tower.
The crude oil prepared by the method is used as an energy source to heat the primary distillation tower, so that the use of external oil is reduced, and the energy source is saved.
In summary, the present application includes at least one of the following beneficial technical effects:
1. the method comprises the steps of pre-treating waste oil, removing organic acid in the waste oil, reducing harmful substances in the waste oil, improving the quality of the waste oil, and further enabling the quality of finished oil prepared from the waste oil to be better; and then heating and evaporating the waste oil into a long-chain hydrocarbon component, and catalytically cracking the long-chain hydrocarbon component into short-chain hydrocarbon, wherein the catalytic cracking can be regarded as high-depth catalytic cracking, the hydrocarbon gas yield is far higher than that of the catalytic cracking, and a liquid product with higher aromatic hydrocarbon content can be obtained, namely the finished oil to be prepared by the method, so that the recovery rate of the finished oil can be effectively improved by adopting the waste oil preparation method. In addition, the equipment adopted by the method is sequentially connected in sequence, different reactions in the waste oil treatment process are divided according to the areas, so that the waste oil treatment process is more systematic and operates efficiently and stably;
2. the application decomposes organic acid in waste oil into water and light hydrocarbon in the pretreatment process, separates and collects the separated water and light hydrocarbon, and the collected water can be recycled, and the light hydrocarbon is condensed to prepare gasoline. The resource recovery and the resource reutilization are realized, and the environmental pollution and the resource waste are reduced;
3. this application has realized heating the primary tower with the crude oil of this application preparation through setting up circulating heater, reduces the use amount of exogenous oil, is favorable to resources are saved.
Drawings
FIG. 1 is a schematic view of an apparatus for preparing a finished oil from used oil according to the examples of the present application.
FIG. 2 is a schematic diagram B of an apparatus for preparing a finished oil from used oil according to the examples of the present application.
Reference numerals illustrate: 1. a pretreatment tank; 2. a primary distillation tower; 3. a reaction kettle; 4. a catalytic tower; 5. a fractionating tower; 6. a de-coloring sand tank; 61. a gasoline de-coloring sand tank; 611. a first tank; 612. a second tank; 62. a diesel oil de-coloring sand tank; 621. tank A; 622. a tank B; 7. an additive tank; 8. a circulation heater; 9. a light hydrocarbon condenser; 10. an oil-water separator; 11. a light hydrocarbon storage tank; 12. a water tank; 13. a concentrate tank; 14. a heater; 141. an electromagnetic heater; 142. a pipe heater; 143. a slag tank; 15. a condenser; 151. a top condenser; 152. a top cooler; 153. a bottom condenser; 16. gasoline tank; 17. chai Youguan; 18. a gasoline storage tank; 19. a diesel storage tank; 20. a gas buffer tank; 21. a gas purification tank; 22. a spray tower; 23. a tail gas absorption tower; 24. a UV photolytic purifier; 25. and (5) a centrifugal fan.
Detailed Description
The present application is described in further detail below with reference to examples. The specific description is: the following examples were conducted under conventional conditions or conditions recommended by the manufacturer, where specific conditions were not noted; the raw materials used in the following examples were all commercially available from ordinary sources except for the specific descriptions.
The technical scheme of the application is as follows:
waste oil is an oil contaminated with physical or chemical impurities, but in which there are still a large number of usable components. In practice, the waste oil is generally subjected to a purification treatment, which converts the waste oil into a finished oil that can be put into service. The waste oil treatment process mainly comprises two steps, wherein one is to add a settling agent to settle indissolvable matters in waste oil, and take upper oily matters as base oil for use after the indissolvable matters are removed. However, the oil still contains soluble organic acids which corrode the metal parts in the machine, resulting in oil-insoluble gelatinous deposits, which increase the viscosity of the oil and reduce its wear resistance. The second is to make simple pretreatment on waste oil, then make flash evaporation and condensation, and make the product oil after condensation, in which the principle of flash evaporation is that after the high-pressure saturated liquid is fed into a container with relatively low pressure, the saturated liquid is changed into saturated steam and saturated liquid due to the sudden drop of pressure. The working property of flash evaporation can be obtained as drying of a gas flow type, so that the energy consumption is high, in addition, when saturated liquid moves at a high speed in a dryer, the abrasion to equipment is serious, and the service life of the equipment is reduced.
Based on the above-identified problems, the present application provides a method and apparatus for preparing a product oil from waste oil, which includes an apparatus for preparing a product oil from waste oil and a method for preparing a product oil from waste oil, wherein the method for preparing a product oil from waste oil is realized by using the apparatus for preparing a product oil from waste oil.
Equipment for preparing finished oil from waste oil
The equipment includes the pretreatment tank 1, the primary distillation tower 2, the reaction kettle 3, the catalytic tower 4, the fractionating tower 5 and the decoloration sand tank 6 that link to each other in proper order, and the following is combined with fig. 1 and fig. 2, and the above-mentioned content is further explained:
referring to fig. 1, an additive tank 7 is connected to the left side of the pretreatment tank 1 through a metering pump, the additive tank 7 is used for storing a flocculant, and the metering pump delivers the flocculant to the pretreatment tank 1. The pretreatment tank 1 is connected with a feed pump, the feed pump is connected below the metering pump, and the feed pump is used for conveying waste oil to the pretreatment tank 1.
The lower extreme of pretreatment tank 1 is connected with preliminary distillation tower 2 charge-in pump, and the one end that preliminary distillation tower 2 charge-in pump kept away from pretreatment tank 1 is connected with circulation heater 8. The upper end of the circulation heater 8 is connected to the primary distillation tower 2, and the circulation heater 8 is used for heating the primary distillation tower 2.
The upper end of the primary distillation tower 2 is connected with a light hydrocarbon condenser 9, the lower end of the light hydrocarbon condenser 9 is connected with an oil-water separator 10, and the oil-water separator 10 is used for separating light hydrocarbon and water. The middle position of the oil-water separator 10 is connected with a light hydrocarbon storage tank 11, the lower end of the oil-water separator is connected with a water tank 12, and the water tank 12 is used for storing water separated by the oil-water separator 10.
The lower extreme of preliminary distillation tower 2 is connected with concentrate jar 13, and concentrate jar 13 is arranged in storing the crude oil in the preliminary distillation tower 2. One end of the concentrate tank 13 is connected with a circulating heat pump, and one end of the circulating heat pump, which is far away from the concentrate tank 13, is connected to the circulating heater 8. A part of crude oil in the concentrate tank 13 is fed to the circulation heater 8 by the circulation heat pump, and the circulation heater 8 heats the primary distillation column 2 with the crude oil. The right side of the concentrated solution tank 13 is connected to the reaction kettle 3, and the other part of crude oil in the concentrated solution tank 13 is conveyed into the reaction kettle 3.
The left side of the reaction kettle 3 is connected between the circulating heater 8 and the circulating heating pump, and the reaction kettle 3 is provided with a heater 14. The heater 14 comprises an electromagnetic heater 141 arranged on the outer wall of the reaction kettle 3, a heating pump arranged at the lower end of the reaction kettle 3, and a pipeline heater 142 connected to one end of the heating pump far away from the reaction kettle 3, wherein one end of the pipeline heater 142 far away from the heating pump is connected to the upper end of the reaction kettle 3. The electromagnetic heater 141 and the pipeline heater 142 are used for heating the reaction kettle 3 in a sectional manner, wherein the first section is that the electromagnetic heater 141 and the pipeline heater 142 heat the reaction kettle 3; the second section is that the electromagnetic heater 141 heats the reaction kettle 3.
A residuum tank 143 is connected between the pipeline heater 142 and the heating pump, the lower end of the residuum tank 143 is connected with a residuum oil pump, and the residuum oil pump conveys residuum to a residuum disposal area for processing.
Referring to fig. 1 and 2, the catalytic tower 4 is connected to the upper end of the reaction kettle 3, the upper end of the catalytic tower 4 is connected to the lower end of the fractionating tower 5, the fractionating tower 5 is connected with a condenser 15, and the condenser 15 comprises a top condenser 151 connected to the upper end of the fractionating tower 5, a top cooler 152 connected to the right side of the top condenser 151, and a bottom condenser 153 connected to the lower end of the fractionating tower 5. The top condenser 151 and the top cooler 152 are used to cool the light component oil flowing out from the upper end of the fractionation column 5, and the bottom condenser 153 is used to cool the heavy component oil flowing out from the bottom of the fractionation column 5. The gasoline tank 16 is connected to the right side of the top cooler 152, and the diesel tank 17 is connected to the right side of the bottom condenser 153.
Referring to fig. 2, the decoloring sand tank 6 includes a gasoline decoloring sand tank 61 and a diesel decoloring sand tank 62, wherein the gasoline decoloring sand tank 61 is divided into a first tank 611 and a second tank 612 connected side by side, and the diesel decoloring sand tank 62 is divided into a tank a621 and a tank B622 connected side by side. The right side of the gasoline tank 16 is connected with a gasoline decolorizing feed pump, the right side of the diesel tank 17 is connected with a diesel decolorizing feed pump, one end of the gasoline decolorizing feed pump far away from the gasoline tank 16 is connected between a first tank 611 and a second tank 612 through a pipeline, the diesel decolorizing feed pump is connected between a first tank 621 and a second tank 622 through a pipeline, the right sides of the first tank 611 and the second tank 612 are connected with a gasoline storage tank 18, and a diesel storage tank 19 is connected between the first tank 621 and the second tank 622.
The right sides of the gasoline storage tank 18 and the diesel storage tank 19 are provided with a gas buffer tank 20, and the upper ends of the gasoline storage tank 18 and the diesel storage tank 19 are connected in the gas buffer tank 20, wherein the oil-water separator 10 and the residual oil tank 143 are also connected with the gas buffer tank 20. The right side of the gas buffer tank 20 is connected with a water ring vacuum pump, and the right side of the water ring vacuum pump is connected with a gas purifying tank 21. The oil gas collected in the gas buffer tank 20 is conveyed to the gas purifying tank 21 by the water ring vacuum pump for purifying, so as to reduce the pollution of the oil gas to the environment.
The gas purification tank 21 is connected with a spray tower 22, a spray pump is connected to the left side of the spray tower 22, and a tail gas absorption tower 23 is connected to the left side of the spray pump. After the oil gas is sprayed and washed by the neutralization liquid in the spray tower 22, the waste gas contained in the oil gas is removed, so that the oil gas is further purified. The spray pump conveys the purified oil gas in the spray tower 22 into the tail gas absorption tower 23, and the tail gas absorption tower 23 absorbs the residual tail gas. The right side of tail gas absorption tower 23 is connected with UV photolysis clarifier 24, and the right side of UV photolysis clarifier 24 is connected with centrifugal fan 25. The UV photolysis purifier 24 irradiates the gas with a high-energy high-ozone UV light beam to further purify the oil gas, so that the oil gas reaches the emission standard, and the centrifugal fan 25 discharges the oil gas reaching the emission standard.
The process parameters of the above equipment are shown in table 1:
table 1 equipment process parameters
The devices not listed in the table can achieve the effect required by the application only by conventional operation.
Method for preparing finished oil from waste oil
The method for preparing the finished oil from the waste oil comprises the following steps:
step S1: waste oil is conveyed into a pretreatment tank through a feed pump, a flocculating agent in an additive tank is conveyed into the pretreatment tank through a metering pump, and the flocculating agent reacts with organic acid in the waste oil to obtain a flocculating product.
Further, the flocculant is an inorganic flocculant, and the inorganic flocculant can be concentrated sulfuric acid, sodium hydroxide solution, trisodium phosphate solution and the like, and the inorganic flocculant flocculates ash, carbon residue, asphaltene and mechanical impurities in the waste oil so as to reduce the impurity content in the waste oil;
still further, the flocculant is sodium hydroxide solution, the mass fraction of the sodium hydroxide solution is 0.5% -1%, the mass fraction is more preferably 0.8%, the addition amount of the sodium hydroxide solution is 20% -40% of the waste oil, and the addition amount is more preferably 30%. Wherein, if the waste oil is not treated, the organic acid in the waste oil comprises naphthenic acid, light acid, fatty acid, phenol and the like, and after the sodium hydroxide reacts with the waste oil, the flocculated product is salt or soap; if the waste oil is acid waste oil refined by sulfuric acid, the sodium hydroxide solution also reacts with free sulfuric acid, sulfonic acid and acid sulfuric acid in the waste oil, and the flocculated product is salt.
Step S2: and conveying the flocculated waste oil into a primary distillation tower through a feed pump, heating the primary distillation tower to 160-200 ℃ by using a circulating heater, heating and evaporating light hydrocarbon and water in the waste oil and overflowing the primary distillation tower to prepare crude oil. Wherein the light hydrocarbon comprises C 1 -C 16 Specific light hydrocarbons include C 5 -C 16 Further light hydrocarbons include C 5 And C 6.
Further, overflowed light hydrocarbon and water enter a light hydrocarbon condenser to be condensed into a water-oil mixture, the water-oil mixture flows into an oil-water separator from the lower end of the primary distillation tower to be separated, and the separated water and water respectively flow into a water tank and a light hydrocarbon storage tank to be stored.
Still further, crude oil enters a concentrated liquid tank, the crude oil is split through the concentrated liquid tank, a circulating heating pump conveys a small part of the crude oil to a circulating heater, and the circulating heater heats a primary distillation tower by utilizing the crude oil, so that the primary distillation tower distills new flocculated waste oil; a small part of crude oil flows into a pipeline heater through a heating pump, and the pipeline heater heats the reaction kettle by utilizing the crude oil; most crude oil enters the reaction kettle through the concentrated liquid tank for staged heating. Wherein, the mass of a small part of crude oil is 1% -5% of the total mass of the crude oil, and the mass of a large part of crude oil is 93% -97% of the total mass of the crude oil.
Wherein the step of heating comprises heating the reaction kettle to 380-420 ℃ by using an electromagnetic heater and a pipeline heater; and then the electromagnetic heater is singly used for heating the reaction kettle to 380-420 ℃, and long-chain hydrocarbon components and oil residues are obtained by evaporating crude oil in the stage heating process.
Step S3: the long-chain hydrocarbon component is conveyed upwards to the catalytic tower along the reaction kettle, oil residues flow into the residue oil tank along a pipeline between the pipeline heater and the heating pump, and the residue oil pump conveys residue oil to a residue oil treatment area for treatment.
Further, a catalyst is added into the catalytic tower, and the catalyst catalyzes and cracks long-chain hydrocarbon components to be cracked into short-chain hydrocarbon components. The catalyst is any one of an acidic solid catalyst, an alkaline catalyst and a noble metal catalyst, wherein the acidic solid catalyst can be aluminosilicate acid, phosphotungstic acid, aluminum oxide, zinc sulfide, cadmium sulfide and the like; the basic catalyst may be sodium oxide, potassium oxide, sodium hydroxide, potassium hydroxide, barium hydroxide, calcium hydroxide, aluminum hydroxide, lithium hydroxide, magnesium hydroxide, zinc hydroxide, copper hydroxide, iron hydroxide, lead hydroxide, cobalt hydroxide, chromium hydroxide, zirconium hydroxide, nickel hydroxide, ammonium hydroxide, sodium carbonate (monohydrate, heptahydrate, decahydrate), sodium bicarbonate (baking soda), potassium carbonate, potassium bicarbonate, etc.; the noble metal catalyst may be platinum, palladium, rhodium, silver, ruthenium, osmium, iridium, gold, and the like.
Step S4: the short-chain hydrocarbon component enters a fractionating tower for fractionation through a catalytic tower, and is fractionated into light component oil and heavy component oil. Wherein the fractionation temperature of the top line is 100-140 ℃ and the fractionation temperature of the bottom line is 350-400 ℃.
Further, the light component oil is alkane, naphthene or aromatic hydrocarbon containing 5-11 carbon atoms, and the further light component oil is alkane and aromatic hydrocarbon containing 8-10 carbon atoms; the carbon content of the heavy component oil is 80% -90%, the hydrogen content is 5% -15%, and the carbon content of the further heavy component oil is 86% -88% and the hydrogen content is 9% -11%.
The light component oil flows into the top cooler through the upper end of the fractionating tower for preliminary cooling, then flows into the top condenser through the top cooler for condensation into gasoline, and the gasoline flows into the gasoline tank through the top condenser for storage; the heavy component oil is condensed into diesel oil through a bottom condenser, and the diesel oil flows into a diesel oil tank through the bottom condenser to be stored.
Still further, the gasoline decoloring feeding pump conveys gasoline into the first tank and the second tank, decoloring is carried out at normal temperature and normal pressure, the diesel feeding pump conveys diesel into the first tank and the second tank, decoloring is carried out at normal temperature and normal pressure, and the removed impurities are colloid asphalt. And after the diesel oil and the gasoline are decolorized, respectively conveying the decolorized diesel oil and the decolorized gasoline into a diesel oil storage tank and a gasoline storage tank, wherein the decolorized gasoline and diesel oil are finished oil.
Examples
Example 1
Pretreatment: firstly, heating a pretreatment tank to 100 ℃, and conveying waste oil and sodium hydroxide solution into the pretreatment tank in the heating process for flocculation deacidification;
and (3) distilling: and (3) conveying the flocculated waste oil into a primary distillation tower, heating the primary distillation tower to 180 ℃ by using a circulating heater, and evaporating and removing water and light hydrocarbons in the flocculated waste oil to obtain crude oil.
And (3) heat treatment: crude oil is conveyed into a reaction kettle for sectional heating, wherein the first section of heating is an electromagnetic heater and a pipeline heater for heating the reaction kettle to 360 ℃, and the second section of heating is an electromagnetic heater for heating the reaction kettle to 400 ℃. Heating and evaporating crude oil to obtain long-chain hydrocarbon group residual oil, and storing the residual oil in a residual oil tank;
catalytic cracking: the long-chain hydrocarbon component enters a catalytic tower, and a catalyst is added into the long-chain hydrocarbon component to catalytically crack the long-chain hydrocarbon into a short-chain hydrocarbon component;
and (3) fractionation: the short-chain hydrocarbon component enters a fractionating tower for fractionation, the fractionation temperature is 380 ℃, light component oil and heavy component oil are obtained after fractionation, and the light component oil is firstly condensed by a top condenser and then cooled by a top cooler to obtain light oil; cooling the heavy component oil through a bottom condenser to obtain heavy oil;
decoloring: conveying the light oil to a gasoline decolorizing sand tank, decolorizing at normal temperature and absolute pressure of 10Kpa to obtain gasoline; the heavy oil enters a diesel oil de-coloring sand tank to be decolored under the conditions of normal temperature and absolute pressure of 10Kpa, and the diesel oil is prepared.
Examples 2 to 3
Examples 2-3 differ from example 1 in the distillation temperatures, which are shown in Table 2 for examples 2-3:
TABLE 2 distillation temperatures
| Initial distillation temperature (. Degree. C.) | |
| Example 2 | 160 |
| Example 3 | 200 |
Examples 4 to 6
Examples 4 to 6 differ from example 1 only in the temperature of the heat treatment, and the temperatures of the heat treatments of examples 4 to 6 are shown in Table 3:
TABLE 3 temperature of heat treatment
| First stage temperature (. Degree. C.) | Second stage temperature (. Degree. C.) | |
| Example 4 | 350 | 400 |
| Example 5 | 360 | 390 |
| Example 6 | 390 | 390 |
Examples 7 to 8
Examples 7-8 differ from example 1 only in the flocculant, examples 7-8 being shown in Table 4:
TABLE 4 flocculant
| Flocculant | |
| Example 7 | Concentrated sulfuric acid |
| Example 8 | Trisodium phosphate |
Comparative example
Comparative example 1
Comparative example 1 differs from example 1 only in that comparative example 1 did not pretreat the used oil.
Comparative example 2
Adding sodium hydroxide solution into waste oil for flocculation deacidification, raising the deacidified saturated waste oil to a high-pressure state, rapidly conveying the high-pressure saturated waste oil into a low-pressure container, changing the saturated waste oil into saturated steam and saturated liquid, taking the saturated liquid for condensation, and obtaining the diesel oil after condensation.
Detection method and data
Detection method
The present application is divided into two tests, one is to test the recovery rate of the finished oil (preferably diesel oil) and the other is to test the physicochemical properties of the finished oil (preferably diesel oil). The calculation method of the recovery rate comprises the following steps:
note that: a is the mass (kg) of waste oil, B is the mass (kg) of diesel oil
The physical and chemical property detection of the finished oil (diesel oil) is carried out by adopting a conventional detection method, and the detection standard is that of the diesel oil: GB25199-2017B5 diesel fuel.
Detecting data
Recovery rates of the finished oils (diesel oils) prepared in examples 1 to 8 and comparative examples 1 to 2 are shown in table 5:
TABLE 5 recovery of finished oil (Diesel)
| Recovery (%) | |
| Example 1 | 90 |
| Example 2 | 89.2 |
| Example 3 | 88 |
| Example 4 | 80 |
| Example 5 | 82 |
| Example 6 | 81 |
| Example 7 | 89 |
| Example 8 | 87 |
| Comparative example 1 | 89 |
| Comparative example 2 | 71 |
The physicochemical parameters of the finished oils (diesel) prepared in examples 1-8 and comparative examples 1-2 are shown in Table 6:
TABLE 6 physicochemical parameters of finished oil Diesel
As can be seen from a combination of tables 5 and 6, the recovery rate of the product oil in comparative example 2 was about 20% lower than that prepared in example 1, and when treating waste oil, a part of the oil was discharged with the sediment in comparative example 2, so that the recovery rate of waste oil in comparative example 2 was lower. By adopting the preparation method, the waste oil can be purified to the greatest extent, the waste oil and impurities are separated, the waste amount of the waste oil is reduced, the conversion rate of the waste oil into the finished oil (diesel oil) is improved, and the recovery rate of the finished oil (diesel oil) is further improved.
From tables 5 and 6, it can be seen that the recovery rates of the finished oil (diesel oil) in example 1 and comparative example 1 are almost the same, but the physicochemical parameters of the finished oil (diesel oil) prepared in comparative example 1 are lower than those of example 1, and since the waste oil of comparative example 1 is not pretreated, some organic acid remains in the prepared finished oil, and the organic acid may lower the physicochemical parameters of the finished oil. The content of organic acid in the finished oil prepared by the method is very small, the quality of the prepared finished oil (diesel oil) is better, and the damage to a machine is smaller when the finished oil is used.
The foregoing are all preferred embodiments of the present application, and are not intended to limit the scope of the present application in any way, therefore: all equivalent changes in structure, shape and principle of this application should be covered in the protection scope of this application.
Claims (10)
1. An apparatus for preparing finished oil from waste oil, characterized in that: the equipment is including the preliminary treatment jar, preliminary distillation tower, reation kettle, catalytic tower, fractionating tower and the decoloration sand jar that link to each other in proper order, the preliminary distillation tower connect in the lower extreme of preliminary treatment jar, be equipped with the heater on the reation kettle, the fractionating tower with be equipped with the condenser between the decoloration sand jar, the condenser including communicate in the top condenser at fractionating tower top with communicate in the bottom condenser at fractionating tower bottom.
2. The apparatus for preparing a finished oil from waste oil according to claim 1, wherein: one side of the primary distillation tower is provided with a circulating heater for heating the primary distillation tower, the lower end of the primary distillation tower is connected with a concentrated solution tank, and the concentrated solution tank is respectively connected to the circulating heater and the reaction kettle.
3. The apparatus for preparing a finished oil from waste oil according to claim 1, wherein: the top of the primary distillation tower is connected with a light hydrocarbon condenser, the bottom of the light hydrocarbon condenser is connected with an oil-water separator, and the oil-water separator is respectively connected with a light hydrocarbon storage tank and a water tank.
4. The apparatus for preparing a finished oil from waste oil according to claim 1, wherein: the heater comprises an electromagnetic heater and a pipeline heater which are arranged on the reaction kettle.
5. A process for preparing a finished oil from used oil, characterized in that it uses an apparatus according to any one of claims 1 to 4, said process comprising: conveying the waste oil into the pretreatment tank for pretreatment;
conveying the pretreated waste oil into a primary distillation tower, and distilling and dehydrating the waste oil and light hydrocarbon at 160-200 ℃ to prepare crude oil;
conveying the crude oil to the reaction kettle, heating to 380-420 ℃ in a partitioning way, and evaporating to obtain long-chain hydrocarbon components and oil residues;
conveying the long-chain hydrocarbon component into the catalytic tower, and adding a catalyst into the long-chain hydrocarbon component for catalytic cracking to obtain a short-chain hydrocarbon component;
and conveying the short-chain hydrocarbon component to the fractionating tower for fractionation to obtain light component oil and heavy component oil, wherein the light component oil is conveyed to the decoloring sand tank for decoloring to obtain gasoline after being condensed by a top condenser, and the heavy component oil is conveyed to the decoloring sand tank for decoloring to obtain diesel after being condensed by a bottom condenser.
6. The method for preparing finished oil from waste oil according to claim 5, wherein the pretreatment comprises: conveying the waste oil into the pretreatment tank and heating to 80-120 ℃;
and adding a flocculating agent into the waste oil in the heating process, and performing flocculation deacidification.
7. The method for preparing finished oil from waste oil according to claim 6, wherein: the flocculant is selected from any one of concentrated sulfuric acid, trisodium phosphate and sodium hydroxide.
8. The method for preparing finished oil from waste oil according to claim 5, wherein the heater comprises an electromagnetic heater and a pipeline heater which are arranged on the reaction kettle;
the staged heating includes: firstly, heating the reaction kettle to 350-380 ℃ by using an electromagnetic heater and the pipeline heater;
and heating the reaction kettle to 380-420 ℃ by using the electromagnetic heater.
9. The method for preparing finished oil by using waste oil according to claim 5, wherein a light hydrocarbon condenser is connected to the top of the primary distillation tower, an oil-water separator is connected to the bottom of the light hydrocarbon condenser, and a light hydrocarbon storage tank and a water tank are respectively connected to the oil-water separator;
the method further comprises the steps of: the removed water and light hydrocarbon enter the light hydrocarbon condenser along the upper end of the primary distillation tower to be cooled into a water-oil mixture;
and the water-oil mixture flows into the oil-water separator for separation, wherein water flows into the water tank for storage, and oil flows into the light hydrocarbon storage tank for storage.
10. The method for preparing finished oil by using waste oil according to claim 5, wherein a circulating heater for heating the primary distillation tower is arranged on one side of the primary distillation tower, a concentrated liquid tank is connected to the lower end of the primary distillation tower, and the concentrated liquid tank is respectively connected to the circulating heater and the reaction kettle;
the process of conveying the crude oil to the reaction kettle comprises the following steps: firstly, conveying the crude oil into the concentrated liquid tank for diversion;
wherein, a part of crude oil flows into the reaction kettle, and another part of crude oil flows into the circulating heater, and the circulating heater utilizes the crude oil to circularly heat the primary distillation tower.
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| CN202310498182.9A CN116396775A (en) | 2023-05-04 | 2023-05-04 | Equipment and method for preparing finished oil from waste oil |
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