CN102786985A - Resource utilization method for waste lubricating oil - Google Patents
Resource utilization method for waste lubricating oil Download PDFInfo
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- CN102786985A CN102786985A CN2012102652797A CN201210265279A CN102786985A CN 102786985 A CN102786985 A CN 102786985A CN 2012102652797 A CN2012102652797 A CN 2012102652797A CN 201210265279 A CN201210265279 A CN 201210265279A CN 102786985 A CN102786985 A CN 102786985A
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- oil
- lubricating oil
- waste lubricating
- distillate
- distillation
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- 239000002699 waste material Substances 0.000 title claims abstract description 43
- 239000010687 lubricating oil Substances 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 34
- 239000003054 catalyst Substances 0.000 claims abstract description 25
- 239000002283 diesel fuel Substances 0.000 claims abstract description 21
- 238000006243 chemical reaction Methods 0.000 claims abstract description 18
- 239000003921 oil Substances 0.000 claims abstract description 16
- 239000002199 base oil Substances 0.000 claims abstract description 11
- 239000003502 gasoline Substances 0.000 claims abstract description 10
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000004821 distillation Methods 0.000 claims description 31
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 21
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 11
- 239000001257 hydrogen Substances 0.000 claims description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims description 11
- 238000005984 hydrogenation reaction Methods 0.000 claims description 11
- 239000002808 molecular sieve Substances 0.000 claims description 9
- 238000004064 recycling Methods 0.000 claims description 9
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 9
- 229910010413 TiO 2 Inorganic materials 0.000 claims description 8
- 239000000567 combustion gas Substances 0.000 claims description 8
- 238000005336 cracking Methods 0.000 claims description 7
- 238000000066 reactive distillation Methods 0.000 claims description 6
- 238000006555 catalytic reaction Methods 0.000 claims description 5
- 229910003294 NiMo Inorganic materials 0.000 claims description 4
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 4
- 239000002131 composite material Substances 0.000 claims description 4
- 239000007789 gas Substances 0.000 claims description 4
- 238000011068 loading method Methods 0.000 claims description 4
- 239000000295 fuel oil Substances 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 6
- 239000000084 colloidal system Substances 0.000 abstract description 5
- 238000006477 desulfuration reaction Methods 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 abstract description 3
- 150000001875 compounds Chemical class 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000006392 deoxygenation reaction Methods 0.000 abstract 1
- 230000009965 odorless effect Effects 0.000 abstract 1
- 230000003197 catalytic effect Effects 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- INILCLIQNYSABH-UHFFFAOYSA-N cobalt;sulfanylidenemolybdenum Chemical compound [Mo].[Co]=S INILCLIQNYSABH-UHFFFAOYSA-N 0.000 description 5
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000010913 used oil Substances 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 3
- 238000013459 approach Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- 239000010457 zeolite Substances 0.000 description 3
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 2
- 238000009874 alkali refining Methods 0.000 description 2
- 239000003818 cinder Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- MRDDPVFURQTAIS-UHFFFAOYSA-N molybdenum;sulfanylidenenickel Chemical compound [Ni].[Mo]=S MRDDPVFURQTAIS-UHFFFAOYSA-N 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 239000002594 sorbent Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical group [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- WHDPTDWLEKQKKX-UHFFFAOYSA-N cobalt molybdenum Chemical compound [Co].[Co].[Mo] WHDPTDWLEKQKKX-UHFFFAOYSA-N 0.000 description 1
- QAHREYKOYSIQPH-UHFFFAOYSA-L cobalt(II) acetate Chemical compound [Co+2].CC([O-])=O.CC([O-])=O QAHREYKOYSIQPH-UHFFFAOYSA-L 0.000 description 1
- SZKXDURZBIICCF-UHFFFAOYSA-N cobalt;pentane-2,4-dione Chemical compound [Co].CC(=O)CC(C)=O SZKXDURZBIICCF-UHFFFAOYSA-N 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- ZKKLPDLKUGTPME-UHFFFAOYSA-N diazanium;bis(sulfanylidene)molybdenum;sulfanide Chemical compound [NH4+].[NH4+].[SH-].[SH-].S=[Mo]=S ZKKLPDLKUGTPME-UHFFFAOYSA-N 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000004945 emulsification Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- -1 nitrogenous compound Chemical class 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-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
- 239000002243 precursor Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000032258 transport Effects 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a resource utilization method for waste lubricating oil and belongs to the fields of environmental protection and energy technology. The method is characterized in that the waste lubricating oil is used as the raw material, is distilled and then is hydrofined to produce high-quality gasoline, diesel and base oil, and comprises the steps that the waste lubricating oil is firstly distilled to obtain a fraction with the temperature lower than 500 DEG C and a fraction with the temperature higher than 500 DEG C, then the fraction with the temperature lower than 500 DEG C is reacted in a manner of hydrofining on a sulfide catalyst, a monoene compound is removed by monoolefine hydrostturation reaction, desulfuration, denitrification, deoxygenation and colloid removal are carried out to produce odorless high-quality mixed oil of the gasoline, the diesel and the base oil, and then the mixed oil is distilled to obtain distillate oil of the gasoline, the diesel and the base oil. The distilled fraction with the temperature higher than 500 DEG C is hydrofined after being reactively distilled. The method disclosed by the invention has the advantages of simple process, high catalyst activity and selectivity, and good economic benefits and industrial application prospects.
Description
Technical field
The invention belongs to environment protection and energy technology field, relate to a kind of method of waste lubricating oil recycling.
Background technology
Waste lubricating oil is meant the lubricating oil that changes from various machineries, vehicle, boats and ships.Lubricating oil in use receives outside contamination to produce a large amount of colloids and oxide compound loses due effect thereby its production process is.According to statistics, China has Motor vehicles 200,000,000 volumes now, more than 10 ten thousand of ships that transports, and nearly 400,000 of motor fishing vessel, only these three lubricating oil of need changing in every month just reach 5,000,000 tons, and quantity is big but seldom to have recycling, has both caused waste oil pollution environment.The waste lubricating oil deep processing becomes clean fuel, in the energy substitution conversion, has more important strategic position.The waste lubricating oil secondary industry also is faced with some problem demanding prompt solutions when welcoming good opportunity to develop.At present; China's waste lubricating oil deep processing prepares the clean fuel oil treatment process roughly has two kinds of approach: first kind of approach, waste lubricating oil are after the normal pressure distillation, and light ends oil is processed oil fuel through acid-alkali refining, and (colourity is high; Irritating smell is arranged, of poor quality) or emulsification after the burning that acts as a fuel.In this simultaneously, the sulfur-bearing nitrogenous impurity becomes SO in combustion processes
xAnd NO
x, environment is polluted.And a large amount of acid sludge, waste soda residue and the sewage of generation in the acid-alkali refining process.Second kind of approach is raw oil with the waste lubricating oil, utilizes the method for heat to make used oil produce gasification, makes its shallow degree cracking through bar shaped Y zeolite alumina silicate catalyst bed then, produces the diesel component product through the condensation youngster at last.But this method, there are two deficiencies in itself, and the first makes alumina silicate catalyst produce coking easily, thereby influences its reactive behavior because waste lubricating oil exists colloid.It two is that sulfur-bearing in the used oil, nitrogenous compound fail to remove, and influences the quality of product.
To abundant waste lubricating oil recycling problem, according to the chemical constitution and the character of waste lubricating oil, we have successfully developed the method for used oil air distillation or catalytic distillation-hydrogenation upgrading-air distillation production vapour, diesel oil and base oil.Waste lubricating oil obtains less than 500 through distillation
oC cut and greater than 500
oThe C cut next will be less than 500
oC cut hydrofining reaction on sulfide catalyst.And greater than 500
oThe C cut adopts the catalyzer with intellecture property, and the cut ratio through catalytic distillation transformation technology adjustment petrol and diesel oil reduces the gum level in the cut; Carry out unifining again and obtain distillate, distillate is produced the high-quality petrol and diesel oil and the basic wet goods of market in urgent need through the normal pressure distillation.The no three wastes produce in air distillation or catalytic distillation-hydrogenation upgrading-air distillation, are a processes green, recycling.
Chinese patent, publication number: CN 102226104A, introduced a kind of method of utilizing waste lubricating oil to produce petrol and diesel oil, its process is because waste lubricating oil all will pass through reactive distillation, and the catalyst for cracking consumption is big, and only produces vapour, diesel oil.
Chinese patent, publication number: CN201010182957.4, the method and the device thereof of introduction Separation and Recovery processed oil from waste lubricating oil, its operation is more, and is more loaded down with trivial details, produce " three wastes ", and product quality is low.
Chinese patent, publication number: CN201010160808.8 introduces the method for utilizing waste oil processing liquid fuel oil, and its operation is many, and waste liquid is many, and the product quality that obtains is low.
Chinese patent, publication number: CN201010151513.4 introduces a kind of preparation method of reclaimed lubricating oil fraction, and its process will be used sorbent material, and it is higher to consume a large amount of sorbent material expenses, and the oil quality that obtains is low.
Chinese patent, publication number: CN201010132513.X introduces a kind of used lubricating oil complete hydrogenation type regenerated catalyst, and it crosses range request 15MPa high pressure, high hydrogen-oil ratio, consumption hydrogen is many, and the product performance that obtain are poor.
Chinese patent, publication number: CN200920141806.7, the novel appts of introduction refining light diesel from waste lubricating oil, the diesel quality that obtains is low, and product yield is low.
Summary of the invention
The technical problem that the present invention will solve is, deficiency in economic performance low to the product specification in the waste lubricating oil conversion process and secondary pollution problems; With vapour, diesel oil and base oil is that target product realizes that waste lubricating oil carries out recycling; And the waste residue and the combustion gas of comprehensive utilization process itself; Make the energy-conservation and environmental protection of production process, avoided secondary pollution.Specifically, the present invention cuts distillate with waste lubricating oil through the normal pressure distillation, less than 500
oThe direct hydrogenation of C distillate obtains petrol and diesel oil through fractionation again.And greater than 500
oThe C BO need be through the upgrading of catalytic reaction distillation repeated hydrogenation.The present invention improved transformation efficiency and the consecutive reaction of balanced reaction selectivity, energy-conservation of consumption reduction, prolonged catalyst life, flow process is simple and reduce investment outlay.
Technical scheme of the present invention is following:
Waste lubricating oil gets into distillation tower and cuts into 500 ℃ of distillate (< 500 ℃) and BOes (> through distillation according to recovered temperature).Distillate directly gets into hydrogenator, controls feeding temperature at 260-380 ℃, hydrogen partial pressure 3-8 MPa, volume space velocity 0.5-4.0 h
-1With hydrogen to oil volume ratio be 200-1000:1; Hydrogen recycles after separation and purification; The sulfide catalyst that hydrogenation uses is the oxide carrier with two mesopore composite structures as loading type NiMo, NiW, CoMo, CoW, NiMoW or CoMoW sulfide catalyst, carrier, and oxide carrier is SiO
2, Al
2O
3, TiO
2, SiO
2-Al
2O
3Or Al
2O
3-TiO
2The gas phase catalysis cracking of BO on molecular sieve/aluminium oxide catalyst.BO is injected the reaction fractionating tower that molecular sieve/aluminium oxide catalyst is housed carry out reactive distillation, the distillate behind the reactive distillation can directly get into hydrogenator unifining, adopts the waste residue and the combustion gas that produce in the waste lubricating oil conversion process to heat.Distillate after the unifining distills through normal pressure, cuts into 280 ℃ of gasoline (< 180 ℃), diesel oil (< 280 ℃) and base oils (> according to recovered temperature).Technique scheme can continuous operation.BO mixes with hydrogen after the interchanger heating gets into hydrogenator through the feedstock pump entering through the cut of catalytic distillation, and the control feeding temperature is at 260-380
oC; Hydrogen partial pressure 3-8 MPa, volume space velocity 0.5-4.0 h
-1With hydrogen to oil volume ratio be 200-1000:1; The sulfide catalyst that hydrogenation uses is the oxide carrier with two mesopore composite structures as loading type NiMo, NiW, CoMo, CoW, NiMoW or CoMoW sulfide catalyst, carrier, and oxide carrier is SiO
2, Al
2O
3, TiO
2, SiO
2-Al
2O
3Or Al
2O
3-TiO
2
The catalyzer that catalytic distillation tower among the present invention uses is the molecular sieve of alumina load, and wherein molecular sieve comprises ZSM-5, y-type zeolite, mordenite and β zeolite or their mixture, and molecular sieve content is 0.5-95wt%.The main effect of catalyzer is the cracking macromole, and carries out isomerization reaction simultaneously.The catalyzer that the hydrogenation reaction tower uses is the oxide carrier with two mesopore composite structures as loading type NiMo, NiW, CoMo, CoW, NiMoW or CoMoW sulfide catalyst, carrier, and oxide carrier is SiO
2, Al
2O
3, TiO
2, SiO
2-Al
2O
3Or Al
2O
3-TiO
2
Through method production of the present invention obtain gasoline fraction (<180 ℃ > yield at 5-15%, octane value is 75-85, density 0.70-0.76g/cm
3, can be used as the blend component of gasoline.Diesel oil distillate (<280 ℃) yield at 10-30%, cetane value is 55, density 0.83-0.86g/cm
3, condensation point is lower than-10 ℃, can be used as low-coagulation diesel oil No. 10.Base oil fractions (>280 ℃) yield at 50-60%, density 0.91-0.97g/cm
3, yield combustion gas and cinder productive rate are not higher than 8%.
The mode of operate continuously, flexible operation, easy are adopted in air distillation of the present invention, catalytic distillation and unifining.
The invention has the beneficial effects as follows:
1) adopt air distillation to combine with the gas phase catalysis cracking process, the combustion gas and the cinder that make full use of process have reduced energy consumption, non-secondary pollution;
2) combine through air distillation and reaction rectification technique and improved the transformation efficiency of balanced reaction, improved the selectivity of reaction, prolonged the Hydrobon catalyst life-span, reduced catalyst levels simultaneously;
3) first fractionation repeated hydrogenation has reduced the hydrogen consumption;
4) high, high, the wide scope of material of yield of quality product.
Description of drawings
Accompanying drawing is a process flow diagram of the present invention.
Among the figure: 1 atmospheric distillation tower; 2 reactive distillation columns; 3 hydrogenators; 4 distillation towers.
Embodiment
Be described in detail specific embodiment of the present invention below in conjunction with technical scheme and accompanying drawing.
Embodiment 1
The raw material waste lubricating oil is injected atmospheric distillation tower, adopt the waste residue and the combustion gas that produce in the used oil conversion process to heat.Cut into 500 ℃ of distillate (< 500 ℃) and BOes (> according to recovered temperature).Following table 1 is air distillation material balance result.
Distillate character before and after following table 2 air distillations
Embodiment 2
The gas phase catalysis cracking of BO on molecular sieve/aluminium oxide catalyst.BO is injected the reaction fractionating tower that molecular sieve/aluminium oxide catalyst is housed to react and the rectifying distillation tower; Catalyzer is made up of the aluminum oxide that contains 30% ZSM-5 and 10% β zeolite; Obtain the columnar product of 2.0-3.0 mm through molding bonded; Length 3-8 mm, bulk density 0.65-0.80 g/mL, intensity is greater than 40 N/mm.Adopt the waste residue and the combustion gas that produce in the waste lubricating oil conversion process to heat, agent-oil ratio is controlled between the 1-20.The combustion gas that produces is used for the heating of distillation tower.Following table 3 is seen catalytic distillation material balance test-results.
Embodiment 3
Hydrogenation catalyst adopts load-type nickel molybdenum sulfur catalyst.Carrier adopts SiO
2-Al
2O
3, specific surface area is at 200-400 m
2/ g, pore volume is at 0.5-2.0 cm
3/ g, the most probable pore size distribution is at 2-4 nm and 10-15nm.Cobalt molybdenum sulphide precursor adopts Xiao Suangu or Cobaltous diacetate or acetylacetone cobalt and ammonium thiomolybdate.Adopt equi-volume impregnating to prepare supported cobalt molybdenum sulphide catalyzer through dipping-drying-steps such as roasting.Following table 4 is seen reaction process condition and product composition.
Can know by table 4, distillate on supported cobalt molybdenum sulphide catalyzer in 360
oC unifining, the content that does not detect diolefine and colloid, sulphur and nitrogen in the product that obtains reduces greatly, shows that supported cobalt molybdenum sulphide catalyzer has good desulfurization removing nitric deolefination efficient.The product water-white that obtains, free from extraneous odour, the petrol and diesel oil mixture that quality is high.
Embodiment 5
Product after the unifining gets into atmospheric distillation tower and cuts into 280 ℃ of gasoline (< 180 ℃), diesel oil (< 280 ℃) and base oils (> according to recovered temperature).5 tables are seen petrol and diesel oil character down.
Can know by table 5, oil distillate on supported cobalt molybdenum sulphide catalyzer in 360
oC unifining does not detect diolefine in the product that obtains, the content of colloid, sulphur and nitrogen reduces significantly, shows that supported cobalt molybdenum sulphide catalyzer has good desulfurization removing nitric deolefination efficient.The product water-white that obtains, free from extraneous odour, the gasoline that quality is high, diesel oil and base oil.
Embodiment 6
With the catalytic distillation diesel oil distillate is raw material, on the basis of embodiment 5 in 6.0MPa and 360
oC carries out stability experiment, and following table 5 is seen the reaction process condition of operation in 200 hours and the product property that obtains at last.
Can know 200 hours experimental result by table 4, on load-type nickel molybdenum sulphide catalyzer in 360
oC unifining does not detect diolefine in the petrol and diesel oil product that air distillation obtains, reach 2 mg100mL for gasoline gum content
-1, also be reduced to 10 mg100mL for the diesel oil gum level
-1, containing with beginning test of sulphur and nitrogen compared constantly basically, meets national petrol and diesel oil standard, shows the product free from extraneous odour that this technology obtains, and has good stability petrol and diesel oil that quality is high and base oil.The above results shows that technology of the present invention has satisfactory stability property.
Claims (3)
1. the method for a waste lubricating oil recycling is characterized in that:
Waste lubricating oil gets into distillation tower and cuts into distillate and BO through distillation according to recovered temperature; Distillate directly gets into hydrogenator, controls feeding temperature at 260-380 ℃, hydrogen partial pressure 3-8 MPa, volume space velocity 0.5-4.0 h
-1, hydrogen to oil volume ratio is 200-1000:1; Hydrogen recycles after separation and purification; Hydrogenation working load type sulfide catalyst, carrier is the oxide carrier with two mesopore composite structures; The gas phase catalysis cracking of BO on molecular sieve/aluminium oxide catalyst; Heavy oil is injected the reaction fractionating tower that molecular sieve/aluminium oxide catalyst is housed carry out reactive distillation, the distillate behind the reactive distillation directly gets into hydrogenator unifining, adopts the waste residue and the combustion gas that produce in the waste lubricating oil conversion process to heat; Distillate after the unifining distills through normal pressure, cuts into gasoline, diesel oil and base oil according to recovered temperature.
2. the method for a kind of waste lubricating oil recycling according to claim 1, its characteristic also is: the loading type sulfide catalyst is NiMo, NiW, CoMo, CoW, NiMoW or CoMoW.
3. the method for a kind of waste lubricating oil recycling according to claim 1, its characteristic also is:, oxide carrier is SiO
2, Al
2O
3, TiO
2, SiO
2-Al
2O
3Or Al
2O
3-TiO
2
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|---|---|---|---|
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|---|---|---|---|
| CN201210265279.7A CN102786985B (en) | 2012-07-27 | 2012-07-27 | Resource utilization method for waste lubricating oil |
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| CN102786985B CN102786985B (en) | 2015-01-07 |
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ID=47152578
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Cited By (6)
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| CN103710132A (en) * | 2013-12-20 | 2014-04-09 | 武汉理工大学 | Engine oil recovery and pretreatment device of vertical retired passenger car |
| CN103820148A (en) * | 2014-01-23 | 2014-05-28 | 周文彬 | Used mineral oil full-automatic control catalytic cracking environment-friendly integrated refining equipment and process |
| CN104004543A (en) * | 2014-05-05 | 2014-08-27 | 大连理工大学 | Method for catalysis upgrading regeneration of waste engine oil |
| CN104629796A (en) * | 2013-11-14 | 2015-05-20 | 东营争峰新能源技术有限公司 | Device for producing diesel oil by using waste diesel oil |
| CN112717946A (en) * | 2020-12-31 | 2021-04-30 | 西北化工研究院有限公司 | Spent lubricating oil hydrogenation regeneration catalyst and preparation method thereof |
| RU2805935C1 (en) * | 2022-07-05 | 2023-10-24 | Акционерное общество "НПО "Стример" | Method and device for determining zeolite resource |
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| CN102226104A (en) * | 2011-05-23 | 2011-10-26 | 大连理工大学 | Method for producing gasoline and diesel by utilizing waste lubricating oil |
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|---|---|---|---|---|
| CN101307272A (en) * | 2008-07-04 | 2008-11-19 | 剧长生 | Regeneration process for waste lubrication oil |
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| CN104629796A (en) * | 2013-11-14 | 2015-05-20 | 东营争峰新能源技术有限公司 | Device for producing diesel oil by using waste diesel oil |
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| CN103820148A (en) * | 2014-01-23 | 2014-05-28 | 周文彬 | Used mineral oil full-automatic control catalytic cracking environment-friendly integrated refining equipment and process |
| CN104004543A (en) * | 2014-05-05 | 2014-08-27 | 大连理工大学 | Method for catalysis upgrading regeneration of waste engine oil |
| CN112717946A (en) * | 2020-12-31 | 2021-04-30 | 西北化工研究院有限公司 | Spent lubricating oil hydrogenation regeneration catalyst and preparation method thereof |
| RU2805935C1 (en) * | 2022-07-05 | 2023-10-24 | Акционерное общество "НПО "Стример" | Method and device for determining zeolite resource |
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