CN102226104B - Method for producing gasoline and diesel by utilizing waste lubricating oil - Google Patents
Method for producing gasoline and diesel by utilizing waste lubricating oil Download PDFInfo
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- 239000002699 waste material Substances 0.000 title claims abstract description 58
- 239000010687 lubricating oil Substances 0.000 title claims abstract description 48
- 239000003502 gasoline Substances 0.000 title claims abstract description 20
- 238000004519 manufacturing process Methods 0.000 title abstract description 5
- 238000000034 method Methods 0.000 claims abstract description 31
- 239000003921 oil Substances 0.000 claims abstract description 31
- 238000004821 distillation Methods 0.000 claims abstract description 26
- 239000003054 catalyst Substances 0.000 claims abstract description 21
- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
- 238000000066 reactive distillation Methods 0.000 claims abstract description 11
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 8
- 239000002994 raw material Substances 0.000 claims abstract description 8
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000002283 diesel fuel Substances 0.000 claims description 29
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 19
- 239000001257 hydrogen Substances 0.000 claims description 9
- 229910052739 hydrogen Inorganic materials 0.000 claims description 9
- 239000002808 molecular sieve Substances 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
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 8
- 239000000567 combustion gas Substances 0.000 claims description 7
- 239000007789 gas Substances 0.000 claims description 6
- 238000006555 catalytic reaction Methods 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 5
- 229910010413 TiO 2 Inorganic materials 0.000 claims description 4
- 238000005336 cracking Methods 0.000 claims description 4
- 239000002131 composite material Substances 0.000 claims description 3
- 238000005194 fractionation Methods 0.000 claims description 3
- 229910003294 NiMo Inorganic materials 0.000 claims description 2
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 2
- 239000004519 grease Substances 0.000 claims description 2
- 230000010354 integration Effects 0.000 claims description 2
- 238000011068 loading method Methods 0.000 claims description 2
- 230000001050 lubricating effect Effects 0.000 claims description 2
- 239000010721 machine oil Substances 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 238000007233 catalytic pyrolysis Methods 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 12
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 7
- 239000000084 colloidal system Substances 0.000 abstract description 7
- 239000000203 mixture Substances 0.000 abstract description 6
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 6
- 230000007613 environmental effect Effects 0.000 abstract description 4
- 150000001875 compounds Chemical class 0.000 abstract description 2
- 230000000694 effects Effects 0.000 abstract description 2
- 239000007791 liquid phase Substances 0.000 abstract 1
- 238000000197 pyrolysis Methods 0.000 abstract 1
- 229910052717 sulfur Inorganic materials 0.000 abstract 1
- 239000011593 sulfur Substances 0.000 abstract 1
- 230000003197 catalytic effect Effects 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 7
- 239000005864 Sulphur Substances 0.000 description 6
- INILCLIQNYSABH-UHFFFAOYSA-N cobalt;sulfanylidenemolybdenum Chemical compound [Mo].[Co]=S INILCLIQNYSABH-UHFFFAOYSA-N 0.000 description 4
- 238000009776 industrial production Methods 0.000 description 4
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 3
- 150000001993 dienes Chemical class 0.000 description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 3
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 239000003818 cinder Substances 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000000314 lubricant Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000002594 sorbent Substances 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- 235000001018 Hibiscus sabdariffa Nutrition 0.000 description 1
- 235000005291 Rumex acetosa Nutrition 0.000 description 1
- 240000007001 Rumex acetosella Species 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 235000019219 chocolate Nutrition 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical compound [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 description 1
- WHDPTDWLEKQKKX-UHFFFAOYSA-N cobalt molybdenum Chemical compound [Co].[Co].[Mo] WHDPTDWLEKQKKX-UHFFFAOYSA-N 0.000 description 1
- 229910001981 cobalt nitrate Inorganic materials 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
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 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
- 238000005265 energy consumption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- MRDDPVFURQTAIS-UHFFFAOYSA-N molybdenum;sulfanylidenenickel Chemical compound [Ni].[Mo]=S MRDDPVFURQTAIS-UHFFFAOYSA-N 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
- 230000009965 odorless effect Effects 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000013502 plastic waste Substances 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 235000003513 sheep sorrel Nutrition 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
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Abstract
The invention discloses a method for producing gasoline and diesel by utilizing waste lubricating oil, belonging to the technical field of environmental protection and energy. The method is characterized in that the lubricating oil is used as the raw material and is subjected to reactive distillation, hydrofining and distillation to produce the high-quality gasoline and diesel; firstly the waste lubricating oil is subjected to reactive distillation to adjust the proportion of gasoline and diesel and reduce the content of colloid; then hydrofining reaction is carried out on a sulfide catalyst; monoene compounds are removed through monoolefine hydrogenation saturation reaction; sulfur, nitrogen and colloid are removed to produce the high-quality gasoline and diesel mixture free from extraneous odour; and the gasoline and diesel mixture is distilled to obtain gasoline and diesel distillates; wherein the sulfide catalyst is prepared by selecting an appropriate carrier according to the composition and properties of the pyrolysis plastic oil and adopting a liquid phase method. The method has the advantages of simple process, high catalyst activity and selectivity and good economic benefits and industrial application prospect.
Description
Technical field
The invention belongs to environment protection and energy technology field, relate to a kind of method of utilizing waste lubricating oil to produce petrol and diesel oil.
Background technology
The waste lubricating oil of Chinese market comes from motor vehicle market and two parts of field of industrial production.According to the analysis to motor vehicle market and field of industrial production waste lubricating oil market growth speed, follow the rapid growth of Chinese motor vehicle market maintenance, the time coming years, the waste lubricating oil market growth speed in Chinese motor vehicle market will keep very fast level.By contrast, owing to being subject to the impact of the aspect policies such as state macro-control, field of industrial production waste lubricating oil market growth speed will keep stable growth.After 2006, Chinese motor vehicle market waste lubricating oil market capacity will be over field of industrial production waste lubricating oil market capacity.According to the just slightly investigation at an ancient unit of weight plan Management Advisory Services industry research center, within 2010, Chinese waste lubricating oil market capacity is 5,000,000 tons, the production of China's lube product and use belong to the liner economy pattern of traditional industrial society's one-way type flow of resources, i.e. " petroleum resources one refining lube product one waste lubricating oil is abandoned " pattern.Waste oil regeneration Shuai Tong developed country compares larger gap.In general, can should be for the lubricants capacity reclaiming 50% left and right of consumption, yet the recovery utilization rate of waste lubricating oil is very low at present, the rerefined oil that returns every year use is less than 10%, a considerable amount of waste lubricating oils flow to not clear, and wherein a part enters environment and pollutes.Thereby lubricating oil is owing to being in use subject to, outside contamination produces a large amount of colloids, oxide compound reduces and even lost due effect meets with discarded.State Bureau of Environmental Protection has classified waste lubricating oil as this century at one of three large emphasis of field of Environment Protection major control, and make full use of waste lubricant oil regeneration reduction finished lube, or waste lubricating oil is refined into gasoline, diesel oil, can alleviate China's oil shortage and the growing imbalance between supply and demand of demand, can promote environmental protection again, turn waste into wealth, create considerable economic benefit, be that country encourages the project of helping, prospect is very wide.
For abundant waste lubricating oil recycling problem, according to the chemical constitution of waste lubricating oil and character, we have successfully developed the new technology that petrol and diesel oil is produced in waste lubricating oil catalytic distillation-hydrogenation upgrading-air distillation.The useless lubricated catalyzer with intellecture property that adopts, the cut ratio by catalytic distillation transformation technology adjustment petrol and diesel oil, reduces the gum level in cut; Carry out again hydrofining and obtain distillate, distillate is produced to the high-quality petrol and diesel oil of market in urgent need etc. through air distillation.In air distillation or the upgrading-air distillation of catalytic distillation-hydrogenation, without the three wastes, producing, is the process of green a, recycling.Following known technology, all comes with some shortcomings:
Chinese patent, publication number: CN201010182957.4, method and the device thereof of introduction Separation and Recovery processed oil from waste lubricating oil, its operation is more, 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 obtaining 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, consume a large amount of sorbent material expenses higher, and the oil quality obtaining is low.
Chinese patent, publication number: CN201010132513.X, introduces a kind of used lubricating oil complete hydrogenation type regenerated catalyst and its preparation method and application, 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 obtaining is low, and product yield is low.
Summary of the invention
The invention provides that a kind of method of utilizing waste lubricating oil to produce petrol and diesel oil is low for the product specification in waste lubricating oil conversion process, deficiency in economic performance and secondary pollution problems, the petrol and diesel oil of take is realized waste lubricating oil as target product and is carried out recycling, and fully utilize waste residue and the combustion gas of process itself, make the energy-conservation and environmental protection of production process, avoided secondary pollution.The present invention is by waste lubricating oil through catalytic reaction distillation, and hydrogenation upgrading, then pass through air distillation, cuts into gasoline (<150 ℃) and diesel oil (>150 ℃) according to recovered temperature.The present invention has improved the transformation efficiency of balanced reaction and the selectivity of consecutive reaction, energy-conservation of consumption reduction, has extended catalyst life, and flow process is simple and reduce investment outlay.
Technical scheme of the present invention is as follows:
Waste lubricating oil raw material waste lubricating oil in the present invention comprises gasoline, bavin machine oil, shafting oil, hydraulic efficiency oil, wear-resistant force feed, transformer oil, various lubricating grease and washes part oil, it is one or two or more kinds mixing wherein, also can select the waste rubber of rubber item as raw material, with waste rubber oil, replace waste lubricating oil as raw material.
The molecular sieve that the catalyzer of the use in the present invention is alumina load, wherein molecular sieve comprises ZSM-5, y-type zeolite, mordenite and β zeolite or their mixture, molecular sieve content is 0.5-95wt%.The size of preformed catalyst is definite according to the diameter of reactive distillation column, and the general equivalent diameter of granules of catalyst and the diameter of reactive distillation column ratio should be less than 0.1.The Main Function of catalyzer is selective splitting macromole, and carries out isomerization reaction simultaneously and obtain corresponding petrol and diesel oil cut.In addition catalyzer is also the filler of rectifying tower, for reacting the separated of product and product cut.
The method is that the gas phase catalysis cracking process on molecular sieve/aluminium oxide catalyst and the process integration of reactor product fractionation separates are carried out in reactive distillation column by waste lubricating oil.Raw material waste lubricating oil is injected to still kettle, adopt the waste residue and the combustion gas that in waste lubricating oil conversion process, produce to heat, still kettle temperature is controlled between 250-500 ℃.When still kettle heating arrives 250 ℃, the oil gas distilling enters in the reactive distillation column that molecular sieve/aluminium oxide catalyst is housed and reacts and rectifying, and agent-oil ratio is controlled between 1-20.Waste lubricating oil enters to mix with hydrogen by interchanger heating by feedstock pump through the cut of catalytic distillation and enters hydrofining reactor, controls feeding temperature at 250-350 ℃; Hydrogen partial pressure 1-6MPa, volume space velocity 0.5-4.0h
-1with hydrogen to oil volume ratio be 100-1000:1; The sulfide catalyst that hydrogenation is used is loading type NiMo, NiW, CoMo, CoW, NiMoW or CoMoW sulfide catalyst, and carrier is oxide carrier or the Carbon Materials with two mesopore composite structures, and oxide carrier is SiO
2, Al
2o
3, TiO
2, SiO
2-Al
2o
3or Al
2o
3-TiO
2.Distillate after hydrofining, through air distillation, cuts into gasoline (<150 ℃) and diesel oil (>150 ℃) according to recovered temperature.
The yield that obtains gasoline fraction (<150 ℃) by method production of the present invention is at 20-30%, and octane value is 75-85, density 0.70-0.76g/cm
3, can be used as the blend component of gasoline.The yield of diesel oil distillate (150-360 ℃) is at 60-80%, and cetane value is 65, density 0.83-0.86g/cm
3, condensation point, lower than-20 ℃, can be used as low-coagulation diesel oil No. 10.Combustion gas and cinder productive rate be not higher than 8%.
Catalytic distillation of the present invention, hydrofining and air distillation adopt the mode of operate continuously, flexible operation, easy.
The present invention adopts air distillation to combine with gas phase catalysis cracking process, and the combustion gas and the cinder that make full use of process have reduced energy consumption, non-secondary pollution; By air distillation and catalytic rectification process, improve the transformation efficiency of balanced reaction, improved the selectivity of reaction, extended the Hydrobon catalyst life-span, reduced catalyst levels simultaneously; First fractionation repeated hydrogenation, has reduced hydrogen consumption; Product yield is high, wide scope of material.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention.
In figure: 1 heating kettle; 2 reactive distillation column 3 hydrofining reaction towers; 4 distillation towers.
Embodiment
Below in conjunction with technical scheme and accompanying drawing, describe specific embodiments of the invention in detail.
Embodiment 1: the gas phase catalysis cracking of waste lubricating oil on molecular sieve/aluminium oxide catalyst.The reactive distillation column that heavy oil injection is equipped with to molecular sieve/aluminium oxide catalyst reacts and rectifying distillation tower, catalyzer is comprised of the aluminum oxide containing 30%ZSM-5 and 10% β zeolite, by molding bonded, obtain the columnar product of 2.0-3.0mm, length 3-8mm, bulk density 0.65-0.80g/mL, intensity is greater than 40N/mm.Adopt the waste residue and the combustion gas that in converting plastic waste to oil conversion process, produce to heat, agent-oil ratio is controlled between 1-20.The combustion gas producing is for the heating of distillation tower.Following table 1 is shown in catalytic distillation material balance test-results
Following table 2 is shown in catalytic distillation front and back oil property
| Raw material | Waste lubricating oil | Catalytic distillation |
| Density/gcm -1 | 0.88 | 0.81 |
| Sulphur/ppm | 9300 | 2200 |
| Nitrogen/ppm | 2800 | 2200 |
| Acid number/mgKOH.g -1 | 3.6 | 3.2 |
| Color | Chocolate | Sorrel |
| There is odorless | Have | Have |
Embodiment 2: supported cobalt molybdenum sulphide catalyzer is Hydrobon catalyst.Carrier adopts SiO
2-Al
2o
3, specific surface area is at 200-400m
2/ g, pore volume is at 0.5-2.0cm
3/ g, most probable pore size distribution is at 2-4nm and 10-15nm.Cobalt molybdenum sulphide precursor adopts Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES or Cobaltous diacetate or acetylacetone cobalt and ammonium thiomolybdate.Adopt equi-volume impregnating to prepare supported cobalt molybdenum sulphide catalyzer through dipping-dry-steps such as roasting.Following table 3 is shown in that reaction process condition and product form.
| Phase run | Initial stage/latter stage |
| Reactor hydrogen dividing potential drop/ |
4 |
| Volume space velocity/h -1 | 0.5 |
| Reactor inlet hydrogen to oil volume ratio | 800 |
| Average reaction temperature/℃ | 300 |
| Product property | ? |
| Diene/g. (100g) -1 | 0 |
| Colloid/mg100mL -1 | 25 |
| Nitrogen/ |
3 |
| Sulphur/μ gg -1 | 46 |
| Other | Color water-white |
? as shown in Table 3, oil distillate on supported cobalt molybdenum sulphide catalyzer in 300 ℃ of hydrofinings, diolefine in the product obtaining, do not detected, the content of colloid, sulphur and nitrogen reduces greatly, shows that supported cobalt molybdenum sulphide catalyzer has good desulfurization removing nitric deolefination efficiency.The product water-white obtaining, free from extraneous odour, the petrol and diesel oil mixture that quality is high.
Embodiment 3: the product introduction atmospheric distillation tower after hydrofining cuts into gasoline (<150 ℃) and diesel oil (>150 ℃) according to recovered temperature.Lower 4 tables are shown in vapour, diesel oil character
| ? | Gasoline | Diesel oil |
| Density/gcm -1 | 0.72 | 0.82 |
| Diene/g. (100g) -1 | 0 | 0 |
| Colloid/ |
2 | 20 |
| Nitrogen/μ gg -1 | 8 | 3 |
| Sulphur/μ gg -1 | 90 | 40 |
| Other | Color: water-white; Octane value: 75 | Color: pale yellow; Cetane value: 65 |
As shown in Table 4, oil distillate obtains petrol and diesel oil distillate through atmospheric distillation.The product free from extraneous odour obtaining, the gasoline that quality is high and diesel oil.
Embodiment 3: catalytic distillation distillate is raw material, on the basis of embodiment 1,2,3,4.0MPa and 300 ℃, carry out stability experiment, and following table 5 is shown in the reaction process condition of operation in 200 hours and finally obtains product property.
| ? | Gasoline | Diesel oil |
| Diene/g. (100g) -1 | 0 | 0 |
| Colloid/ |
2 | 21 |
| Nitrogen/μ gg -1 | 8 | 3 |
| Sulphur/μ gg -1 | 90 | 40 |
| Other | Color: water-white; Octane value: 75 | Color: pale yellow; Cetane value: 65 |
? the experimental result of 200 hours in 300 ℃ of hydrofinings, does not detect diolefine in the petrol and diesel oil product obtaining in air distillation on load-type nickel molybdenum sulphide catalyzer as shown in Table 4, for gasoline gum content, reaches 2mg100mL
-1, for diesel oil gum level, be also reduced to 21mg100mL
-1, sulphur and nitrogen containing comparing substantially constantly with starting test, meet national petrol and diesel oil standard, show the product free from extraneous odour that this technology obtains, have good stability, the vapour that quality is high, diesel oil.The above results shows that technology of the present invention has satisfactory stability.
Claims (4)
1. utilize waste lubricating oil to produce a method for petrol and diesel oil, gas phase catalysis cracking process and the reactor product fractionation separates process integration of waste lubricating oil on molecular sieve/aluminium oxide catalyst carried out in reactive distillation column; It is characterized in that:
Waste lubricating oil is injected to still kettle, adopt the waste residue and the combustion gas that in waste lubricating oil conversion process, produce to heat, still kettle temperature is controlled at 250-500 ℃; The oil gas distilling enters in the reactive distillation column that molecular sieve/aluminium oxide catalyst is housed and reacts and rectifying, and agent-oil ratio is controlled at 1-20; After catalytic pyrolysis, waste lubricating oil enters hydrofining reaction tower, feeding temperature 250-350 ℃, hydrogen partial pressure 1-6MPa, volume space velocity 0.5-4.0h through interchanger heating
-1, hydrogen to oil volume ratio 100-1000:1; The sulfide catalyst that hydrogenation is used is loading type sulfide catalyst; Carrier is the oxide carrier with two mesopore composite structures; Distillate after hydrofining, through air distillation, cuts into gasoline and diesel oil according to recovered temperature;
Described sulfide catalyst is NiMo, NiW, CoMo, CoW, NiMoW or CoMoW;
The described oxide carrier with two mesopore composite structures is SiO
2, Al
2o
3, TiO
2, SiO
2-Al
2o
3or Al
2o
3-TiO
2.
2. a kind of method of utilizing waste lubricating oil to produce petrol and diesel oil according to claim 1, be further characterized in that: waste lubricating oil comprises gasoline, bavin machine oil, shafting oil, hydraulic efficiency oil, wear-resistant force feed, transformer oil, various lubricating grease and washes part oil, is one or two or more kinds mixing wherein.
3. a kind of useless lubricated method of producing petrol and diesel oil of utilizing according to claim 1 and 2, is further characterized in that: in reactive distillation column, carry out reaction and rectifying, hydrofining and air distillation operate continuously.
4. a kind of method of utilizing waste lubricating oil to produce petrol and diesel oil according to claim 3, is further characterized in that: waste rubber oil replaces waste lubricating oil as raw material.
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| CN102676219A (en) * | 2012-05-15 | 2012-09-19 | 大连理工大学 | Method for utilizing coal tar to produce gasoline and diesel |
| CN102786985B (en) * | 2012-07-27 | 2015-01-07 | 大连理工大学 | Resource utilization method for waste lubricating oil |
| CN203582814U (en) * | 2013-08-29 | 2014-05-07 | 连力生 | Production device for producing diesel by using waste lubricating oil |
| CN104650949A (en) * | 2013-11-20 | 2015-05-27 | 东营争峰新能源技术有限公司 | Device for producing diesel oil through catalytic distillation of waste engine oil |
| CN103555367A (en) * | 2013-11-25 | 2014-02-05 | 辽宁中旭石油化工有限公司 | Method for producing naphtha, diesel oil and lubricant base oil by using used lubrication oil |
| CN104399512B (en) * | 2014-12-10 | 2017-01-11 | 郭帅 | Efficient and environment-friendly catalyst for waste tire oil regeneration |
| 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 |
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|---|---|---|---|---|
| CN101475870A (en) * | 2009-01-17 | 2009-07-08 | 大连理工大学 | Method for producing petrol and diesel oil by recycling waste lubricant oil |
| CN101845323A (en) * | 2010-05-14 | 2010-09-29 | 大连理工大学 | Process for producing petrol and diesel oil by plastic oil |
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| AU5607594A (en) * | 1992-11-17 | 1994-06-08 | Green Oasis Environmental Inc. | A process for converting waste motor oil to diesel fuel |
| BR9915120B1 (en) * | 1998-11-06 | 2010-12-14 | A process for the production of high quality medium oils and distillates from a hydrocarbon charge in which at least 20% by volume boils above 340 ° C and a plant for the production of high quality oils and, where appropriate, distillates high quality media. | |
| CN1132922C (en) * | 2001-01-05 | 2003-12-31 | 中国石油化工股份有限公司 | Waste oil recovering mathod |
-
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101475870A (en) * | 2009-01-17 | 2009-07-08 | 大连理工大学 | Method for producing petrol and diesel oil by recycling waste lubricant oil |
| CN101845323A (en) * | 2010-05-14 | 2010-09-29 | 大连理工大学 | Process for producing petrol and diesel oil by plastic oil |
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