CN107892990A - A kind of method of waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil - Google Patents
A kind of method of waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil Download PDFInfo
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- CN107892990A CN107892990A CN201711120967.3A CN201711120967A CN107892990A CN 107892990 A CN107892990 A CN 107892990A CN 201711120967 A CN201711120967 A CN 201711120967A CN 107892990 A CN107892990 A CN 107892990A
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- waste mineral
- lubricating oil
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- 238000000034 method Methods 0.000 title claims abstract description 100
- 239000002699 waste material Substances 0.000 title claims abstract description 51
- 239000010687 lubricating oil Substances 0.000 title claims abstract description 47
- 239000002199 base oil Substances 0.000 title claims abstract description 40
- 239000002480 mineral oil Substances 0.000 title claims abstract description 38
- 235000010446 mineral oil Nutrition 0.000 title claims abstract description 38
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 21
- 230000008929 regeneration Effects 0.000 title claims description 23
- 238000011069 regeneration method Methods 0.000 title claims description 23
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 59
- 239000002994 raw material Substances 0.000 claims abstract description 39
- 230000008569 process Effects 0.000 claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 239000012535 impurity Substances 0.000 claims abstract description 14
- 239000000654 additive Substances 0.000 claims abstract description 9
- 230000000996 additive effect Effects 0.000 claims abstract description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000001257 hydrogen Substances 0.000 claims abstract description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 6
- 239000003054 catalyst Substances 0.000 claims description 58
- 239000003921 oil Substances 0.000 claims description 50
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 32
- 239000000047 product Substances 0.000 claims description 22
- 238000007670 refining Methods 0.000 claims description 16
- 238000006298 dechlorination reaction Methods 0.000 claims description 13
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 12
- 238000005292 vacuum distillation Methods 0.000 claims description 12
- 238000010438 heat treatment Methods 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 10
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 9
- 229910052759 nickel Inorganic materials 0.000 claims description 9
- 239000011148 porous material Substances 0.000 claims description 9
- 238000011045 prefiltration Methods 0.000 claims description 9
- 229910052721 tungsten Inorganic materials 0.000 claims description 9
- 238000005406 washing Methods 0.000 claims description 9
- 238000004821 distillation Methods 0.000 claims description 8
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 8
- 239000002671 adjuvant Substances 0.000 claims description 7
- 239000003513 alkali Substances 0.000 claims description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims description 6
- 239000002245 particle Substances 0.000 claims description 6
- 239000000377 silicon dioxide Substances 0.000 claims description 6
- 150000007524 organic acids Chemical class 0.000 claims description 5
- 150000003839 salts Chemical class 0.000 claims description 5
- 239000002283 diesel fuel Substances 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 4
- 239000000314 lubricant Substances 0.000 claims description 4
- 238000004062 sedimentation Methods 0.000 claims description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 239000012752 auxiliary agent Substances 0.000 claims description 3
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 3
- 239000000292 calcium oxide Substances 0.000 claims description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 3
- 238000004581 coalescence Methods 0.000 claims description 3
- 238000007324 demetalation reaction Methods 0.000 claims description 3
- 239000000284 extract Substances 0.000 claims description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 3
- 239000002808 molecular sieve Substances 0.000 claims description 3
- 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 3
- 239000011787 zinc oxide Substances 0.000 claims description 3
- 238000005194 fractionation Methods 0.000 abstract description 10
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 abstract description 9
- 239000000460 chlorine Substances 0.000 abstract description 9
- 229910052801 chlorine Inorganic materials 0.000 abstract description 9
- 238000004939 coking Methods 0.000 abstract description 9
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 7
- 230000007774 longterm Effects 0.000 abstract description 6
- 239000010426 asphalt Substances 0.000 abstract description 5
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 4
- 238000005260 corrosion Methods 0.000 abstract description 4
- 230000007797 corrosion Effects 0.000 abstract description 4
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 4
- 239000011574 phosphorus Substances 0.000 abstract description 4
- 239000010703 silicon Substances 0.000 abstract description 4
- 229910052710 silicon Inorganic materials 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 description 11
- 239000002184 metal Substances 0.000 description 8
- 229910052752 metalloid Inorganic materials 0.000 description 6
- 150000002738 metalloids Chemical class 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- 239000002585 base Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000005530 etching Methods 0.000 description 5
- 229910052751 metal Inorganic materials 0.000 description 5
- 241000196324 Embryophyta Species 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 239000011575 calcium Substances 0.000 description 3
- 239000004927 clay Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 238000005461 lubrication Methods 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 238000000526 short-path distillation Methods 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- 239000011701 zinc Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 238000004061 bleaching Methods 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000005119 centrifugation Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- FPVGTPBMTFTMRT-NSKUCRDLSA-L fast yellow Chemical compound [Na+].[Na+].C1=C(S([O-])(=O)=O)C(N)=CC=C1\N=N\C1=CC=C(S([O-])(=O)=O)C=C1 FPVGTPBMTFTMRT-NSKUCRDLSA-L 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 238000002203 pretreatment Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 244000025254 Cannabis sativa Species 0.000 description 1
- HYBBIBNJHNGZAN-UHFFFAOYSA-N Furaldehyde Natural products O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 1
- 240000005702 Galium aparine Species 0.000 description 1
- 235000014820 Galium aparine Nutrition 0.000 description 1
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 1
- 241000612118 Samolus valerandi Species 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- LOTCVJJDZFMQGB-UHFFFAOYSA-N [N].[O].[S] Chemical compound [N].[O].[S] LOTCVJJDZFMQGB-UHFFFAOYSA-N 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000006229 carbon black Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 239000003863 metallic catalyst Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 239000003223 protective agent Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 238000009418 renovation Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000011973 solid acid Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/02—Working-up used lubricants to recover useful products ; Cleaning mineral-oil based
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M2203/00—Organic non-macromolecular hydrocarbon compounds and hydrocarbon fractions as ingredients in lubricant compositions
- C10M2203/10—Petroleum or coal fractions, e.g. tars, solvents, bitumen
- C10M2203/102—Aliphatic fractions
- C10M2203/1025—Aliphatic fractions used as base material
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10N—INDEXING SCHEME ASSOCIATED WITH SUBCLASS C10M RELATING TO LUBRICATING COMPOSITIONS
- C10N2020/00—Specified physical or chemical properties or characteristics, i.e. function, of component of lubricating compositions
- C10N2020/01—Physico-chemical properties
- C10N2020/02—Viscosity; Viscosity index
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Lubricants (AREA)
Abstract
The invention discloses a kind of method that waste mineral oil perhydro type regenerates production top-grade lubricating oil base oil, this method is additionally arranged pre-hydrotreating reaction technique between existing raw material pretreatment process and hydrogenation fractionating technique, under conditions of hydrogen is faced, the heavy metal additive and gum asphalt that are stripped of in lube cut and nonmetallic chlorine, phosphorus, the impurity such as silicon, the removing of these impurity solves the coking problem at the top of the hydrofining reactor in high-pressure hydrogenation fractionation process step below, and solves the problems, such as the chlorine corrosion of the equipment such as heat exchanger in being hydrogenated with high-pressure hydrogenation fractionation process, it ensure that hydrogenation plant long-term operation in high-pressure hydrogenation fractionation process.
Description
Technical field
The invention belongs to save and environmental technology field, it is high-grade to regenerate production more particularly, to a kind of waste mineral oil perhydro type
The method of lube base oil.
Background technology
Lubricating oil is made up of from composition 80%-90% base oil and 10%-20% additive, primary chemical
Composition is a variety of hydro carbons and the mixture of a small amount of non-hydrocarbons.But lubricating oil is in use for some time due to physics, chemistry
Or human factor result in the performance degradation of lubricating oil, generate such as aldehyde, ketone, resin, pitch colloidal materials, carbon black and organic
Acid, salt, water, metal fillings etc. pollute impurity, it is impossible to are further continued for using and turn into waste lubricating oil.Actually waste lubricating oil does not give up,
And simply a few percent therein that used lubricating oil really goes bad, therefore how effectively to remove these in waste lubricating oil
Impurity, it is the key of waste lubricant oil regeneration.The regeneration technology of waste lubricating oil mainly has distillation-pickling-clay-filtered at present, sinks
Drop-pickling-carclazyte distillation, sedimentation-distillation-pickling-clay-filtered, distillation-ethanolic extraction-clay-filtered, distillation-
Furfural treatment-clay-filtered, sedimentation-flocculation-clay-filtered etc..Above-mentioned technique all existence foundation oil utilization rates are low, it is big to produce
The shortcomings that measuring solid waste and acid sludge.Overcome the shortcomings of above-mentioned technique, Hydrofining Technology need to be used, with the presence of hydrogen
Under conditions of, through physics and it is chemical the methods of remove water, sulphur, nitrogen, chlorine, oxygen and various additives therein, obtain lubricate oil base
Plinth oil and the petrol and diesel oil blend component for meeting the requirement of state V.
With the further investigation and development of Technology of Used Lube Oil Regeneration, the place of the industrialized unit of waste lubricant oil regeneration
Reason amount is also increasing, therefore to environmental requirement also more and more higher.Such as Chinese patent (patent No. ZL200610086926.2)
Patent use clay treatment process equipment investment is few, simple to operate, good product quality, be middle-size and small-size regenerator for waste lubricating oil
Preferred process for purification.When the treating capacity increase of regenerator for waste lubricating oil, the quantity of clay-filtered caused spent bleaching clay slag
It is consequently increased, the harmless treatment of spent bleaching clay slag brings certain difficulty.
It is public in the technical scheme such as Chinese patent (CN102504933A) discloses a kind of renovation process of waste lubricating oil
The pre-treatment step of waste oil is opened：Waste lubricating oil is placed in a blender with stirring, adds the alkalization of waste lubricating oil
Compound, in room temperature to 10-60 minutes are stirred under the conditions of 100 degree, then move into and 1-10h settled in settling tank, with remove moisture and
Impurity.Short-path distillation is carried out afterwards, at least passes through following two-step distillation successively, and first order short-path distillation operating condition is temperature
150-250, vacuum 30-100pa, fractionate out light lubricating oil oil base stock, and then material enters second level short-path distillation, its
Operating condition is temperature 180-260, vacuum 5-20pa, steams middle matter lube oil base stocks, Residual oil is discharged by bottom of towe, the skill
Reclaimed oil purity is not high after the processing of art Conditioning regimen method, and regeneration efficiency is not also high, and not simple by pre-treatment step
Just, it is unfavorable for industrializing integrated production.
Chinese patent CN106350112A discloses the side that a kind of waste mineral oil pre-processed-be hydrogenated with reclaimed lubricating oil base oil
Method, this method comprise the following steps：Pretreatment and hydrofinishing；The preprocessing part includes deposition dehydrating, washing, dish successively
Chip centrifuge, horizontal centrifuge centrifugation, luwa evaporator evaporation and vacuum distillation step, pretreated lubrication oil base
Plinth oil plant passes through hydrofinishing again.Concrete operation step is：(1) waste mineral oil is introduced into settling tank, the water during sedimentation removing is oily
With greasy filth and big solid particle；(2) subsequently into water washing tank, alkali lye, water and demulsifier are added in water washing tank to remove
Organic acid and water miscible additive in oil；(3) wet oil in step (2) is sequentially entered into disc centrifuge centrifugation, crouched
Formula centrifuge removes solid impurity and water；(4) waste lubricating oil in step (3) is entered back into fused salt heating furnace, is heated to 300-
Enter luwa evaporator after 380 DEG C to evaporate；Preferable component lube stock in the waste mineral oil evaporated enters back into vacuum distillation
Tower, cuts out different lube cuts, and residual oil flows out in evaporator bottom of towe；(5) step (4) pretreated lube base
Oil plant is from being introduced into equipped with carrying out the further imurity-removal of pre- hydrofinishing in protectant reactor；It is useless through pre- hydrofinishing
Lubricating oil enters hydrogenation main reactor, and hydrofinishing is realized in the presence of hydrogenation catalyst, makes non-ideal group in feedstock oil
Divide hydrogenation saturation, product carries out stripping drying process, produces qualified products.This method can effectively remove big portion in useless lubrication
Point undesirable components, step are simple and easy to operate.But there is hydrofining reactor top in use in this method
The coking problem in portion, and there is etching problem in the equipment such as heat exchanger in being hydrogenated with.
The content of the invention
The invention solves first technical problem be to provide a kind of high-grade lubrication of waste mineral oil perhydro type regeneration production
The method of oil base oil；It this method solve the method mesohigh hydrofining reactor that Chinese patent CN106350112A is used
The coking problem at top, and there is etching problem in solve the equipment such as heat exchanger in hydrofining reaction.In addition, also solve
The product index pour point after hydrofinishing, viscosity index (VI), the oxidation stability etc. of having determined do not reach III class above top-grade lubricating oil base
The requirement of plinth oil index, further improve the quality of product.
In order to solve the above technical problems, invention adopts the following technical scheme that：
A kind of method of waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil of the present invention, comprises the following steps：
S1, raw material pretreatment process unit
S1-1, waste mineral oil are introduced into settling tank, water and greasy filth and big solid particle during sedimentation removing is oily；
S1-2, subsequently into water washing tank, alkali lye, water and demulsifier are added in water washing tank come remove organic acid in oil and
Water miscible additive；
S1-3, wet oil in step S1-2 sequentially entered into closed mechanical interception formula prefilter, closed mechanical interception formula
Fine filter and closed mechanical interception formula coalescer removing solid impurity and water；
S1-4 and then it would be heated to 200 DEG C and enter flash column, flash overhead extracts light component and minor amount of water；
S1-5, the bottom of towe oil in step S1-4 is entered back into and arrives 300-380 DEG C with fused salt heating furnace heating lava heat exchange
Luwa evaporator evaporation；Preferable component lube stock in the waste mineral oil evaporated enters back into vacuum distillation tower, cuts out
Different lubricant base oil fraction raw materials, residual oil flow out in evaporator bottom of towe；
S2, pre-hydrotreating reaction technique unit
S2-1, by the Lube basic oil material feedstocks from step S1-5 by heating stove heat, after being heated to 300-360 DEG C
Sequentially enter protection demetalization reactor and dechlorination reaction device；Guard catalyst is filled in the protection demetalization reactor and is taken off
Metallic catalyst, hydrotreating catalyst and dechlorination catalyst are filled in the dechlorination reaction device；
S2-2, the reacted oil of step S2-1 enter back into stripper removing hydrogen sulfide and ammonia, obtain hydrogenating materials；
S3, hydrogenation fractionating technique unit
By the hydrogenating materials after step S2-2 strippers it is heated after, sequentially enter hydrofining reactor, hydrogenation
Reforming reactor and post-refining reactor carry out high-pressure hydrogenation reaction；Product after hydrogenation enters back into conventional atmospheric distillation tower
And/or vacuum distillation tower, separate naphtha, diesel oil and it is various it is light, in, heavy lubricating oil base oil component.
The present invention is creatively additionally arranged pre-hydrotreating reaction between existing raw material pretreatment process and hydrogenation fractionating technique
Technique, the heavy metal additive and gum asphalt and nonmetallic chlorine being stripped of under conditions of hydrogen is faced in lube cut,
The impurity such as phosphorus, silicon, the removing of these impurity solve the hydrofining reactor top in high-pressure hydrogenation fractionation process step below
The coking problem in portion, and solve the problems, such as the chlorine corrosion of the equipment such as heat exchanger in being hydrogenated with high-pressure hydrogenation fractionation process, protect
Hydrogenation plant long-term operation in high-pressure hydrogenation fractionation process is demonstrate,proved.
In addition, the hydrogenation part in the present invention adds hydro-upgrading reaction, using isomerization-visbreaking modifying catalyst technology
Product pour point is reduced, improves product viscosity index and oxidation stability.
As the further improvement of technical scheme, the additional proportion of alkali lye, water and demulsifier in the step S1-2 is
0.1-0.2：1-1.5：0.01-0.05.
Preferably, in the step S1-3, the closed mechanical interception formula prefilter, the essence filtering of closed mechanical interception formula
The filtering accuracy of device and closed mechanical interception formula coalescer is：15 μm of prefilter, 1 μm of fine filter, coalescence precision 30-
50ppm。
Preferably, in the step S1-5, the operating condition of vacuum distillation is：300-360 DEG C of feeding temperature；Vacuum 5-
20pa；100-150 DEG C of tower top temperature.
As the further improvement of technical scheme, in step S2-1, process conditions are：In the case where facing hydrogen state, 0.5-
Under 1.0MPa lower pressures, 300-360 DEG C of reaction temperature, reaction velocity 0.2-0.5h-1, hydrogen-oil ratio 100-200:1.
Preferably, in step S2-1, the guard catalyst includes but is not limited to be carried for activity by aluminum oxide and silica
Body, load 2%-5%MO3Catalyst, and have Raschig ring, ball and bunge bedstraw herb of different shape and particle diameter etc..And change guarantor
The technology that grading loading is used according to different-grain diameter is loaded in shield agent in the reactor, is had stronger adsorption gel and is held dirty energy
Power.
Preferably, in step S2-1, it is active carrier that the catalyst for demetalation, which includes but is not limited to aluminum oxide, load
2.0%-5.0%MO3, 1.0%-2.5%NiO catalyst.
Preferably, in step S2-1, the hydrotreating catalyst includes but is not limited to aluminum oxide and silica for activity
Carrier, load 2%-5% WO3, 2.0%-3.0%NiO catalyst.
Preferably, in step S2-1, the dechlorination catalyst includes but is not limited to main as activity using calcium oxide and zinc oxide
Body, auxiliary agent concave convex rod is added, absorption chlorosity is up to more than 30%.
As the further improvement of technical scheme, in step s3, hydrofining reactor and the hydro-upgrading reaction
Device temperature is 320-360 DEG C, 260-320 DEG C of post-refining temperature of reactor；The hydrofining reactor, hydro-upgrading reaction
Pressure 8.0-15.0MPa, total air speed 0.5-1.0h in device and post-refining reactor-1, hydrogen-oil ratio 500-1200:1, supplement essence
Before reactor processed temperature is controlled with heat exchanger；Atmospheric distillation tower inlet temperature is 230-250 DEG C；Vacuum tower inlet temperature is
320-350 DEG C, more than vacuum 5-20pa.
Preferably, in step s3, the Hydrobon catalyst in the hydrofining reactor include but is not limited to by
Alumina support supports active component W, Ni and adjuvant component P compositions, in terms of the gross mass of the catalyst, active component and helps
The content of agent component is：WO325%-35%, NiO 2.0%-7.0%, P2.0%-5.5%, and the pore volume of the catalyst >=
0.40mL/g, specific surface area >=200m2/g。
Preferably, in step s3, the catalyst for hydro-upgrading in the hydro-upgrading reactor include but is not limited to by
ZSM-22 molecular sieves and alumina support support active component W, Ni composition, in terms of the gross mass of the catalyst, active component
Content is：WO310%-20%, NiO 2.0%-5.0%, and pore volume >=0.35mL/g of the catalyst, specific surface area >=
260m2/g。
Preferably, in step s3, the post-refining catalyst in the post-refining reactor include but is not limited to by
Alumina support supports active component W, Ni composition, in terms of the gross mass of the catalyst, the content of active component and adjuvant component
For：WO320%-30%, NiO 2.0%-5.0%, and pore volume >=0.42mL/g of the catalyst, specific surface area >=250m2/g。
Any scope described in the present invention includes any numerical value and end value or end value between end value and end value
Between any subrange for being formed of any number.
Unless otherwise specified, each raw material in the present invention can be obtained by commercially available purchase, equipment used in the present invention
The conventional equipment in art or the prior art with reference to art can be used to carry out.
Compared with prior art, the present invention has the advantages that：
1. the present invention solves the coking problem at the top of high-pressure hydrogenation finishing reactor, and solves hydrofining reaction
There is etching problem in the equipment such as middle heat exchanger.Add the long-term operation of High-pressure Hydrogenation Unit, traditional waste mineral oil
In high-pressure hydrogenation regeneration operating cycle 3-5 month, high-pressure hydrogenation fractionating device can be brought up to 12 service cycle by present invention process
More than individual month.
2. the hydrogenation part in the present invention adds hydro-upgrading reaction, using isomerization-visbreaking modification technology, production is reduced
Product pour point, product viscosity index and oxidation stability are improved, improve the bad quality of base oil in original waste mineral oil, carry
High properties of product, the lube base oil produced can reach III high-grade class base oil index request.
Brief description of the drawings
The embodiment of the present invention is described in further detail below in conjunction with the accompanying drawings
Fig. 1 is present invention process flow chart；
Embodiment
In order to illustrate more clearly of the present invention, with reference to preferred embodiment, the present invention is described further.Ability
Field technique personnel should be appreciated that following specifically described content is illustrative and be not restrictive, and this should not be limited with this
The protection domain of invention.
A kind of method of waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil of the present invention, comprises the following steps：
S1, raw material pretreatment process unit
S1-1, waste mineral oil are introduced into settling tank, water and greasy filth and big solid particle during sedimentation removing is oily；
S1-2, subsequently into water washing tank, alkali lye, water and demulsifier are added in water washing tank come remove organic acid in oil and
Water miscible additive；
S1-3, wet oil in step S1-2 sequentially entered into closed mechanical interception formula filter prefilter, fine filter
Solid impurity and water are removed with coalescer；
S1-4 and then it would be heated to 200 DEG C and enter flash column, flash overhead extracts light component and minor amount of water；
S1-5, the bottom of towe oil in step S1-4 is entered back into and arrives 300-380 DEG C with fused salt heating furnace heating lava heat exchange
Luwa evaporator evaporation；Preferable component lube stock in the waste mineral oil evaporated enters back into vacuum distillation tower, cuts out
Different lube cuts, residual oil flow out in evaporator bottom of towe；
In raw material pretreatment process, waste mineral oil first passes through step S1-1, S1-2 and S1-3 and is dehydrated, takes off slag, so
Flash removing part water and light component etc. by step S1-4 afterwards to handle, it is laggard that the heavy constituent oil after processing enters luwa evaporator
Enter vacuum distillation tower, the lubricating oil rationality component distilation in waste mineral oil is come out, the restructuring containing heavy metal, gum asphalt
Divide to extract out in bottom of towe and can be used as good asphalt stock；
S2, pre-hydrotreating reaction technique unit
S2-1, by the pre-hydrotreating reaction raw material from step S1-4 by heating stove heat, after being heated to 300-360 DEG C according to
It is secondary to enter protection demetalization reactor and dechlorination reaction device；Guard catalyst and Tuo Jin are filled in the protection demetalization reactor
Metal catalyst, hydrotreating catalyst and dechlorination catalyst are filled in the dechlorination reaction device；It is described protection demetalization reactor and
Dechlorination reaction device is used to further remove chlorine, the phosphorus carried into the part heavy metal and gum asphalt and additive in oil
With the material such as silicon；
S2-2, the reacted lube cuts of step S2-1 enter back into stripper removing hydrogen sulfide and ammonia, obtain high pressure
Hydrogenating materials；
S3, hydrogenation fractionating technique unit
By the high-pressure hydrogenation raw material after step S2-2 strippers it is heated after, sequentially enter hydrofining reactor,
Hydro-upgrading reactor and post-refining reactor carry out high-pressure hydrogenation reaction；To carry out removing the impurity such as sulphur nitrogen oxygen and matter, enter
Row aromatic hydrocarbons saturation, isomerization dewaxing reduce the reaction such as oil pour point；Product after hydrogenation enter back into conventional atmospheric distillation tower and/or
Vacuum distillation tower, separate naphtha, diesel oil and it is various it is light, in, heavy lubricating oil base oil component.
The present invention is creatively additionally arranged pre-hydrotreating reaction between existing pretreating process and high-pressure hydrogenation fractionation process
Technique, under conditions of hydrogen low pressure is faced, the impurity such as heavy metal and nonmetallic chlorine, phosphorus, silicon for being stripped of in lube cut, these
The removing of impurity solves the coking problem at the top of the hydrofining reactor in high-pressure hydrogenation fractionation process step below, and
Also solve the problems, such as the chlorine corrosion of the equipment such as heat exchanger in being hydrogenated with high-pressure hydrogenation fractionation process, ensure that high-pressure hydrogenation is fractionated work
Hydrogenation plant long-term operation in skill.
In certain embodiments of the present invention, the additional proportion of the alkali lye in the step S1-2, water and demulsifier is
0.1-0.2：1-1.5：0.01-0.05.
In certain embodiments of the present invention, it is the closed mechanical interception formula prefilter, closed in the step S1-3
The filtering accuracy of mechanical interception formula fine filter and closed mechanical interception formula coalescer is：15 μm of prefilter, the μ of fine filter 1
M, coalescence precision 30-50ppm.
In certain embodiments of the present invention, in the step S1-5, the operating condition of vacuum distillation is：Feeding temperature
300-360℃；Vacuum 5-20pa；100-150 DEG C of tower top temperature.
In certain embodiments of the present invention, in step S2-1, process conditions are：In 0.5-1.0MPa lower pressures
Under, 300-360 DEG C of reaction temperature, reaction velocity 0.2-0.5h-1, hydrogen-oil ratio 100-500:1.
In certain embodiments of the present invention, in step S2-1, the guard catalyst includes but is not limited to by aluminum oxide
It is active carrier with silica, loads 2%-5%MO3Catalyst, and have the Raschig ring of different shape and particle diameter, ball and four
Leaf grass etc..And change protective agent and load the technology that grading loading is used according to different-grain diameter in the reactor, there is stronger suction
Attached colloid and the dirty ability of appearance.
In certain embodiments of the present invention, in step S2-1, the catalyst for demetalation includes but is not limited to aluminum oxide
For active carrier, 2.0%-5.0%MO is loaded3, 1.0%-2.5%NiO catalyst.
In certain embodiments of the present invention, in step S2-1, the hydrotreating catalyst includes but is not limited to aoxidize
Aluminium and silica are active carrier, load 2%-5% WO3, 2.0%-3.0%NiO catalyst.
In certain embodiments of the present invention, in step S2-1, the dechlorination catalyst includes but is not limited to calcium oxide
It is active main body with zinc oxide, adds auxiliary agent concave convex rod, absorption chlorosity is up to more than 30%.
In certain embodiments of the present invention, in step s3, hydrofining reactor and the hydro-upgrading reactor
Temperature is 320-360 DEG C, 260-320 DEG C of post-refining temperature of reactor；The hydrofining reactor, hydro-upgrading reactor
With the pressure system total 8.0-15.0MPa, total air speed 0.5-1.0h in post-refining reactor-1, hydrogen-oil ratio 500-1200：1, mend
Fill before finishing reactor and control temperature with heat exchanger；Atmospheric distillation tower inlet temperature is 230-250 DEG C；Vacuum tower inlet temperature
For 320-350 DEG C, more than vacuum 5-20pa.
In certain embodiments of the present invention, in step s3, the hydrogenation catalyst during hydrofinishing is specifically
Active component W, Ni is supported by alumina support and adjuvant component P is formed, in terms of the gross mass of the catalyst, active component and
The content of adjuvant component is：WO325%-35%, NiO 2.0%-7.0%, P2.0%-5.5%, and the pore volume of the catalyst >=
0.40mL/g, specific surface area >=200m2/g。
In certain embodiments of the present invention, in step s3, the hydro-upgrading catalysis in the hydro-upgrading reactor
Agent including but not limited to supports active component W, Ni by ZSM-22 molecular sieves and alumina support and formed, with total matter of the catalyst
Gauge, the content of active component are：WO310%-20%, NiO 2.0%-5.0%, and pore volume >=0.35mL/ of the catalyst
G, specific surface area >=260m2/g。
In certain embodiments of the present invention, in step s3, the post-refining catalysis in the post-refining reactor
Agent including but not limited to supports active component W, Ni by alumina support and formed, in terms of the gross mass of the catalyst, active component
Content with adjuvant component is：WO320%-30%, NiO 2.0%-5.0%, and pore volume >=0.42mL/g of the catalyst, than
Surface area >=250m2/g。
Embodiment 1
A kind of method of waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil, concrete technology condition are as follows：Take
Waste mineral oil sample, as shown in the sample 1 in table 1 below, after testing, the waste mineral oil raw material color is deep, acid number is high, sulfur content
High, chlorinity height, content of beary metal are high, and the raw material is hydrogenated with technique unit by raw material pretreatment process unit with pre-, and raw material enters
The main process conditions of three technique units are shown in Table 2, and the lube base oil of pretreatment of raw material and weighted BMO spaces output is former
Expect property such as table 3.The property of product lube base oil such as table 4 after hydrogenation fractionating.
Table 1：The waste mineral oil feedstock property of embodiment 1
| Property | Waste mineral oil raw material 1 | Waste mineral oil raw material 2 |
| Density/g.cm-3 | 0.878 | 0.864 |
| Color | Black | Black |
| Acid number/mgKOH/g | 3.5 | 8.4 |
| Moisture, % | 3.5 | 4.0 |
| Sulfur content, ppm | 3502 | 2853 |
| Chlorinity, ppm | 521 | 680 |
| Metal and metalloid content | ||
| ω(P)/ppm | 1081 | 956 |
| ω(Si)/ppm | 50 | 46 |
| ω(Na)/ppm | 158 | 220 |
| ω(Ca)/ppm | 1855 | 2123 |
| ω(Mg)/ppm | 278 | 356 |
| ω(Fe)/ppm | 64 | 84 |
| ω(Zn)/ppm | 1058 | 1825 |
The raw material of 2 embodiment of table 1 enters the main process conditions of three technique units
| Process conditions | Raw material pretreatment process unit | Pre-hydrotreating technique unit | Hydrogenation fractionating technique unit |
| Temperature/DEG C | Enter luwa evaporator raw material 340 | Raw material enters furnace outlet 320 | Raw material enters furnace outlet 340 |
| Pressure/MPa | - | 0.15 | 10.0 |
| Air speed | - | 0.5 | 0.4 |
| Hydrogen-oil ratio | - | 100 | 800 |
The pretreatment of raw material of 3 embodiment of table 1 and weighted BMO spaces product property
| Property | Pretreatment of raw material oil | Weighted BMO spaces oil |
| Density/g.cm-3 | 0.8606 | 0.860 |
| Color | It is red bright | Yellow |
| Acid number/mgKOH/g | 0.8 | 0.01 |
| Moisture, % | 0.1 | Vestige |
| Sulfur content, ppm | 2820 | 320 |
| Chlorinity, ppm | 485 | 0.5 |
| Metal and metalloid content | ||
| ω(P)/ppm | 2.5 | ＜ 0.5 |
| ω(Si)/ppm | 0.5 | ＜ 0.5 |
| ω(Na)/ppm | 1.0 | ＜ 0.5 |
| ω(Ca)/ppm | 10 | ＜ 0.5 |
| ω(Mg)/ppm | 1.2 | ＜ 0.5 |
| ω(Fe)/ppm | 0.9 | ＜ 0.5 |
| ω(Zn)/ppm | 5.3 | ＜ 0.5 |
The property of product lube base oil after the hydrogenation fractionating of 4 embodiment of table 1.
Raw material in the embodiment 1 of table 1 is reacted by the process conditions in table 2, as can be seen from Table 3 after pretreating process
Content of beary metal does not reach hydrogenation index request (hydrogenation index total metalses ＜ 10ppm) also, but by pre- hydrogenation technique after
Heavy metal and chlorinity can ensure the effect of hydrogenation technique long-term operation.
Each product after hydrogenation fractionating has reached III class lubricating oil base oil index request as can be seen from Table 3
Using the technique of the present invention, do not occur coking problem, and hydrofinishing at the top of high-pressure hydrogenation finishing reactor
The equipment such as heat exchanger does not also occur etching problem in reaction, and high-pressure hydrogenation fractionating device can be operated week by present invention process
Phase brings up to 18 months.
Embodiment 2
A kind of method of waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil, concrete technology condition are as follows：Table 1
In raw material 2 by following process conditions, the raw material enters by raw material pretreatment process unit and pre- hydrogenation technique unit, raw material
The main process conditions of three technique units are shown in Table 5, and the lube base oil of pretreatment of raw material and weighted BMO spaces output is former
Expect property such as table 6.The property of product lube base oil such as table 7 after hydrogenation fractionating.
The raw material of 5 embodiment of table 1 enters the main process conditions of three technique units
| Process conditions | Raw material pretreatment process unit | Pre-hydrotreating technique unit | Hydrogenation fractionating technique unit |
| Temperature/DEG C | Enter luwa evaporator raw material 340 | Raw material enters furnace outlet 320 | Raw material enters furnace outlet 340 |
| Pressure/MPa | - | 0.20 | 15.0 |
| Air speed | - | 0.6 | 0.5 |
| Hydrogen-oil ratio | - | 200 | 1000 |
The pretreatment of raw material of 6 embodiment of table 1 and weighted BMO spaces product property
| Property | Pretreatment of raw material oil | Weighted BMO spaces oil |
| Density/g.cm-3 | 0.8602 | 0.863 |
| Color | It is red bright | Yellow |
| Acid number/mgKOH/g | 0.7 | 0.01 |
| Moisture, % | 0.1 | Vestige |
| Sulfur content, ppm | 2150 | 150 |
| Chlorinity, ppm | 412 | 0 |
| Metal and metalloid content | ||
| ω(P)/ppm | 2.0 | ＜ 0.5 |
| ω(Si)/ppm | 0.5 | ＜ 0.5 |
| ω(Na)/ppm | 1.0 | ＜ 0.5 |
| ω(Ca)/ppm | 8.9 | ＜ 0.5 |
| ω(Mg)/ppm | 1.0 | ＜ 0.5 |
| ω(Fe)/ppm | 0.7 | ＜ 0.5 |
| ω(Zn)/ppm | 5.1 | ＜ 0.5 |
The property of product lube base oil after the hydrogenation fractionating of 7 embodiment of table 1.
Raw material in the embodiment 1 of table 1 is reacted by the process conditions in table 5, as can be seen from Table 6 after pretreating process
Content of beary metal does not reach hydrogenation index request (hydrogenation index total metalses ＜ 10ppm) also, but by pre- hydrogenation technique after
Heavy metal and chlorinity can ensure the effect of hydrogenation technique long-term operation.
Each product after hydrogenation fractionating has reached III class lubricating oil base oil index request as can be seen from Table 7
Using the technique of the present invention, do not occur coking problem, and hydrofinishing at the top of high-pressure hydrogenation finishing reactor
The equipment such as heat exchanger does not also occur etching problem in reaction, and high-pressure hydrogenation fractionating device can be operated week by present invention process
Phase brings up to 24 months.
Comparative example 1
Reclaimed lubricating oil base oil is pre-processed-is hydrogenated with using a kind of waste mineral oil disclosed in Chinese patent CN106350112A
Method, the product produced by embodiment 1 does not reach III class lubricating oil base oil index request, and high-pressure hydrogenation fractionation dress
Put and only maintain by 6 months service cycle, cause coking at the top of high-pressure hydrogenation finishing reactor, high pressure heat exchanger chlorine corrosion is tight
Weight.The class lubricating oil part basis oil industry index request of 8 sinopec of table III
The class lubricating oil part basis oil industry index request of 8 sinopec of table III
Obviously, the above embodiment of the present invention is only intended to clearly illustrate example of the present invention, and is not pair
The restriction of embodiments of the present invention.For those of ordinary skill in the field, may be used also on the basis of the above description
To make other changes in different forms.Here all embodiments can not be exhaustive.It is every to belong to this hair
Row of the obvious changes or variations that bright technical scheme is extended out still in protection scope of the present invention.
Claims (10)
- A kind of 1. method of waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil, it is characterised in that：Including following step Suddenly：S1, raw material pretreatment process unitS1-1, waste mineral oil are introduced into settling tank, water and greasy filth and big solid particle during sedimentation removing is oily；S1-2, subsequently into water washing tank, alkali lye, water and demulsifier are added in water washing tank to remove organic acid in oil and water-soluble The additive of property；S1-3, wet oil in step S1-2 is sequentially entered to closed mechanical interception formula prefilter, closed mechanical interception formula essence mistake The filter system arrangement of filter and closed mechanical interception formula coalescer, remove solid impurity and water；S1-4 and then it would be heated to 200 DEG C and enter flash column, flash overhead extracts light component and minor amount of water；S1-5, bottom of towe oil in step S1-4 is entered back into and scraped with fused salt heating furnace heating lava heat exchange to 300-380 DEG C Film evaporator evaporates；Preferable component lube stock in the waste mineral oil evaporated enters back into vacuum distillation tower, cuts out difference Lubricant base oil fraction raw material, residual oil evaporator bottom of towe flow out；S2, pre-hydrotreating reaction technique unitS2-1, by the Lube basic oil material feedstocks from step S1-5 by heating stove heat, after being heated to 300-360 DEG C successively Enter protection demetalization reactor and dechlorination reaction device；Guard catalyst and demetalization are filled in the protection demetalization reactor Catalyst, hydrotreating catalyst and dechlorination catalyst are filled in the dechlorination reaction device；S2-2, the reacted oil of step S2-1 enter back into stripper removing hydrogen sulfide and ammonia, obtain hydrogenating materials；S3, hydrogenation fractionating technique unitBy the hydrogenating materials after step S2-2 strippers it is heated after, sequentially enter hydrofining reactor, hydro-upgrading Reactor and post-refining reactor carry out high-pressure hydrogenation reaction；Product after hydrogenation enter back into conventional atmospheric distillation tower and/ Or vacuum distillation tower, separate naphtha, diesel oil and it is various it is light, in, heavy lubricating oil base oil component.
- 2. the method for waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil, its feature exist according to claim 1 In：The additional proportion of alkali lye, water and demulsifier in step S1-2 is 0.1-0.2：1-1.5：0.01-0.05.
- 3. the method for waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil, its feature exist according to claim 1 In：Preferably, in step S1-3, the closed mechanical interception formula prefilter, closed mechanical interception formula fine filter and closed The filtering accuracy of mechanical interception formula coalescer is：15 μm of prefilter, 1 μm of fine filter, coalescence precision 30-50ppm.
- 4. the method for waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil, its feature exist according to claim 1 In：Preferably, in step S1-5, the operating condition of vacuum distillation is：300-360 DEG C of feeding temperature；Vacuum 5-20pa；Tower top 100-150 DEG C of temperature.
- 5. the method for waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil, its feature exist according to claim 1 In in step S2-1, process conditions are：In the case where facing hydrogen state, 0.5-1.0MPa lower pressures, 300-360 DEG C of reaction temperature, Reaction velocity 0.2-0.5h-1, hydrogen-oil ratio 100-200:1.
- 6. the method for waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil, its feature exist according to claim 1 In：Preferably, in step S2-1, it is active carrier that the guard catalyst, which includes but is not limited to by aluminum oxide and silica, is born Carry 2%-5%MO3Catalyst.
- 7. the method for waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil, its feature exist according to claim 1 In：Preferably, in step S2-1, it is active carrier that the catalyst for demetalation, which includes but is not limited to aluminum oxide, loads 2.0%- 5.0%MO3, 1.0%-2.5%NiO catalyst.
- 8. the method for waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil, its feature exist according to claim 1 In：Preferably, in step S2-1, the hydrotreating catalyst includes but is not limited to aluminum oxide and silica is active carrier, Load 2%-5% WO3, 2.0%-3.0%NiO catalyst.
- 9. the method for waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil, its feature exist according to claim 1 In：Preferably, in step S2-1, the dechlorination catalyst includes but is not limited to using calcium oxide and zinc oxide as active main body, adds Adding assistant concave convex rod, absorption chlorosity is up to more than 30%.
- 10. the method for waste mineral oil perhydro type regeneration production top-grade lubricating oil base oil, its feature exist according to claim 1 In：In step s3, hydrofining reactor and the hydro-upgrading temperature of reactor is 320-360 DEG C, post-refining reaction 260-320 DEG C of device temperature；Pressure 8.0- in the hydrofining reactor, hydro-upgrading reactor and post-refining reactor 15.0MPa, total air speed 0.5-1.0h-1, hydrogen-oil ratio 500-1200:1, temperature is controlled with heat exchanger before post-refining reactor； Atmospheric distillation tower inlet temperature is 230-250 DEG C；Vacuum tower inlet temperature is 320-350 DEG C, more than vacuum 5-20pa；Preferably, in step s3, the Hydrobon catalyst in the hydrofining reactor includes but is not limited to by aoxidizing Alumina supporter supports active component W, Ni and adjuvant component P compositions, in terms of the gross mass of the catalyst, active component and auxiliary agent group Point content be：WO325%-35%, NiO 2.0%-7.0%, P2.0%-5.5%, and the pore volume of the catalyst >= 0.40mL/g, specific surface area >=200m2/g；Preferably, in step s3, the catalyst for hydro-upgrading in the hydro-upgrading reactor includes but is not limited to by ZSM- 22 molecular sieves and alumina support support active component W, Ni composition, in terms of the gross mass of the catalyst, the content of active component For：WO310%-20%, NiO 2.0%-5.0%, and pore volume >=0.35mL/g of the catalyst, specific surface area >=260m2/g；Preferably, in step s3, the post-refining catalyst in the post-refining reactor includes but is not limited to by aoxidizing Alumina supporter supports active component W, Ni composition, and in terms of the gross mass of the catalyst, the content of active component and adjuvant component is： WO320%-30%, NiO 2.0%-5.0%, and pore volume >=0.42mL/g of the catalyst, specific surface area >=250m2/g。
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5783068A (en) * | 1994-09-13 | 1998-07-21 | Total Raffinage Distribution, S.A. | Process for dechlorination of a spent oil fraction |
| CN1571829A (en) * | 2001-10-16 | 2005-01-26 | 国际壳牌研究有限公司 | Upgrading of pre-processed used oils |
| CN104611058A (en) * | 2015-02-05 | 2015-05-13 | 武汉科林精细化工有限公司 | Hydrofining process of waste lubricating oil |
| CN105733793A (en) * | 2014-12-06 | 2016-07-06 | 中国石油化工股份有限公司 | Hydrogenation method for regenerating waste lubricating oil, |
| CN106350112A (en) * | 2015-07-14 | 2017-01-25 | 新疆聚力环保科技有限公司 | Method for pretreating waste mineral oil and performing hydrogenation regeneration to produce lubricating base oil |
| CN107254330A (en) * | 2017-08-15 | 2017-10-17 | 湖北润驰环保科技有限公司 | A kind of waste lubricating oil perhydro method produces the process engineering for regenerating of high-grade low-freezing lube base oil |
-
2017
- 2017-11-14 CN CN201711120967.3A patent/CN107892990B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5783068A (en) * | 1994-09-13 | 1998-07-21 | Total Raffinage Distribution, S.A. | Process for dechlorination of a spent oil fraction |
| CN1571829A (en) * | 2001-10-16 | 2005-01-26 | 国际壳牌研究有限公司 | Upgrading of pre-processed used oils |
| CN105733793A (en) * | 2014-12-06 | 2016-07-06 | 中国石油化工股份有限公司 | Hydrogenation method for regenerating waste lubricating oil, |
| CN104611058A (en) * | 2015-02-05 | 2015-05-13 | 武汉科林精细化工有限公司 | Hydrofining process of waste lubricating oil |
| CN106350112A (en) * | 2015-07-14 | 2017-01-25 | 新疆聚力环保科技有限公司 | Method for pretreating waste mineral oil and performing hydrogenation regeneration to produce lubricating base oil |
| CN107254330A (en) * | 2017-08-15 | 2017-10-17 | 湖北润驰环保科技有限公司 | A kind of waste lubricating oil perhydro method produces the process engineering for regenerating of high-grade low-freezing lube base oil |
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Denomination of invention: A method for producing high-grade lubricating base oil through hydrogen regeneration of waste mineral oil Granted publication date: 20201113 Pledgee: Bank of China Limited Urumqi Branch Pledgor: XINJIANG JULI ENVIRONMENTAL PROTECTION TECHNOLOGY Co.,Ltd. Registration number: Y2024980038341 |