CN106190238A - A kind of waste lubricant oil by hydrogenation regeneration technology - Google Patents
A kind of waste lubricant oil by hydrogenation regeneration technology Download PDFInfo
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- CN106190238A CN106190238A CN201610659091.9A CN201610659091A CN106190238A CN 106190238 A CN106190238 A CN 106190238A CN 201610659091 A CN201610659091 A CN 201610659091A CN 106190238 A CN106190238 A CN 106190238A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
- C10G45/12—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/03—Catalysts comprising molecular sieves not having base-exchange properties
- B01J29/0308—Mesoporous materials not having base exchange properties, e.g. Si-MCM-41
- B01J29/0341—Mesoporous materials not having base exchange properties, e.g. Si-MCM-41 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/041—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41
- B01J29/045—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
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- 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
- C10M175/0016—Working-up used lubricants to recover useful products ; Cleaning with the use of chemical agents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
- B01J2229/183—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself in framework positions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
- B01J2229/186—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/10—Lubricating oil
Abstract
The invention discloses a kind of waste lubricating oil base oil hydrogenation regeneration technology, described technique includes pretreatment unit, hydrogenation regeneration unit and separative element, described hydrogenation regeneration unit uses fixed bed reactors, fixed bed reactors are filled with hydrogenation catalyst, described catalyst includes that carrier and active component, described carrier are incorporation hetero atom Co in synthetic bone shelf structure2+KIT 1, described active component for nitridation two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and the mixture of tungsten carbide wc.The reaction condition of described fixed bed reactors is: reaction temperature is 280 370 DEG C, reaction pressure 3 8MPa, hydrogen to oil volume ratio 40 50, volume space velocity 0.5 2.5h‑1.Reclaimed oil total sulfur content can be controlled less than 5ppm by this technique, controls total nitrogen content therein within 10ppm simultaneously.
Description
Technical field
The present invention relates to a kind of process for regeneration of waste lubricating oil, be specifically related to a kind of useless lubrication using special catalyst to carry out
Oil hydrogenation regeneration technology.
Background technology
In the epoch of this intense industrialization, the various vehicles and the extensive application of machinery, expedite the emergence of the extensive of lubricating oil
Application.Lubricating oil can effectively reduce or remove the phase mutual friction between vehicles mechanical accessory, and it extensively should
Minimizing sliding friction field for mechanical fitting, machine tool and other spare parts of engine, industrial equipment and factory.Lubricating oil
After used a period of time, the high temperature produced due to work and mechanical shearing, aoxidize and use the foreign body etc. that environment produces, moisten
Lubricating oil gradually loses lubricating function, it is necessary to replace with new lubricating oil.The used greasy property that this cyclic process produces
The lubricating oil reduced, the most referred to as waste lubricating oil.
China is the second-biggest-in-the-world lubricating oil country of consumption being only second to the U.S., and China's lubricating oil aggregate demand in 2010 is 490-
5100000 tons, it is contemplated that to the year two thousand twenty, lubricating oil aggregate demand is 600-800 ten thousand tons.The annual waste lubricating oil produced is the most big, as
Fruit is discarded in environment, can cause serious environmental pollution, it is therefore necessary to waste lubricating oil is carried out reclaiming.
Worldwide, the development of Technology of Used Lube Oil Regeneration substantially experienced by sour soil method → without acid system → hydrogenation
The process of method.The technique of main flow is distillation-hydrogenation method at present.
Distillation-hydrogenation method is the most representative with the technique of Puralube (German) limited company.The flow process of this technique
As follows:
1) pretreatment, in high temperature and high pressure environment, is sufficiently mixed hot hydrogen with raw oil, then sequentially enters flash distillation-steaming
Evaporate knockout tower, make the mink cell focus rich in asphalitine and metal and lubricating oil and light Component seperation.The Colophonium that sub-argument goes out is after treatment
Can be used as Colophonium blend component.It is to be exactly one to face hydrogen-deasphalting process that this unit operates it, it is therefore an objective to add the useless lubrication of heat damage
Additive component in oil, and additive, asphalitine, metal and other solid impurities are separated from waste lubricating oil, with
It is processed further remaining ingredient processing.
2) catalytic hydrogenation.Specially designed antigravity system comprises two reaction under high pressure rooms, the first reative cell (also known as
" protection reative cell ") remove the metal failing in pretreatment to completely remove, also function to the effect of preliminary desulfurization simultaneously.Second reaction
In room, catalyst is fully contacted with alkene key molecule and the aromatic hydrocarbons key molecule of lubricating oil, makes hydrogenation reaction quickly carry out, rises simultaneously
To complete desulfurization removing nitric effect.
3) finished product separates and product processes and reuse.Product is admitted to height-low pressure separator, through high-temperature pressure-reduction and
Low-temperature reduced-pressure, at the by-product that the catalytic hydrogenation stage produces, such as chloride and sulfide, is admitted to together with unreacted hydrogen
Alkali-water wash system, is neutralized reaction, chloride and sulfide and is removed, and remaining hydrogen is purified and recycles.?
The lubricating oil produced in reaction enters stripping-distillation column and carries out fractional distillation, obtains Petroleum, diesel oil and lube cut, at the bottom of tower
Residue returns the distillation column freshening of pretreatment stage.
But in above-mentioned technique, in catalytic hydrogenation unit, the catalyst desulfurizing denitrogenation degree of depth of employing is limited, can only be by total sulfur
Content is removed to about 100ppm, it is impossible to total sulfur content is reduced to 10ppm even below 5ppm.The most how to provide a kind of useless
Lube base oil hydrogenation regeneration technology, can effectively control the sulfur content in lubricating oil at 10ppm in desulfurization removing nitric unit
Hereinafter, to meet standard, can effectively remove nitride therein simultaneously, and realize the regeneration of waste lubricating oil, be that this area faces
A difficult problem.
Summary of the invention
It is an object of the invention to propose a kind of waste lubricant oil by hydrogenation regeneration technology, this technique can be by waste lubricant oil by hydrogenation
Regeneration, and the total sulfur content of reclaimed oil is reduced to below 10ppm, meanwhile, also making of the catalyst that this technique uses
In reclaimed oil, the removing ratio of nitride is more significant.
For reaching this purpose, the present invention by the following technical solutions:
A kind of non-lubricated oil hydrogenation regeneration technology, described technique includes pretreatment unit, hydrogenation regeneration unit and separates single
Unit.
Described hydrogenation regeneration unit uses fixed bed reactors, is filled with hydrogenation catalyst in fixed bed reactors, described
Catalyst includes carrier and active component.Described carrier is incorporation hetero atom Co in synthetic bone shelf structure2+KIT-1.Described work
Property component for nitridation two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and the mixture of tungsten carbide wc.Described fixed bed reactors
Reaction condition is: reaction temperature is 280-370 DEG C, reaction pressure 3-8MPa, hydrogen to oil volume ratio 40-50, volume space velocity 0.5-
2.5h-1。
In the present invention, not having particular/special requirement for pretreatment unit, it can use existing equipment and technique, such as
Flash distillation-separated equipment, to realize the separation of mink cell focus, lubricating oil and lighter hydrocarbons.
Preferably, the pretreatment of the present invention is preferably carried out under hydroconversion condition, to realize Linqing heat treatment-deasphalting mesh
, thus by the additive heat resolve in waste lubricating oil.
Pretreated lubricating oil enters hydrofinishing unit.Described hydrofinishing unit uses fixed bed reactors, Gu
Being filled with hydrogenation catalyst in fixed bed reactor, described catalyst includes carrier and active component..
KIT-1 molecular sieve has one-dimensional channels and crosses each other to form three-dimensional disordered structure, and this structure is conducive to catalysis, absorption
During material transmission.Pure silicon mesopore molecular sieve KIT-1 has heat stability more more preferable than MCM-241, HMS and hydrothermally stable
Property.The present invention through in numerous mesoporous materials, such as KIT-1, KIT-6, MCM-22, MCM-36, MCM-48, MCM-49,
MCM56 etc., carry out contrast test selection, find that only KIT-1 can reach the goal of the invention of the present invention, and other mesoporous materials are all
Having such-and-such defect, there is the technical difficulty being difficult to overcome when being applied in the present invention, therefore the present invention selects to use
KIT-1 is as carrier basis.
Although pure silicon KIT-1 mesopore molecular sieve hydro-thermal performance is outstanding, but inventor's research is later discovered that, it adds
Hetero atom or surface are after chemical modification, and its hydrothermal stability obtains bigger raising.Therefore, it is modified by the present invention, with
Increase its catalysis activity.The approach that KIT-1 mesopore molecular sieve is modified is by the present invention: in KIT-1 building-up process, adds Co2+
Saline solution, before KIT-1 framework of molecular sieve structure is formed, by isomorphous substitution by Co2+Replace part backbone element thus embedding
Enter in the skeleton of molecular sieve, improve catalysis activity, absorption and the thermodynamic stability of KIT-1 mesopore molecular sieve on the whole
Can etc..
Although the method being modified KIT-1 mesopore molecular sieve or approach are a lot, inventor finds, the catalysis of the present invention
Agent can only use doping Co2+KIT-1 could realize sulfur content as carrier and control and the balance of loss of octane number, inventor tastes
Try to adulterate in KIT-1: Al3+、Fe3+、Zn2+、Ga3+In the ion at generation anionic surface center, find all to realize institute
State effect.Exchanged Cu by ion with another modified approach of inventor2+It is supported on KIT-1 inner surfaces of pores to compare, the present invention
Isomorphous substitution approach more stable.Although described mechanism is current and unclear, but this has no effect on the enforcement of the present invention, invention
People is according to well-known theory and it is experimentally confirmed that there is cooperative effect between itself and the active component of the present invention.
Described Co2+Doping in KIT-1 must control within specific content range, and its doping is with weight
Meter, for the 0.56%-0.75% of KIT-1 weight, such as 0.57%, 0.58%, 0.59%, 0.6%, 0.61%, 0.62%,
0.63%, 0.64%, 0.65%, 0.66%, 0.67%, 0.68%, 0.69%, 0.7%, 0.71%, 0.72%, 0.73%,
0.74 etc..
Inventor finds, outside this range, can cause drastically reducing of waste lubricating oil denitrogenation and desulfurized effect.More make us
Joyful, work as Co2+When doping in KIT-1 controls in the range of 0.63%-0.72%, its desulphurizing ability is the strongest, when
Draw with Co2+Doping is transverse axis, and during curve chart with target desulfurized effect as the longitudinal axis, in this content range, sulfur content can control
Within the scope of extremely low, its desulfurized effect produced, far beyond expection, belongs to unforeseeable technique effect.
The total content of described active component is the 1%-15% of carrier KIT-1 weight, preferably 3-12%, further preferred 5-
10%.Such as, described content can be 2%, 2.5%, 3%, 3.5%, 4%, 4.5%, 5%, 5.5%, 6%, 6.5%,
7%, 7.5%, 8%, 8.5%, 9%, 9.5%, 10%, 10.5%, 11%, 11.5%, 12%, 12.5%, 13%,
13.5%, 14%, 14.5% etc..
In the present invention, it is particularly limited to active component for nitridation two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and tungsten carbide wc
Mixed proportion, inventor find, the effect that different mixed proportions reaches is entirely different.Inventor finds, nitrogenizes two molybdenums
MO2N, tungsten nitride W2N, molybdenum carbide Mo2The mixed proportion (mol ratio) of C and tungsten carbide wc is 1:(0.4-0.6): (0.28-
0.45): (0.8-1.2), nitridation two molybdenum MO are only controlled2N, tungsten nitride W2N, molybdenum carbide Mo2The mol ratio of C and tungsten carbide wc exists
In the range of Gai, sulfur content in lube base oil can be realized and control at below 10ppm and denitrification ability notable.Namely
Saying, four kinds of active components of the present invention are only 1:(0.4-0.6 in mol ratio): (0.28-0.45): time (0.8-1.2), just tool
Standby cooperative effect.Outside this molar ratio range, or omit or replace any one component, all can not realize collaborative effect
Should.
Preferably, two molybdenum MO are nitrogenized2N, tungsten nitride W2N, molybdenum carbide Mo2The mol ratio of C and tungsten carbide wc is 1:(0.45-
0.5): (0.35-0.45): (0.8-1.0), more preferably 1:(0.45-0.48): (0.4-0.45): (0.9-1.0),
Preferably 1:0.48:0.42:0.95.
The preparation method of described catalyst can take infusion process and other alternative methods, the people in the art of routine
The prior art unrestricted choice that member can grasp according to it, the present invention repeats no more.The typical but non-limiting example of the present invention
As follows:
Sodium silicate, cetyl trimethylammonium bromide (CTAB), sodium ethylene diamine tetracetate (EDTA) and distilled water are massaged
You mix the ratio than 1:0.25:1:60, load with in teflon-lined autoclave pressure, after stirring under 373K
Constant temperature 24h, the pH of re-adjustments mixture are 10.5, after constant temperature 4 times, take out product, with distilled water cyclic washing to filtrate
PH=7, then under 373K, constant temperature overnight, obtains the KIT-1 with surfactant.KIT-1 with surfactant is existed
Roasting 1.5h under 523K, then roasting 6h in air atmosphere under 813K, obtains KIT-1 powder body.By this powder body 0.1mol/L
Salpeter solution carry out pickling (control solid-to-liquid ratio is 1:10), under room temperature stir 0.5h, filter, be washed with distilled water to filtrate
Dry under pH=7,373K and obtain matrix KIT-1 molecular sieve.
Preferably, the reaction condition of described fixed bed reactors is: reaction temperature is 320-340 DEG C, reaction pressure 4-
6MPa, hydrogen to oil volume ratio 40-50, volume space velocity 1.5-2.0h-1。
Preferably, described hydrofining technology flow process includes, after mixing from the lubricating oil of pretreatment with hydrogen, through optional
Heat exchanger heat exchange, then enter fixed bed reactors after the heating of heated stove and be fixed a reactor, product enters point
From unit.
Preferably, described hydrogenation desulfurization and denitrogenation fixed bed reactors include 1-5 beds, further preferred 2-3
Individual beds.
The separative element of the present invention does not the most do specific restriction, its objective is to realize hydrogen and reclaims, obtain reclaimed oil and
Other by-products.Typical but non-limiting example includes, is introduced into depressurized system from hydrorefined product and reduces pressure,
Realize gas-liquid separation.Gas-phase product returns hydrofinishing unit through alkali cleaning, and liquid phase enters stripping-distillation column and carries out fractional distillation, tower top
Obtaining Petroleum, side line respectively obtains diesel oil and lubricating oil, heavy oil and residue and discharges from the bottom of tower.This separative element is all known skill
Art, the application does not do specific detailed restriction.
Through the lubricating oil that the waste lubricant oil by hydrogenation regeneration technology of the present invention obtains, according to the requirement of technique, can arrange
Different side lines obtains the lube base oil of various criterion, and this arranges and can realize by adjusting the side stream temperature of distillation column,
The present invention repeats no more.
The waste lubricant oil by hydrogenation regeneration technology of the present invention is by choosing specific catalyst, and described catalyst is miscellaneous by mixing
Atom Co2+KIT-1 as carrier, and choose the nitridation two molybdenum MO of special ratios2N, tungsten nitride W2N, molybdenum carbide Mo2C and carbon
Change tungsten WC as active component so that this catalyst produces cooperative effect, and the hydrodesulfurization to reclaimed oil can control always
Sulfur content is less than 5ppm, controls the total nitrogen content in reclaimed oil within 10ppm simultaneously.
Detailed description of the invention
The waste lubricant oil by hydrogenation regeneration technology of the present invention is illustrated by the present invention by following embodiment.
Embodiment 1
Preparing catalyst by infusion process, carrier is doping Co2+KIT-1, Co2+Doping control in KIT-1
System is at the 0.65% of carrier quality.Described active component nitrogenizes two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and tungsten carbide wc
Total content is the 10% of carrier quality, and its mol ratio is 1:0.4:0.3:0.8.
Described Catalyst packing enters fixed bed reactors, and the reaction tube of described reactor is by the stainless steel of internal diameter 50mm
Becoming, beds is set to 3 layers, and reaction bed temperature UGU808 type temp controlled meter is measured, and raw material waste lubricating oil is by north
The double plunger micro pump of capital satellite manufactory manufacture carries continuously, and hydrogen is supplied and use Beijing Sevenstar-HC D07-by gas cylinder
11A/ZM mass-flow gas meter coutroi velocity, loaded catalyst is 2kg.Reacted product is laggard through the cooling of water-bath room temperature
Row gas-liquid separation.
Raw materials used is the useless 5W30 lubricating oil from Great Wall.
Raw material is the most preprocessed, and flash distillation-separated equipment is passed through in this pretreatment, it is achieved mink cell focus, lubricating oil and lighter hydrocarbons
Separation.Described pretreatment is carried out under hydroconversion condition, to realize Linqing heat treatment-deasphalting purpose, thus by useless lubrication
Additive heat resolve in oil.
Pretreated lubricating oil enters hydrofinishing unit.Described hydrofinishing unit uses fixed bed reactors, Gu
Fixed bed reactor is filled with described Hydrobon catalyst.The reaction condition controlling fixed bed reactors is: reaction temperature is
320 DEG C, reaction pressure 4MPa, hydrogen to oil volume ratio 50, volume space velocity 1.5h-1。
The product of hydrogenated reaction enters depressurized system and reduces pressure, it is achieved gas-liquid separation.Gas-phase product returns through alkali cleaning
Hydrofinishing unit, liquid phase enters stripping-distillation column and carries out fractional distillation, and tower top obtains Petroleum, and side line respectively obtains diesel oil and profit
Lubricating oil, heavy oil and residue are discharged from the bottom of tower.
The lube product that test finally gives, total sulfur content is reduced to 3ppm, and total alkaline nitrogen content is reduced to 7ppm.
Embodiment 2
Preparing catalyst by infusion process, carrier is doping Co2+KIT-1, Co2+Doping control in KIT-1
System is at the 0.7% of carrier quality.Described active component nitrogenizes two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and tungsten carbide wc
Total content is the 10% of carrier quality, and its mol ratio is 1:0.6:0.45): 1.2.
Remaining condition is same as in Example 1.
Testing final product, total sulfur content is reduced to 3ppm, and total alkaline nitrogen content is reduced to 9ppm.
Comparative example 1
The carrier of embodiment 1 is replaced with γ-Al2O3, remaining condition is constant.
Testing final product, total sulfur content is reduced to 41pm, and total alkaline nitrogen content is reduced to 57ppm.
Comparative example 2
The carrier of embodiment 1 is replaced with unadulterated KIT-1, and remaining condition is constant.
Testing final product, total sulfur content is reduced to 37ppm, and total alkaline nitrogen content is reduced to 56ppm.
Comparative example 3
Co by embodiment 12+Replace with Zn2+, remaining condition is constant.
Testing final product, total sulfur content is reduced to 37ppm, and total alkaline nitrogen content is reduced to 54ppm.
Comparative example 4
By the Co in embodiment 12+Doping in KIT-1 controls at the 0.5% of carrier quality, and remaining condition is constant.
Testing final product, total sulfur content is reduced to 42ppm, and total alkaline nitrogen content is reduced to 57ppm.
Comparative example 5
By the Co in embodiment 12+Doping in KIT-1 controls at the 0.8% of carrier quality, and remaining condition is constant.
Testing final product, total sulfur content is reduced to 39ppm, and total alkaline nitrogen content is reduced to 55ppm.
Embodiment 1 shows with comparative example 1-5, certain content scope that the application uses and certain loads metal ion
KIT-1 carrier, when replacing with other known carriers of this area, or carrier is identical but Co2+During doping difference, all reach not
To the technique effect of the present invention, the therefore Co of the certain content scope of the present invention2+Doping KIT-1 carrier and other components of catalyst
Between possess cooperative effect, described hydrogenation desulfurization and denitrogenation unit creates unforeseeable technique effect.
Comparative example 6
Omit the MO in embodiment 12N, remaining condition is constant.
Testing final product, total sulfur content is reduced to 47ppm, and total alkaline nitrogen content is reduced to 60ppm.
Comparative example 7
Omitting the WC in embodiment 1, remaining condition is constant.
Testing final product, total sulfur content is reduced to 49ppm, and total alkaline nitrogen content is reduced to 58ppm.
Above-described embodiment and comparative example 6-7 explanation, several active component of catalyst of the hydrodesulfurization of the present invention it
Between there is specific contact, be omitted or substituted one of which or several, all can not reach the certain effects of the application, it was demonstrated that it produces
Give birth to cooperative effect.
Applicant states, the present invention illustrates the technique of the present invention by above-described embodiment, but the invention is not limited in
Above-mentioned technique, does not i.e. mean that the present invention has to rely on above-mentioned detailed catalysts and could implement.Those of skill in the art
Member is it will be clearly understood that any improvement in the present invention, and the equivalence of raw material each to product of the present invention is replaced and the interpolation of auxiliary element, tool
Body way choice etc., within the scope of all falling within protection scope of the present invention and disclosure.
Claims (6)
1. a waste lubricating oil base oil hydrogenation regeneration technology, described technique includes pretreatment unit, hydrogenation regeneration unit and divides
From unit, it is characterised in that
Described hydrogenation regeneration unit uses fixed bed reactors, is filled with hydrogenation catalyst, described catalysis in fixed bed reactors
Agent includes that carrier and active component, described carrier are incorporation hetero atom Co in synthetic bone shelf structure2+KIT-1, described activity group
It is divided into nitridation two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and the mixture of tungsten carbide wc, the reaction of described fixed bed reactors
Condition is: reaction temperature is 280-370 DEG C, reaction pressure 3-8MPa, hydrogen to oil volume ratio 40-50, volume space velocity 0.5-2.5h-1。
It is hydrogenated with regeneration technology the most as claimed in claim 1, it is characterised in that hetero atom Co2+Doping be KIT-1 weight
0.63%-0.72%.
It is hydrogenated with regeneration technology the most as claimed in claim 1, it is characterised in that the total content of described active component is carrier KIT-
The 3-12% of 1 weight, preferably 5-10%.
It is hydrogenated with regeneration technology the most as claimed in claim 1, it is characterised in that nitrogenize two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide
Mo2The mol ratio of C and tungsten carbide wc is 1:(0.45-0.5): (0.35-0.45): (0.8-1.0), more preferably 1:
(0.45-0.48): (0.4-0.45): (0.9-1.0), most preferably 1:0.48:0.42:0.95.
It is hydrogenated with regeneration technology the most as claimed in claim 1, it is characterised in that the reaction condition of described fixed bed reactors is:
Reaction temperature is 320-340 DEG C, reaction pressure 4-6MPa, hydrogen to oil volume ratio 40-50, volume space velocity 1.5-2.0h-1。
It is hydrogenated with regeneration technology the most as claimed in claim 1, it is characterised in that described fixed bed reactors include 1-5 catalysis
Agent bed, preferably includes 2-3 beds.
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