CN106085501A - A kind of hydrorefining basic oil lubricating oil technique - Google Patents
A kind of hydrorefining basic oil lubricating oil technique Download PDFInfo
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- CN106085501A CN106085501A CN201610669652.3A CN201610669652A CN106085501A CN 106085501 A CN106085501 A CN 106085501A CN 201610669652 A CN201610669652 A CN 201610669652A CN 106085501 A CN106085501 A CN 106085501A
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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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
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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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- 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
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
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- Crystallography & Structural Chemistry (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of hydrorefining basic oil lubricating oil technique, described technique includes solvent refining unit, hydrogenation desulfurization and denitrogenation unit and hydrofinishing unit, described hydrogenation desulfurization and denitrogenation unit uses fixed bed reactors, being 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+MCM 41.Described active component is 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 350 370 DEG C, reaction pressure 9 11MPa, hydrogen to oil volume ratio 300 600, volume space velocity 1.0 2.5h‑1.Lube base oil total sulfur content can be controlled, less than 5ppm, to control the total nitrogen content in base oil within 10ppm by this technique simultaneously.
Description
Technical field
The present invention relates to a kind of lube base oil processing technique, be specifically related to a kind of profit using special catalyst to carry out
Lubricant base oil hydrofining technology.
Background technology
The raising of lube product quality, it is desirable to base oil has a higher Viscosity Index, less evaporation loss, more preferably
Oxidation stability and low temperature flow.Such as in order to produce, the 5W meeting GF-2 and G-3 standard is oily or long-life automatic biography
Hydrodynamic, it is necessary to use some or all of II class meeting API base oil criteria for classification or III class base oil, and with conventional
It is to use hydrogenation work that solvent refining I class base oil then cannot modulate this up-to-standard series products, II class and III class base oil
Skill produces, and its quality index is: saturated hydrocarbons mass fraction is all higher than 90%, and sulfur nutrient is respectively less than 0.03%；In viscosity
Index aspect, II class is 80-120, and Group III is more than 120.
The companies such as Exxon develop a kind of group technology combined by lubricating oil solvent with hydrotreating, i.e.
By the charging of hydrotreater, first pass through solvent refining to reduce the nitride in charging and condensed-nuclei aromatics content.Owing to changing
Being apt to feedstock quality, hydrotreating can be carried out under the temperature and pressure relatively relaxed.The most not only can improve the viscous of base oil
Degree index, and viscosity loss is little, and light stability is good.Further, since hydroprocessing condition compares mitigation, the knot of paraffin in raw material
Structure seldom wrecks, therefore. and during obtained hydrogenated oil solvent dewaxing, its filtering property connects with solvent-refined oil very much
Closely, the hydrogenated oil obtained by distillate direct hydrogenation processes, during solvent dewaxing, the rate of filtration is the slowest. need to add
Add filter aid to improve the dewaxing rate of filtration.Due to the existing solvent refining unit in most of refineries, therefore this technique is used only to need to increase
Add a set of medium pressure hydrogenation treatment facility, just can go out high viscosity index (HVI) base oil from low-quality crude oil production, have and require less investment while yielding quicker results
Feature.
In order to preferably improve the product quality of solvent refining-hydrotreating group technology, Exxon company and stone section of China
Institute all have employed the hydrogen addition technology of multiple reactors in series.In the RHC technique of Exxon exploitation, it is provided with three reactors, first
Individual reactor selects harsher hydroconversion condition, it is therefore an objective to improving the viscosity index (VI) of product, second reactor is to overcome
The thermodynamical equilibrium restriction to aromatic hydrogenation, selects the operation temperature lower than first reactor, is beneficial to aromatic hydrogenation, the
One, two reactor fillings is all the KF-840 nickel-molybdenum catalyst not having acidity, and the 3rd reactor filling is then hydrogenation activity
Strong catalyst, it is therefore an objective to reduce the carcinogen in oil product and improve the light stability of product. thus obtained it is hydrogenated to
Oil, after distillation excision light oil, carries out solvent dewaxing to reduce its pour point.This technique in 1999 Exxon-Mobil's
Baytown refinery puts into commercial production.
Solvent refining-hydrotreating group technology the RHT of Shi Ke institute of China exploitation.Being provided with two reactors, first anti-
Answer that device loads is to have high desulfurization, denitrogenation and the tungsten-Raney nickel RL-1 of hydrogenation open-loop performance.Second reactor filling
Be have the saturated performance of high aromatic hydrogenation, do not have acidity catalyst build RJW-2, according to a set of working ability of this technology building
Lube oil hydrogenation processing means for 20Mt/a is constructed and put into operation in Jingmen general petrochemical works November calendar year 2001.
But in above-mentioned technique, in desulfurization removing nitric unit, using Ni-Mo or Ni-W catalyst, wherein Ni belongs to noble metal,
Price is higher, and secondly the above-mentioned catalyst desulfurizing denitrogenation degree of depth is limited, it is impossible to total sulfur content is removed to below 10ppm.The most such as
What provides a kind of hydrorefining basic oil lubricating oil technique, can be effectively by the sulfur in lube base oil in desulfurization removing nitric unit
Content controls at below 10ppm, to meet standard, simultaneously can effectively remove nitride therein, is face one of this area
A difficult problem.
Summary of the invention
It is an object of the invention to propose a kind of hydrorefining basic oil lubricating oil technique, this technique can will lubricate oil base
Total sulfur content in plinth oil is reduced to below 10ppm, to meet lubricating oil standard.Meanwhile, going back of the catalyst that this technique uses
The removing ratio making nitride in base oil is more significant.
For reaching this purpose, the present invention by the following technical solutions:
A kind of hydrorefining basic oil lubricating oil technique, described technique includes solvent refining unit, hydrogenation desulfurization and denitrogenation list
Unit and hydrofinishing unit.
Described hydrogenation desulfurization and denitrogenation 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+MCM-41.Institute
State active component for nitridation two molybdenum MO2N, tungsten nitride W2N, molybdenum carbide Mo2C and the mixture of tungsten carbide wc.Described fixed bed reaction
The reaction condition of device is: reaction temperature is 350-370 DEG C, reaction pressure 9-11MPa, hydrogen to oil volume ratio 300-600, volume space velocity
1.0-2.5h-1。
In the present invention, not having particular/special requirement for solvent refining unit, it can use existing equipment and technique, this
Specific restriction is not done in invention.
Typical but non-limiting solvent refining unit generally comprises extraction and solvent recovery two parts.With furfural treatment it is
Example, raw material inversely contacts, in certain temperature (in extraction tower (in the past with packed column, use rotating disc column in the recent period) with furfural
As be 60～130 DEG C) with solvent ratio (generally 1～4:1) under the conditions of, be divided into biphase.Undesirable components is present in the extraction of bottom
Taking in liquid, in order to both ensure raffinate oil quality, the most do not reduce productivity, extraction tower should keep higher tower top temperature and relatively low tower
End temperature (the general temperature difference is 20～50 DEG C).Raw material needs before entering extraction tower to remove air, in order to avoid furfural oxidation.Furfural enters extraction tower
Before need drying, in order to avoid reducing its solvability.
Raffinate contains furfural less, use flush distillation and stripping to reclaim furfural；Extract contains furfural more, use
Multiple-effect evaporation and stripping reclaim furfural to reduce energy consumption.The heat stability of furfural is poor, thus the heating-up temperature of solvent recovery is not
Should be more than 230 DEG C.
The recovery process of aqueous furfural, formulates according to following feature, i.e. the azeotropic mixture steam of furfural and water condenses also
After being cooled to uniform temperature, the water-soluble liquid phase containing a small amount of furfural and the furfuryl aldehyde solution phase containing a small amount of water can be divided into.
MCM-41 is ordered into mesoporous material, and its duct is that six side's ordered arrangement, size are uniform, aperture size can with synthesis time
The difference adding directed agents and synthetic parts changes between 1.5～10nm, lattice parameter about 4.5nm, specific pore volume about 1mL/g,
MCM-41 uniform pore diameter, has higher specific surface area (1000m2/ g) and big adsorption capacity (0.7mL/g), the most organic
The free diffusing of molecule.The present invention through in numerous mesoporous materials, such as MCM-22, MCM-36, MCM-48, MCM-49,
MCM56, carries out contrast test selection, finds that only MCM-41 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
MCM-41 is as carrier basis.
The acidity of silica MCM-41 own is the most weak, is directly used as catalyst activity relatively low.Therefore, it is changed by the present invention
Property, to increase its catalysis activity.The approach that MCM-41 mesopore molecular sieve is modified is by the present invention: in MCM-41 building-up process,
Add Co2+Saline solution, before MCM-41 framework of molecular sieve structure is formed, by isomorphous substitution by Co2+Replace part skeleton unit
Element thus embed in the skeleton of molecular sieve, improve on the whole MCM-41 mesopore molecular sieve catalysis activity, absorption and heat
Mechanical stability can wait.
Although the method being modified MCM-41 mesopore molecular sieve or approach are a lot, inventor finds, the present invention urges
Agent can only use doping Co2+MCM-41 could realize sulfur content as carrier and control and the balance of loss of octane number, invention
People has attempted adulterating in MCM-41: Al3+、Fe3+、Zn2+、Ga3+In the ion at generation anionic surface center, find all can not
Realize described effect.Exchanged Cu by ion with another modified approach of inventor2+It is supported on MCM-41 inner surfaces of pores to compare,
The isomorphous substitution approach of the present invention is more stable.Although described mechanism is current and unclear, but this has no effect on the reality of the present invention
Executing, inventor 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 MCM-41 must control within specific content range, and its doping is with weight
Meter, for the 0.56%-0.75% of MCM-41 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 lubricant base-oil denitrification and desulfurized effect.More
Pleasurable, work as Co2+When doping in MCM-41 controls in the range of 0.63%-0.72%, its desulphurizing ability is
By force, when drawing with Co2+Doping is transverse axis, during curve chart with target desulfurized effect as the longitudinal axis, and sulfur content in this content range
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 MCM-41 weight, preferably 3-12%, further preferably
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.
Preferably, the reaction condition of described fixed bed reactors is: reaction temperature is 360-370 DEG C, reaction pressure 10-
10.5MPa, hydrogen to oil volume ratio 400-600, volume space velocity 1.5-2.0h-1。
Preferably, described desulfurization removing nitric technological process includes, mixes from solvent-refined lube base oil with hydrogen
After, through optional heat exchanger heat exchange, then after the heating of heated stove, entrance fixed bed reactors carry out hydrogenation desulfurization and denitrogenation, and reaction is produced
Thing separates through gas-liquid separation tower.Optionally, gas phase returns and mixes with base oil and hydrogen, and liquid phase enters follow-up hydrofinishing list
Unit.
Preferably, described hydrogenation desulfurization and denitrogenation fixed bed reactors include 1-5 beds, further preferred 2-3
Individual beds.
The hydrofinishing unit of the present invention does not the most do specific restriction, its objective is to realize hydrogenation saturated, it is achieved base oil is pacified
Improve qualitatively.These techniques are all known, and the application does not do specific restriction.
The hydrogenation desulfurization and denitrogenation technique of the present invention is by choosing specific catalyst, and described catalyst is by mixing hetero atom
Co2+MCM-41 as carrier, and choose the nitridation two molybdenum MO of special ratios2N, tungsten nitride W2N, molybdenum carbide Mo2C and carbonization
Tungsten WC is as active component so that this catalyst produces cooperative effect, and the hydrodesulfurization to lube base oil can control always
Sulfur content is less than 5ppm, controls the total nitrogen content in lube base oil within 10ppm simultaneously.
Detailed description of the invention
The hydrogenation desulfurization and denitrogenation technique of the present invention is illustrated by the present invention by following embodiment.
Embodiment 1
Preparing catalyst by infusion process, carrier is doping Co2+MCM-41, Co2+Doping in MCM-41
Control 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 carrier quality 10%, 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 base oil is by Beijing
The double plunger micro pump of 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 for the lube base oil from decompression distillation three lines (be commonly called as subtracting three line).
Raw material first passes through furfural treatment unit, and then the hydrogenation desulfurization and denitrogenation unit of the entrance present invention, controls hydrodesulfurization
Denitrification reaction condition is: temperature 360 DEG C, reaction pressure 10MPa, hydrogen to oil volume ratio 500, volume space velocity 2h-1.Subsequently enter hydrogenation
Refined unit, hydrofinishing unit uses the catalyst RJW-2 of Beijing Shi Keyuan, and controlling hydrogenation temperature is 280 DEG C.
Testing final product, total sulfur content is reduced to 2ppm, and total alkaline nitrogen content is reduced to 6ppm.
Embodiment 2
Preparing catalyst by infusion process, carrier is doping Co2+MCM-41, Co2+Doping in MCM-41
Control 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 carrier quality 10%, 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 7ppm.
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 26ppm, and total alkaline nitrogen content is reduced to 42ppm.
Comparative example 2
The carrier of embodiment 1 is replaced with unadulterated MCM-41, and remaining condition is constant.
Testing final product, total sulfur content is reduced to 21ppm, and total alkaline nitrogen content is reduced to 28ppm.
Comparative example 3
Co by embodiment 12+Replace with Zn2+, remaining condition is constant.
Testing final product, total sulfur content is reduced to 29ppm, and total alkaline nitrogen content is reduced to 46ppm.
Comparative example 4
By the Co in embodiment 12+Doping in MCM-41 controls at the 0.5% of carrier quality, and remaining condition is constant.
Testing final product, total sulfur content is reduced to 31ppm, and total alkaline nitrogen content is reduced to 43ppm.
Comparative example 5
By the Co in embodiment 12+Doping in MCM-41 controls at the 0.8% of carrier quality, and remaining condition is constant.
Testing final product, total sulfur content is reduced to 23ppm, and total alkaline nitrogen content is reduced to 44ppm.
Embodiment 1 shows with comparative example 1-5, certain content scope that the application uses and certain loads metal ion
MCM-41 carrier, when replacing with other known carriers of this area, or carrier is identical but Co2+During doping difference, all reach
Less than the technique effect of the present invention, the therefore Co of the certain content scope of the present invention2+Doping MCM-41 carrier and catalyst other
Possessing cooperative effect between component, 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 37ppm, and total alkaline nitrogen content is reduced to 48ppm.
Comparative example 7
Omitting the WC in embodiment 1, remaining condition is constant.
Testing final product, total sulfur content is reduced to 39ppm, and total alkaline nitrogen content is reduced to 46ppm.
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 hydrorefining basic oil lubricating oil technique, described technique includes solvent refining unit, hydrogenation desulfurization and denitrogenation unit
With hydrofinishing unit, it is characterised in that
Described hydrogenation desulfurization and denitrogenation unit uses fixed bed reactors, is filled with hydrogenation catalyst in fixed bed reactors, described
Catalyst includes that carrier and active component, described carrier are incorporation hetero atom Co in synthetic bone shelf structure2+MCM-41, 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 350-370 DEG C, reaction pressure 9-11MPa, hydrogen to oil volume ratio 300-600, volume space velocity 1.0-
2.5h-1。
2. hydrofining technology as claimed in claim 1, it is characterised in that hetero atom Co2+Doping be MCM-41 weight
0.63%-0.72%.
3. hydrofining technology as claimed in claim 1, it is characterised in that the total content of described active component is carrier MCM-
The 3-12% of 41 weight, preferably 5-10%.
4. hydrofining technology 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.
5. hydrofining technology as claimed in claim 1, it is characterised in that the reaction condition of described fixed bed reactors is:
Reaction temperature is 360-370 DEG C, reaction pressure 10-10.5MPa, hydrogen to oil volume ratio 400-600, volume space velocity 1.5-2.0h-1。
6. hydrofining technology 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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| CN106523113A (en) * | 2016-11-10 | 2017-03-22 | 无锡市明盛强力风机有限公司 | Automobile exhaust pipe with purification effect and production method thereof |
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