CN106190247A - A kind of aerial kerosene hydrofining technology - Google Patents

A kind of aerial kerosene hydrofining technology Download PDF

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Publication number
CN106190247A
CN106190247A CN201610668155.1A CN201610668155A CN106190247A CN 106190247 A CN106190247 A CN 106190247A CN 201610668155 A CN201610668155 A CN 201610668155A CN 106190247 A CN106190247 A CN 106190247A
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fixed bed
mcm
bed reactors
molybdenum
hydrogen
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朱忠良
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Xishan Lvchun Plastic Products Factory
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Xishan Lvchun Plastic Products Factory
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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
    • 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
    • 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
    • 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
    • B01J2229/20—After treatment, characterised by the effect to be obtained to introduce other elements in the catalyst composition comprising the molecular sieve, but not specially in or on the molecular sieve itself
    • 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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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Dispersion Chemistry (AREA)
  • Materials Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention discloses a kind of aerial kerosene hydrofining technology, described technique uses fixed bed reactors, is filled with hydrogenation desulfurization and denitrogenation catalyst in fixed bed reactors, and 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 260 320 DEG C, and hydrogen dividing potential drop is 2.8 3.6MPa, hydrogen to oil volume ratio 150 250, volume space velocity 2.0 4.0h‑1.Aerial kerosene total sulfur content can be controlled, less than 5ppm, to control the total nitrogen content in aerial kerosene within 10ppm by this technique simultaneously.

Description

A kind of aerial kerosene hydrofining technology
Technical field
The present invention relates to aerial kerosene hydrodesulfurization process for refining, be specifically related to a kind of boat using special catalyst to carry out Empty kerosene hydrogenation desulfuration purification technique.
Background technology
Aerial kerosene is one of oil product.English name Jet fuel No.3, calls jet fuel.Main by difference The hydrocarbon compound composition of fraction.Aerial kerosene is mainly used as the fuel of aero-turbine.
Along with transportation is increasingly stronger to Economic Stimulus effect, China's transportation cause development in recent years is swift and violent. From the point of view of the consumption figure of State Statistics Bureau's statistics, China's jet fuel consumption figure the whole year in 2008 is 1279.9 ten thousand tons, with The consumption figure of the same period in 2007 is compared and has been gone up 3.6%, and from the point of view of the import volume of customs statistics, China fires 2008 years jets Expecting import altogether 647.8 ten thousand tons, increased by 23.5% on a year-on-year basis, monthly import volume reaches 540,000 tons.
In the world always according to the standard of JETA-1, the quality of jet fuel being come requirement, this also becomes jet combustion in the world The standard criterion of material trade deal.Its total acid number of this standard-required (mgKOH/g) is not more than 0.015, and total sulfur content maximum must not More than 0.30wt%, i.e. cannot be greater than 30ppm, corrosive nature is also required by aerial kerosene simultaneously.Analysis of experiments shows, impact The main cause of boat coal silver slice corrosion is the elementary sulfur in active sulfide, and when its content reaches 2 μ g/g, boat coal silver slice corrosion is the most not Qualified, silver slice corrosion can be promoted with elementary sulfur when mercaptan and disulphide etc. coexist.
Along with heaviness, the in poor quality of world's crude oil are deepened day by day, crude oil sulfur content is more and more higher, and the lightweight of high-quality is former Oil is constantly reducing.The crude oil of refinery's processing in recent years mostly is imported crude oil, and relative density increases year by year, in several years of the beginning of this century The average density of whole world refinery processing crude oil rises to about 0.8633.The problem that sulfur content is high is the most extremely serious, the current world The yield of upper sour crude oil and sour crude accounts for more than the 75% of world's crude oil total output.20th century the mid-90 whole world refinery The crude oil average sulfur content of processing is 0.9%, and the beginning of this century has increased to 1.6%.
For producing the cleaning jet fuel (aerial kerosene) of high-quality, desulfurization technology obtains huge attention.Current desulfurization Technology, divides from the angle whether being hydrogenated with, is divided into hydrodesulfurization and non-hydrodesulfurization.Hydrodesulfurization technology is intrinsic excellent due to it Gesture becomes the technology of processing high grade fuel oil the most ripe.Compared to conventional process for refining, kerosene hydrogenation Technique decreases alkaline residue and hargil exhaust emission, and it is the most higher for the adaptability of raw material, and therefore hydrogenation technique is future development Main way.
The hydrogenation technique of current jet fuel (aerial kerosene) is similar, and typical technique is as follows: virgin kerosene is certainly Raw material tank field is sent into raw material surge tank, with kerosene raffinate heat exchange after feed pump boosts to about 3.0MPa, then mixes with hydrogen Again with product heat exchange.Enter charging heating furnace after mixed hydrogen raw material and product heat exchange to be heated to reacting temperature required entrance Hydrogenation reactor.Mixed hydrogen raw material carries out hydrogenation reaction under the effect of catalyst, enters after product and mixed hydrogen raw material heat exchange High pressure hot separator is isolated major part and is generated oil, high-pressure separator top oil gas priority and recycle hydrogen, cold high pressure separator base oil After heat exchange inject desalted water, then enter air cooler, water cooler be cooled to 40 DEG C enter cold high pressure separators isolate hydrogen.Cold anticyclone It is combined into stripper with high pressure hot separator base oil after separator oil and high pressure hot separator gas heat exchange.
But existing hydrofining technology is all to arrange for former high-quality edible vegetable oil.For current high sulfur content The virgin kerosene that crude oil production obtains, owing to its high sulfur content, its catalyst used and hydroconversion condition are all difficult to be suitable for, produces The setting that meets the requirements be reduce sulfur content to below 10ppm, can not be suitable for.
A kind of jet fuel (aerial kerosene) hydrodesulfurization is provided, can be effectively by the aviation of high sulfur content Sulfur content in kerosene controls at below 10ppm, with satisfied discharge and Corrosion standards, is a difficult problem facing of this area.
Summary of the invention
It is an object of the invention to propose a kind of aerial kerosene hydrodesulfurization process for refining, this technique can be by aerial kerosene In total sulfur content be reduced to below 10ppm, with satisfied discharge and Corrosion standards.
For reaching this purpose, the present invention by the following technical solutions:
A kind of aerial kerosene hydrofining technology, described technique uses fixed bed reactors, loads in fixed bed reactors Hydrogenation catalyst, described catalyst is had to include 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 260-320 DEG C, and hydrogen dividing potential drop is 2.8-3.6MPa, Hydrogen to oil volume ratio 150-250, volume space velocity 2.0-4.0h-1。
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 aerial kerosene desulfurized effect.More pleasurable It is to work as Co2+When doping in MCM-41 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 extremely low Within the scope of, 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 aerial kerosene can be realized and control at below 10ppm and denitrification ability notable.It is to say, this Four kinds of active components of invention are only 1:(0.4-0.6 in mol ratio): (0.28-0.45): time (0.8-1.2), just possess association Same effect.Outside this molar ratio range, or omit or replace any one component, all can not realize cooperative effect.
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 280-300 DEG C, and hydrogen dividing potential drop is 3.0- 3.4MPa, hydrogen to oil volume ratio 180-220, volume space velocity 2.0-4.0h-1。
Preferably, described technological process includes, virgin kerosene, after filter, surge tank, is pumped into heat exchanger by feed pump With product boat coal heat exchange, after heat exchange, it is mixed to form hydrogen oil mixture with recycle hydrogen and new hydrogen, again laggard with product heat exchange Enter heating furnace, be heated to reaction temperature and enter hydrofining reactor (fixed bed reactors), hydrogen oil mixture in the reactor Under catalyst action, the reaction such as carry out that hydrodesulfurization, denitrogenation, deoxidation, alkene is saturated and aromatic hydrocarbons is saturated, product is through changing Heat, more water cooled to predetermined temperature, enter high-pressure separator, high-pressure separator top gas phase returns recycle hydrogen as recycle hydrogen and delays Rushing tank, oil phase enters low pressure separator, and the generation oil drawn bottom low pressure separator enters stripper after product heat exchange, Tower top oil gas enters separatory tank after air cooling, water-cooled and obtains Petroleum, and stripping tower bottom obtains aerial kerosene.
Preferably, described fixed bed reactors include 1-5 beds, further preferred 2-3 beds.
The hydrofining technology 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 tungsten carbide wc As active component so that this catalyst produces cooperative effect, and the hydrodesulfurization to aerial kerosene can control at total sulfur content low In 5ppm, the total nitrogen content in aerial kerosene is controlled within 10ppm simultaneously.
Detailed description of the invention
The hydrofining 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+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 aerial kerosene 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 for virgin kerosene, its total sulfur content 267ppm, basic n content is 299ppm.
Controlling reaction condition is: temperature 300 DEG C, hydrogen dividing potential drop 3.2MPa, hydrogen to oil volume ratio 200, volume space velocity 2h-1。
Testing final product, total sulfur content is reduced to 2ppm, and total alkaline nitrogen content is reduced to 8ppm.
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 6ppm.
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 21ppm, and total alkaline nitrogen content is reduced to 32ppm.
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 32ppm, and total alkaline nitrogen content is reduced to 37ppm.
Comparative example 3
Co by embodiment 12+Replace with Zn2+, remaining condition is constant.
Testing final product, total sulfur content is reduced to 28ppm, and total alkaline nitrogen content is reduced to 39ppm.
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 33ppm, and total alkaline nitrogen content is reduced to 44ppm.
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 25ppm, and total alkaline nitrogen content is reduced to 37ppm.
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 hydrofining technology 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 34ppm, and total alkaline nitrogen content is reduced to 47ppm.
Comparative example 7
Omitting the WC in embodiment 1, remaining condition is constant.
Testing final product, total sulfur content is reduced to 38ppm, 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 hydrofining technology 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. an aerial kerosene hydrofining technology, described technique uses fixed bed reactors, is filled with in fixed bed reactors Hydrogenation catalyst, described catalyst includes carrier and active component, it is characterised in that
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 260-320 DEG C, and hydrogen dividing potential drop is 2.8-3.6MPa, hydrogen oil Volume ratio 150-250, volume space velocity 2.0-4.0h-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 280-300 DEG C, and hydrogen dividing potential drop is 3.0-3.4MPa, hydrogen to oil volume ratio 180-220, volume space velocity 2.0-4.0h-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.
CN201610668155.1A 2016-08-12 2016-08-12 A kind of aerial kerosene hydrofining technology Pending CN106190247A (en)

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Application publication date: 20161207