CN106281452A - A kind of residuum hydrodesulfurization RFCC group technology of sour crude - Google Patents
A kind of residuum hydrodesulfurization RFCC group technology of sour crude Download PDFInfo
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- CN106281452A CN106281452A CN201610657010.1A CN201610657010A CN106281452A CN 106281452 A CN106281452 A CN 106281452A CN 201610657010 A CN201610657010 A CN 201610657010A CN 106281452 A CN106281452 A CN 106281452A
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- oil
- hydrogenation
- rfcc
- hydrodesulfurization
- decompression residuum
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Classifications
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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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- 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
- C10G2400/04—Diesel oil
Abstract
The invention discloses the hydrodesulfurization RFCC group technology of the decompression residuum of a kind of sour crude, decompression residuum and optional catalytic cracked oil pulp steam thing, optional heavy catalytic cycle oil, optional distillate together with enter residual hydrogenation equipment, carrying out hydrogenation reaction in the presence of hydrogen and hydrogenation catalyst, separating reaction product obtains gas, hydrotreated naphtha, hydrogenated diesel oil and hydrogenated residue；Hydrogenated residue individually or enters heavy oil catalytically cracking equipment together with vacuum gas oil (VGO), carries out cracking reaction in the presence of Cracking catalyst, and separating reaction product obtains dry gas, liquefied gas, gasoline, diesel oil, heavy-cycle oil and slurry oil；Described residual hydrogenation equipment uses fixed bed reactors, is filled with hydrogenation catalyst in fixed bed reactors.Total sulfur content in High Sulfur Vacuum Residue catalytic cracking production can be reduced to below 5ppm by this technique, and makes Useful Time of Hydrogenation Catalyst reach more than 2 years.
Description
Technical field
The present invention relates to a kind of residuum hydrodesulfurization-RFCC group technology, be specifically related to a kind of employing specific
The residuum hydrodesulfurization of the sour crude that catalyst is carried out-RFCC group technology.
Background technology
Residual oil is primarily referred to as from atmospheric and vacuum distillation unit bottom heavy constituent out, and wherein atmospheric unit is out called normal pressure slag
Oil, decompressor out be called decompression residuum.Decompression residuum darkish complexion thickness, in semi-solid under room temperature, its character and crude oil
Character is relevant.In petroleum refinery, residual oil is usually used in processing and produces the products such as petroleum coke, residual lubricating oil, Colophonium, or as splitting
Change raw material.
At present, alternative residuum conversion process technique has tens kinds, and hydrogenation technique is well recognized as economic and environment-friendly deeply
Processing technique.After the impurity such as residual oil hydrogenated process removing metal, sulfur, nitrogen, improve hydrogen content, can urge as the heavy oil of high-quality
Change cracked stock.Additionally residual hydrocracking heavy oil is due to molecular structure relation, processes through RFCC, octane number
The highest, the productivity of C3, C4 alkene is the highest, and the sulfur content in product is the lowest simultaneously, can meet the requirement of modern environmental protection, therefore
Now residual hydrogenation tail oil is obtained the most universal application directly as the technique of Rfcc Feedstock.
The residual hydrogenation technology of the most industrialization or technology maturation according to reactor types, can be divided into fixed bed,
4 types such as moving bed, ebullated bed (expanded bed) and suspension bed (slurry bubble bed).Wherein, fixed bed Residue Hydrotreating Technology is instead
The different beds answering device load different types of catalyst, to remove metal heteroatom and sulfur, nitrogen element in heavy oil, heavy to it
Component is changed a social system.This technique combines with catalytic cracking process and can be completely converted into market by being worth relatively low decompression residuum
Costly gasoline, diesel oil, it is achieved making full use of of oil refining resource.
Although have the fixed bed hydrogenation technology with Chevron company and Uop Inc. at present, but current residual oil deep processing
Based on the decompression residuum that Middle East light oil before being all based on and domestic crude oil produce, these residual oil compositions not very complexity,
Heavy constituent is less, after the most described decompression residuum and the mixing of atmospheric tower base oil, can directly enter RFCC (RFCC) dress
Put and process.
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%.
But existing Residue Hydrotreating Technology for be all domestic and the decompression residuum in the Middle East, the catalyst that it uses is used
When High Sulfur Vacuum Residue, desulfurized effect difference and catalysqt deactivation are fast.The most how to provide the hydrodesulfurization of High Sulfur Vacuum Residue-
RFCC group technology, effectively the sulfur content in product can control at below 5ppm, and improve the use longevity of catalyst
Life, is a difficult problem facing of this area.
Summary of the invention
It is an object of the invention to propose the hydrodesulfurization-RFCC combination of the decompression residuum of a kind of sour crude
Technique, effectively the sulfur content in product can control at below 5ppm, and improve the service life of catalyst.
For reaching this purpose, the present invention by the following technical solutions:
The hydrodesulfurization of the decompression residuum of a kind of sour crude-RFCC group technology, decompression residuum is with optional
Catalytic cracked oil pulp steam thing, optional heavy catalytic cycle oil, optional distillate enter residual hydrogenation dress together
Putting, carry out hydrogenation reaction in the presence of hydrogen and hydrogenation catalyst, separating reaction product obtains gas, hydrotreated naphtha, hydrogenation
Diesel oil and hydrogenated residue；Hydrogenated residue individually or enters heavy oil catalytically cracking equipment, at cracking catalysis together with vacuum gas oil (VGO)
Carrying out cracking reaction in the presence of agent, separating reaction product obtains dry gas, liquefied gas, gasoline, diesel oil, heavy-cycle oil and slurry oil.
Wherein optional, heavy-cycle oil is recycled to residual hydrogenation equipment.
Optionally, slurry oil is after separated goes out residue, and the thing that steams of slurry oil is back to hydrogenation plant.
Described residual hydrogenation equipment 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 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 350-450 DEG C, and hydrogen dividing potential drop is 12-17MPa, hydrogen
Oil volume is than 600-1000, volume space velocity 0.15-0.4h-1。
In the decompression residuum of described sour crude, sulfur content is more than 1wt%, preferably more than 1.5wt%.
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 middle coalite tar desulfurized effect.More make us glad
Happiness, works as Co2+When doping in KIT-1 controls in the range of 0.63%-0.72%, its desulphurizing ability is the strongest, when painting
System is 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, in can realizing, in coalite tar, sulfur content controls 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 370-420 DEG C, and hydrogen dividing potential drop is 14-
15MPa, hydrogen to oil volume ratio 700-900, volume space velocity 0.15-0.3h-1。
Preferably, described fixed bed reactors include 2-10 beds, further preferred 2-5 catalyst bed
Layer.
The technological process of the present invention is as follows:
Residual oil and hydrogen enter residual hydrocracking device, react in the presence of a hydrogenation catalyst, separate residual oil and add
The product of hydrogen, obtains gas, hydrotreated naphtha, hydrogenated diesel oil and hydrogenated residue, wherein gas, hydrotreated naphtha and hydrogenation
Diesel oil respectively through pipeline ejector, hydrogenated residue then through pipeline together with the optional vacuum gas oil (VGO) from pipeline through pipeline
Enter heavy oil catalytically cracking equipment, react in the presence of Cracking catalyst, the product of heavy oil separation catalytic cracking,
To dry gas, liquefied gas, gasoline, diesel oil, heavy-cycle oil and slurry oil, wherein dry gas, liquefied gas, gasoline and diesel oil draw through pipeline respectively
Going out device, heavy-cycle oil is recycled to residual hydrocracking device through pipeline successively, and slurry oil enters distilling apparatus through pipeline, isolates
Residue go out device through pipeline, slurry oil steam thing successively through pipeline enter residual hydrocracking device 3, optional distillate
Residual hydrocracking device is entered successively through pipeline.
The hydrofining technology of the present invention is by choosing specific catalyst, and described catalyst is by mixing hetero atom Co2+
KIT-1 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 the decompression residuum of sour crude can control
Total sulfur content is less than 5ppm, and the catalyst of catalytic hydrogenation unit can reach more than 2 years service life 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+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 is by Beijing satellite system
The double plunger micro pump making factory's manufacture carries continuously, and hydrogen is supplied and use Beijing Sevenstar-HC D07-11A/ZM gas by gas cylinder
Weight effusion meter coutroi velocity, hydrogenation catalyst loadings is 2kg.Reacted product enters RFCC unit.
Raw materials used for Kazakhstan's decompression residuum, its sulfur content is up to 3.27%, i.e. 32700ppm.
Controlling reaction condition is: temperature 390 DEG C, hydrogen dividing potential drop 14.0MPa, hydrogen to oil volume ratio 800, volume space velocity 0.2h-1。
Testing final product, total sulfur content is reduced to 4ppm, and beds pressure drop is unchanged.
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 2ppm, and beds pressure drop is unchanged.
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 32ppm, and beds pressure drop increases above 0.05%.
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 39ppm, and beds pressure drop increases above 0.05%.
Comparative example 3
Co by embodiment 12+Replace with Zn2+, remaining condition is constant.
Testing final product, total sulfur content is reduced to 40ppm, and beds pressure drop increases above 0.05%.
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 41ppm, and beds pressure drop increases above 0.05%.
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 43ppm, and beds pressure drop increases above 0.05%.
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 present invention technique effect (desulfurization degree and beds change in pressure drop, change in pressure drop reflect catalyst inactivation speed
Degree), the therefore Co of the certain content scope of the present invention2+Collaborative effect is possessed between doping KIT-1 carrier and other components of catalyst
Should, 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 49ppm, and beds pressure drop increases above 0.05%.
Comparative example 7
Omitting the WC in embodiment 1, remaining condition is constant.
Testing final product, total sulfur content is reduced to 52ppm, and beds pressure drop increases above 0.05%.
Above-described embodiment and the explanation of comparative example 6-7, hydrogenation catalyst several activity group of the hydrofining technology of the present invention
The specific contact an of/existence, is omitted or substituted one of which or several, all can not reach the certain effects of the application, it was demonstrated that
Which create 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. the hydrodesulfurization of the decompression residuum of sour crude-RFCC group technology, decompression residuum and optional
Catalytic cracked oil pulp steam thing, optional heavy catalytic cycle oil, optional distillate enter residual hydrogenation equipment together,
Carrying out hydrogenation reaction in the presence of hydrogen and hydrogenation catalyst, separating reaction product obtains gas, hydrotreated naphtha, hydrogenated diesel oil
And hydrogenated residue；Hydrogenated residue individually or enters heavy oil catalytically cracking equipment together with vacuum gas oil (VGO), deposits in Cracking catalyst
Carrying out cracking reaction under, separating reaction product obtains dry gas, liquefied gas, gasoline, diesel oil, heavy-cycle oil and slurry oil；Described slag
Oil hydrogenation plant uses fixed bed reactors, is filled with hydrogenation catalyst in fixed bed reactors, and described hydrogenation catalyst includes
Carrier and active component, it is characterised in that
Described carrier is incorporation hetero atom Co in synthetic bone shelf structure2+KIT-1,
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 300-420 DEG C, and hydrogen dividing potential drop is 13-15MPa, hydrogen oil body
Long-pending ratio 800-1200, volume space velocity 0.3-0.8h-1。
2. hydrodesulfurization-RFCC the group technology of the decompression residuum of sour crude as claimed in claim 1, it is special
Levy and be, hetero atom Co2+The 0.63%-0.72% that doping is KIT-1 weight.
3. hydrodesulfurization-RFCC the group technology of the decompression residuum of sour crude as claimed in claim 1, it is special
Levying and be, the total content of described active component is the 3-12% of carrier KIT-1 weight, preferably 5-10%.
4. hydrodesulfurization-RFCC the group technology of the decompression residuum of sour crude as claimed in claim 1, it is special
Levy and be, 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. hydrodesulfurization-RFCC the group technology of the decompression residuum of sour crude as claimed in claim 1, it is special
Levying and be, the reaction condition of described fixed bed reactors is: reaction temperature is 370-420 DEG C, and hydrogen dividing potential drop is 14-15MPa, hydrogen oil
Volume ratio 700-900, volume space velocity 0.15-0.3h-1。
6. hydrodesulfurization-RFCC the group technology of the decompression residuum of sour crude as claimed in claim 1, it is special
Levying and be, described fixed bed reactors include 2-10 beds, preferably 2-5 beds.
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| US11860292B2 (en) | 2016-11-17 | 2024-01-02 | Trinamix Gmbh | Detector and methods for authenticating at least one object |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1262969A (en) * | 2000-03-02 | 2000-08-16 | 南开大学 | Catalyst using TiO2 as carrier to load metal nitride Mo2N |
| CN1470327A (en) * | 2002-07-24 | 2004-01-28 | 北京石油化工学院 | Metal nitride catalyst preparing method and catalyst |
| CN1895777A (en) * | 2005-07-14 | 2007-01-17 | 北京化工大学 | Porous molecular-sieve catalyst for assembling carbide and its preparation |
| WO2013149014A1 (en) * | 2012-03-29 | 2013-10-03 | Wayne State University | Bimetal catalysts |
| CN105251527A (en) * | 2015-11-11 | 2016-01-20 | 中国石油大学(北京) | Composite molecular sieve and hydrodesulfurization catalyst prepared with composite molecular sieve as carrier |
-
2016
- 2016-08-11 CN CN201610657010.1A patent/CN106281452A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1262969A (en) * | 2000-03-02 | 2000-08-16 | 南开大学 | Catalyst using TiO2 as carrier to load metal nitride Mo2N |
| CN1470327A (en) * | 2002-07-24 | 2004-01-28 | 北京石油化工学院 | Metal nitride catalyst preparing method and catalyst |
| CN1895777A (en) * | 2005-07-14 | 2007-01-17 | 北京化工大学 | Porous molecular-sieve catalyst for assembling carbide and its preparation |
| WO2013149014A1 (en) * | 2012-03-29 | 2013-10-03 | Wayne State University | Bimetal catalysts |
| CN105251527A (en) * | 2015-11-11 | 2016-01-20 | 中国石油大学(北京) | Composite molecular sieve and hydrodesulfurization catalyst prepared with composite molecular sieve as carrier |
Non-Patent Citations (14)
| Title |
|---|
| F•维拉尼: "《稀土技术及其应用》", 31 July 1986, 烃加工出版社 * |
| 中国石油化工集团公司人事部，等: "《加氢裂化装置操作工》", 30 September 2008, 中国石化出版社 * |
| 何鸣元，等: "《《石油炼制和基本有机化学品合成的绿色化学》》", 31 January 2006, 中国石化出版社 * |
| 姜琳琳: "全馏分FCC汽油加氢改质中改性MCM-41催化性能研究", 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》 * |
| 崔克清，等: "《化工工艺及安全》", 31 May 2004, 化学工业出版社 * |
| 张文成: "改性MCM-41 分子筛的制备及加氢催化性能研究", 《第十一届全国青年催化学术会议论文集（下）》 * |
| 李静海，等: "《展望21世纪的化学工程》", 31 October 2004, 化学工业出版社 * |
| 林世雄: "《石油炼制工程（第三版）》", 31 July 2000, 化学工业出版社 * |
| 王基铭: "《石油炼制辞典》", 30 September 2013, 中国石化出版社 * |
| 王海彦，等: "《石油加工工艺学》", 31 January 2014, 中国石化出版社 * |
| 王福安，等: "《绿色过程工程引论》", 31 October 2002, 化学工业出版社 * |
| 王雷，等: "《炼油工艺学》", 31 August 2011, 中国石化出版社 * |
| 邝生鲁: "《现代精细化工高新技术与产品合成工艺》", 31 December 1997, 科学技术文献出版社 * |
| 阎子峰: "《纳米催化技术》", 31 May 2003, 化学工业出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11860292B2 (en) | 2016-11-17 | 2024-01-02 | Trinamix Gmbh | Detector and methods for authenticating at least one object |
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