CN106190295A - 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 PDF

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Publication number
CN106190295A
CN106190295A CN201610669646.8A CN201610669646A CN106190295A CN 106190295 A CN106190295 A CN 106190295A CN 201610669646 A CN201610669646 A CN 201610669646A CN 106190295 A CN106190295 A CN 106190295A
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oil
hydrogenation
rfcc
hydrodesulfurization
decompression residuum
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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
    • 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
    • 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
    • C10G2300/10—Feedstock materials
    • C10G2300/1077—Vacuum residues
    • 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)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Materials Engineering (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)

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

The residuum hydrodesulfurization of a kind of sour crude-RFCC group technology
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 Cu 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 350-450 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%.
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: be situated between to the Siliceous MCM-41 of finished product Porous molecular sieve inner surfaces of pores introduces Cu2+, this approach can be exchanged Cu by ion2+It is supported on the inner surface of MCM-41, Thus improve catalysis activity, absorption and the Thermodynamically stable performance etc. of MCM-41 mesopore molecular sieve on the whole.
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 Cu2+MCM-41 as carrier could realize sulfur content control effect, inventor has attempted at MCM- Adulterate in 41 Al3+、Fe3+、Zn2+、Ga3+In the ion at generation anionic surface center, find all to realize described effect.To the greatest extent Manage described mechanism current and unclear, but this have no effect on the enforcement of the present invention, inventor according to well-known theory with it is experimentally confirmed that Cooperative effect is there is between itself and the active component of the present invention.
Described Cu2+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 middle coalite tar desulfurized effect.More make us glad Happiness, works as Cu2+When doping in MCM-41 controls in the range of 0.63%-0.72%, its desulphurizing ability is the strongest, when painting System is with Cu2+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 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, 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.
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 Cu2+ 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 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 Cu2+MCM-41, Cu2+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 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 5ppm, and beds pressure drop is unchanged.
Embodiment 2
Preparing catalyst by infusion process, carrier is doping Cu2+MCM-41, Cu2+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 4ppm, 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 37ppm, and beds pressure drop increases above 0.05%.
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 29ppm, and beds pressure drop increases above 0.05%.
Comparative example 3
Cu by embodiment 12+Replace with Zn2+, remaining condition is constant.
Testing final product, total sulfur content is reduced to 23ppm, and beds pressure drop increases above 0.05%.
Comparative example 4
By the Cu 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 21ppm, and beds pressure drop increases above 0.05%.
Comparative example 5
By the Cu 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 33ppm, 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 MCM-41 carrier, when replacing with other known carriers of this area, or carrier is identical but Cu2+During doping difference, all reach Less than the present invention technique effect (desulfurization degree and beds change in pressure drop, change in pressure drop reflect catalyst inactivation speed Degree), the therefore Cu of the certain content scope of the present invention2+Collaborative effect is possessed between doping MCM-41 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 54ppm, 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 Cu 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 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 Cu2+The 0.63%-0.72% that doping is MCM-41 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 MCM-41 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.
CN201610669646.8A 2016-08-12 2016-08-12 A kind of residuum hydrodesulfurization RFCC group technology of sour crude Pending CN106190295A (en)

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