CN110408431A - A kind of method of group technology processing low grade oils - Google Patents
A kind of method of group technology processing low grade oils Download PDFInfo
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- CN110408431A CN110408431A CN201910357027.9A CN201910357027A CN110408431A CN 110408431 A CN110408431 A CN 110408431A CN 201910357027 A CN201910357027 A CN 201910357027A CN 110408431 A CN110408431 A CN 110408431A
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- catalytic cracking
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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
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
Abstract
The invention discloses a kind of methods of group technology processing low grade oils.After inferior feedstock oil and hydrogen enter the molten hydrogen of mixer saturation, pass through weighted BMO spaces area first；Reaction effluent enters hydrotreating reaction area with catalytic cracking recycle oil after separation, gained reaction effluent is separated, it obtains hydrogenated residue and carries out catalytic cracking reaction, it obtains recycle oil and/or slurry oil is recycled to weighted BMO spaces reaction zone, obtain another part recycle oil and be recycled to hydrotreating reaction area；Wherein the reaction temperature t1 of weighted BMO spaces reaction zone is higher than the reaction temperature t2 in hydrotreating reaction area.The method of the present invention can be improved the utilization rate of hydrotreating major catalyst, extend the operation cycle of combined unit, and increase the operational efficiency of device.
Description
Technical field
The present invention relates to petroleum refining field more particularly to a kind of use residual hydrocracking and catalytic cracking combined techniques
The method for handling heavy oil residue.
Background technique
Currently, demand of the refined products market to light, middle matter oil product will be in continuous upward trend both at home and abroad, to fuel oil etc.
The demand of heavy oil product is then on a declining curve.Further, since the pressure of environmental protection increasingly increases, various countries generally improve petroleum
The quality criteria requirements of the especially automobile-used petrol and diesel oil product of product.It, can be with more economical reasonable generation under above-mentioned market trend
Valence realize heavy oil lighting, can make again obtained product meet the oil Refining Technologies of the constantly petrol and diesel oil product specification of harshness at
One of the technology of domestic and international oil Refining Technologies developer's focus development.
In the various processes of heavy oil product lighting, heavy oil product is subjected to hydrotreating, right back end hydrogenation first
It is a kind of preferable technical process that tail oil, which carries out catalyzed cracking processing,.By adding hydrogen, significantly reduce metal in these raw materials,
Sulphur, nitrogen, asphalt content improve hydrogen-carbon ratio, and then provide excellent raw material for devices such as catalytic cracking and delayed cokings.At present
Main hydrogenation technique mainly has ebullated bed, suspension bed, moving bed and fixed-bed process, and wherein suspension bed and moving bed process be also
It is very immature, and higher cost.Ebullated bed high investment, and operation difficulty is larger.Fixed bed is because at low cost, easy to operate
And safety is small, technology maturation, thus develops very fast.
In the prior art, it is realized by being provided with multiple hydrogenators of multiple hydrogenation catalyst beds to heavy oil product
Hydrotreating.But the usual viscosity of heavy oil product is larger, metal impurities or asphalitine are higher, in hydrogenation process, metal and
Coke can be gradually deposited on catalyst, be easy to make rapid catalyst deactivation, bed blocking, pressure rise, this phenomenon is the
One hydrogenator is especially serious, moreover, when the pressure drop in first reactor reaches or approaches the theoretical pressure drop upper limit, instead
It answers and easily occurs hot spot in device, device can only be forced to stop work at this time, shorten the operation cycle of heavy oil product hydrotreater.
It is former that CN1349554A discloses a kind of up-flow reactor system hydrotreating heavy with stratiform catalyst bed
The method of material.With the upflow fixed bed reactor hydrotreating metal of the catalyst of at least two different hydrogenation activities, sulphur and
The heavy charge of carbon containing residual matter pollution.But this method cycle of operation is short, is usually no more than 1 year.
Itd is proposed in CN1484684A replaceable reactor and can short-circuit reaction device hydrotreatment of heavy hydrocarbon fraction method, should
It is traditional down-type fixed-bed reactor that reactor is protected in patent, if Ca, Fe content are higher in raw material, due to reaction
Logistics from top to bottom, if the gap between these solid impurity blocking catalysts, though in protective agent duct deposited metal energy
When power does not arrive saturation capacity, this reactor pressure decrease can also be increased, so that another reactor must be switched to.
CN102453530A discloses a kind of method of hydrotreating of processing heavy oil product, heavy oil product feedstock oil and hydrogen mixing
Enter hydrogenation protecting reaction zone afterwards, then immediately proceed to hydrotreating reaction area, setting at least two is in parallel in hydrogenation protecting area
Can switch the up flow type hydrogenation protecting reactor used in turn.The method that the invention uses four kinds of hydrogenation protecting agent gradations, has
Extend the operation cycle of device conducive to removing metal to prevent from blocking and improving the service life of major catalyst.But this method is to device
The increase rate of the cycle of operation is still little.
Residual hydrogenation tail oil is obtained into more and more common application directly as the technique of Rfcc Feedstock, and
One of most effective crude conversion technology, it can obtain more light-end products from residual oil.It is urged in traditional residual hydrogenation-
Change in cracking group technology, catalytic cracking recycle oil is to be recycled in catalytic cracking unit to be further processed.Since recycle oil contains
There is polycyclic aromatic hydrocarbon, thus light oil yield is low, green coke amount is big, increases regenerator load, reduces heavy oil catalytically cracking equipment
Treating capacity and economic benefit.In addition the sulfur content of recycle oil is higher, is about higher by one times than hydrogenation tail oil, recycle oil circulation but also
Product sulfur content rises.
CN106701191A discloses a kind of method of hydrogenation and catalystic cracking process residual oil, including adds hydrogen pre-
Handle reaction zone, hydrotreating reaction area and catalytic cracking reaction zone；The method includes the following contents: residual oil raw material and hydrogen
Successively pass through concatenated weighted BMO spaces reaction zone and hydrotreating reaction area after mixing, the reaction in hydrotreating reaction area is flowed out
Object carries out gas-liquid separation, and gas phase is recycled back to weighted BMO spaces reaction zone and/or hydrotreating reaction area, and liquid phase is directly entered catalysis
Cracking reaction area carries out catalytic cracking reaction, the isolated dry gas of catalytic cracking reaction effluent, liquefied gas, catalytically cracked gasoline
Fraction, catalytic cracking diesel oil fraction, heavy catalytic cycle oil and catalytic cracked oil pulp, wherein catalytic cracking diesel oil and catalysis
Some or all of cracking slurry oil is recycled back to hydrotreating reaction area and carries out hydrotreating reaction area.This method can extend device
Stabilization operation period, but this method operation it is more complex.
Summary of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of method of group technology processing low grade oils, and especially one
Kind can give full play to differential responses area catalyst performance, increase the heavy oil hydrogenation treatment method of device operation cycle.
A kind of method of group technology processing low grade oils provided by the present invention, including the following contents:
(1) at least one weighted BMO spaces reaction zone, a hydrotreating reaction area and a catalytic cracking reaction zone are provided；Add
Include hydrogenation protecting catalyst and Hydrodemetalation catalyst in hydrogen pretreatment reaction zone, includes adding hydrogen in hydrotreating reaction area
Desulphurization catalyst and hydrodenitrogeneration (carbon residue conversion) catalyst include catalytic cracking catalyst in catalytic cracking reaction zone；
(2) inferior feedstock oil, the recycle oil in weighted BMO spaces area, catalytic cracked oil pulp, partially catalyzed cracking recycle oil and hydrogen
Enter mixer together to form the molten hydrogen logistics of saturation and gaseous hydrogen is discharged；
(3) the molten hydrogen logistics of saturation from step (2) enters weighted BMO spaces reaction zone, and liquid is carried out under the conditions of weighted BMO spaces
Metal impurities are removed 40wt%~90wt% by phase hydrogenation reaction, and sulphur is removed 20wt%~70wt%, obtain tenor reduction
Reaction effluent；
(4) reaction effluent obtained by step (3) is separated into the first high-pressure separator, obtains the first hydrogen-rich gas and the first liquid
Body, separating obtained first hydrogen-rich gas are recycled after compressor compresses after can isolating after further treatment hydrogen；
(5) first liquid a part obtained by step (4) is recycled back to weighted BMO spaces reaction zone, another part and partially catalyzed cracking
Enter hydrotreating reaction area after recycle oil mixing, carries out hydrogenation reaction under hydroprocessing conditions；
(6) reaction effluent obtained by step (5) enters the progress gas-liquid separation of the second separator, obtains the second hydrogen-rich gas and second
Liquid；Separating obtained second hydrogen-rich gas can be recycled back to hydrotreating reaction area after desulfurization and compressor compresses, separate institute
It obtains second liquid and enters fractionating system；
(7) second liquid product obtained by step (6) enters fractionating column, obtains gas, naphtha, hydrogenated diesel oil and hydrogenation tail oil；
(8) hydrogenation tail oil obtained by step (7) enters catalytic cracking reaction zone, and it is anti-that cracking is carried out in the presence of catalytic cracking catalyst
It answers, reaction generates after oil is fractionated and obtains dry gas, liquefied gas, catalytically cracked gasoline, catalytic cracking diesel oil, catalytic cracking recycle oil
And catalytic cracked oil pulp；
(9) catalytic cracking recycle oil obtained by step (8) is divided into two parts, and a part is used as flux oil after mixing with catalytic cracked oil pulp
Mixer before being recycled back to weighted BMO spaces reactor, another part are recycled to first, hydrotreating reaction area reactor and enter
Mouthful.
It according to the method for the present invention, can also include the following contents in step (9): by catalytic cracking bavin obtained by step (8)
The all or part of oil is recycled to the entrance of the last one reactor in hydrotreating reaction area.
In the present invention, wherein the average reaction temperature t1 of step (3) the weighted BMO spaces reaction zone adds higher than step (5)
The average reaction temperature t2 of hydrogen processing reaction zone, 5~40 DEG C of t2 high of preferably t1 ratio, 10~30 DEG C of t2 high of preferably t1 ratio.
According to the method for the present invention, more than two weighted BMO spaces reaction zones are wherein provided in step (1), this two with
On weighted BMO spaces reaction zone be usually be arranged in parallel, the reaction zone of changeable operation.Therefore, method of the invention can be with
It can be cut out into reaction stream after one of weighted BMO spaces reaction zone is not able to satisfy service requirement including step (10)
Journey, and by second weighted BMO spaces reaction zone incision process flow, the weighted BMO spaces reaction zone cut out can be urged
The displacement of agent draws off the old catalyst of inactivation, reload fresh and/or regenerated catalyst.
The weighted BMO spaces reaction zone is not able to satisfy service requirement and refers to: the effluent of weighted BMO spaces reaction zone can not
The pressure drop for meeting at least one catalyst bed in the feed needs or weighted BMO spaces reaction zone of downstream hydrogenation treatment region reaches
There is hot spot in the pressure drop upper limit or catalyst bed.
The standard of the feed needs for being unable to satisfy downstream hydrogenation processing reaction zone can be with are as follows: weighted BMO spaces reaction zone
Exporting the tenor in product liquid is more than specified value.Specifically, judging weighted BMO spaces reaction zone outlet product liquid is
The standard of the no feed needs for meeting downstream hydrogenation treatment region is, tenor in effluent liquid (refer to W metal, V, Fe,
The summation of Na and Ca equal size) it has been more than the 8 μ g/g of μ g/g~50, preferably 10 μ of μ g/g~30 g/g.
The pressure drop upper limit is 0.4~0.8 times, preferably 0.5~0.8 times of reactor design maximum pressure drop.It is described
Hot spot is that the radial temperature difference at least one catalyst bed is 15~50 DEG C, preferably 15~30 DEG C.
In heavy oil hydrogenation treatment method of the invention, the heavy oil feedstock oil refers to by topped crude, petroleum residual oil, oil
The hydro carbons for the high asphalt content that sand, pitch, shale oil, liquefaction coal or reclaimed oil obtain.Heavy oil feedstock oil usually contains various
Pollutant, carbon residue is high, and the impurity contents such as sulphur and nitrogen are high, and tenor is typically larger than 30mg/g.The method of the present invention is especially
It is suitble to the heavy oil feedstock of processing high metal content, is especially suitable for processing metal (nickel+vanadium) content and is greater than 60mg/g and/or iron content
Greater than 10mg/g and/or calcium content is greater than the heavy oil feedstock of 10mg/g.
In method of the invention, the hydrogenation protecting catalyst that weighted BMO spaces reaction zone uses can be protected for residual hydrogenation
Agent, or prepared according to feedstock property by conventional method in that art.Residual hydrogenation protective agent is this field conventional catalyst, can be with
Using commercial goods.The hydrogenation protecting agent using porous refractory inorganic oxide such as aluminium oxide as carrier, group VIB and/or
The oxide of VIII race's metal such as W, Mo, Co, Ni etc. is the catalyst of active component, such as by the limited public affairs of Sinopec's share
Take charge of the FZC series residual hydrogenation protective agent of catalyst branch production.
The Hydrodemetalation catalyst can be residuum hydrogenating and metal-eliminating catalyst, or according to feedstock property by this
The preparation of field conventional method.These catalyst are typically all the group VIB using porous refractory inorganic oxide such as aluminium oxide as carrier
And/or VIII one or more of oxides of race's metal such as W, Mo, Co, Ni etc. be active component, be selectively added other each
The catalyst of the elements such as kind auxiliary agent such as P, Si, F, B.The Hydrodemetalation catalyst, on the basis of the total weight of catalyst,
And in terms of oxide, the content of molybdenum and/or tungsten is 0.5~15 weight %, and the content of cobalt and/or nickel is 0.3~8 weight %, remaining
Amount is alumina support.The alumina support be a kind of bimodal hole alumina support, 0.5~2.0 milliliter of Kong Rongwei/
Gram, specific surface area is 120~350 meters2/ gram, aperture accounts for total pore volume 30~90% in 10~30 nanometers of Kong Rong, and aperture is 100
~2000 nanometers of Kong Rong accounts for total pore volume 10~50%, and bore dia is less than 10 nanometers, between 30-100 nanometers and be greater than
2000 nanometers of the sum of Kong Rong accounts for 20% or less total pore volume.It is arrived needed for the diffusion process and reaction of reactant molecule in order to balance
The catalyst of active surface, the bimodal pore distribution with macropore and mesoporous is shown in weighted BMO spaces reaction zone reaction process
Preferable performance.In weighted BMO spaces reaction zone, the admission space ratio of hydrogenation protecting catalyst and Hydrodemetalation catalyst
Generally 5:95~95:5, preferably 10:90~60:40.
Heavy oil hydrogenation treatment method according to the present invention, wherein preferably adding the de- gold of hydrogen in weighted BMO spaces reaction zone
The downstream of metal catalyst can also include Hydrobon catalyst.The loadings of Hydrobon catalyst are hydrodemetallisation catalyst
The 5%~30% of agent loadings.
The Hydrobon catalyst can be the common residuum hydrodesulfurization catalyst in this field, or according to raw material
Property is prepared by conventional method in that art.Catalyst is typically all using porous refractory inorganic oxide such as aluminium oxide as carrier the
The oxide of VI B race and/or VIII race's metal such as W, Mo, Co, Ni etc. are active component, are selectively added various other auxiliary agents such as
P, the catalyst of the elements such as Si, F, B.Due in this technology in weighted BMO spaces reaction zone product it is restricted to tenor, be
The more preferable overall performance optimization for playing catalyst system uses improved Hydrobon catalyst, the overall performance of the catalyst
Between conventional Hydrodemetalation catalyst and Hydrobon catalyst, i.e., the aperture of the catalyst is compared with conventional hydrodesulfurization
Catalyst is bigger, holds metal ability with preferable, activity is slightly higher compared with conventional hydro catalyst for demetalation, has stronger add
Hydrogen desulphurizing ability.
The Hydrobon catalyst, on the basis of the total weight of catalyst, and in terms of oxide, molybdenum and/or tungsten
Content is 10~25 weight %, and the content of cobalt and/or nickel is 1~6 weight %, and surplus is alumina support.The aluminium oxide
Kong Rong is not less than 0.35 ml/g, and specific surface area is 150~350 meters2/ gram, aperture accounts for total pore volume in 6~15 nanometers of Kong Rong
70% or more.
In the method for the present invention, reaction condition can be according to the reaction effect that the property and requirement of raw material reach by this field
General knowledge determines.In general the reaction condition of weighted BMO spaces reaction zone is that reaction pressure is 5MPa~35MPa, preferably
It is 10MPa~20MPa, average reaction temperature is to be operated at 340 DEG C~430 DEG C, preferably 340 DEG C~420 DEG C, volume is empty when liquid
Speed is generally in 0.1h-1~5.0h-1, preferably 0.3h-1~3.0h-1In the range of, hydrogen to oil volume ratio is 200~2000, preferably
300~1500, liquid phase circulation ratio (recycle oil/fresh feed oil mass ratio) is 0.1:1~10:1, preferably 0.2:1~3:1.
In method of the invention, the reaction of one or more hydrogenation protecting is can be set in the weighted BMO spaces reaction zone
Device, each hydrogenation protecting reactor is at least provided with a hydrogenation protecting catalyst bed, if being provided with multiple catalyst beds,
The recycle oil for being saturated molten hydrogen can be squeezed into, between reaction bed to reach reduction catalyst bed temperature rise and reaction is replenished in time
The purpose of required hydrogen.
In the method for the present invention, the mixer used can be eddy mixer, be also possible to static mixer, jet mixing
The isostructural mixer of device.
In the method for the present invention, catalyst used in hydrotreating reaction area can be the common heavy oil product in this field and add
Hydrogen handles catalyst, and optimum catalyst property can be optimized according to feedstock property.Catalyst generally comprise it is a variety of, such as plus hydrogen
Desulphurization catalyst and hydrodenitrogenation catalyst etc..These catalyst are typically all to be with porous refractory inorganic oxide such as aluminium oxide
The oxide of carrier, group VIB and/or VIII race's metal such as W, Mo, Co, Ni etc. are active component, are selectively added other each
The catalyst of the elements such as kind auxiliary agent such as P, Si, F, B.
In the hydrotreating reaction area, the admission space of Hydrobon catalyst and hydrodenitrogenation catalyst is than general
For 20:80~80:20, preferably 40:60~70:30.
The hydrodenitrogenation catalyst, on the basis of the total weight of catalyst, and in terms of oxide, molybdenum and/or tungsten
Content is 12~30 weight %, and the content of cobalt and/or nickel is 3~12 weight %, and surplus is alumina support.The aluminium oxide
Kong Rong is not less than 0.35 ml/g, and specific surface area is 150~350 meters2/ gram, aperture accounts for total pore volume in 6~15 nanometers of Kong Rong
40~75%.
According to the method for the present invention, wherein it can also add hydrogen including Hydrodemetalation catalyst in hydrotreating reaction area
Catalyst for demetalation is seated in the upstream of Hydrobon catalyst, and the loadings of Hydrodemetalation catalyst are hydrotreating reaction
The 2%~30% of area's catalyst total filling amount.
In hydrotreating reaction area catalyst filling sequence be usually make reaction stream successively with hydrodemetallisation catalyst
Agent, Hydrobon catalyst and hydrodenitrogenation catalyst contact, also have certainly by the technology of these types of catalyst mixed packing.On
State the technology contents that Catalyst packing technology is well known to those skilled in the art.Catalyst can use commercial goods, as in
The FZC series residuum hydrogenating and metal-eliminating catalysts of petrochemical industry Fushun Petrochemical Research Institute, state development and production, desulphurization catalyst and de-
Nitrogen catalyst can also be prepared according to this field existing method.
In method of the invention, the reaction condition in hydrotreating reaction area is that reaction pressure is 5MPa~35MPa, preferably
It is 10MPa~20MPa, average reaction temperature is 320 DEG C~420 DEG C, and preferably 330 DEG C~410 DEG C, volume space velocity is when liquid
0.1h-1~5.0h-1, preferably 0.3h-1~3.0h-1, hydrogen to oil volume ratio is 200~1500, preferably 300~1200.
In the method for the present invention, weighted BMO spaces and hydrotreating two reaction zones belong to serial operation, therefore two reactions
The pressure in area is the same pressure rating, because the presence of pressure drop might have difference slightly.
In the method for the present invention, hydrodemetallization and partial hydro-desulfurization reaction are substantially carried out in weighted BMO spaces reaction zone,
It is operated at a higher temperature, is conducive to the progress of demetalization reaction, to enable the activity of Hydrodemetalation catalyst
It is fully used.The material for being stripped of a large amount of metal impurities enters hydrotreating reaction area and is further reacted.Due to
A large amount of metal impurities are stripped of, the material into hydrotreating reaction area is greatly lowered the murder by poisoning of hydrotreating zone catalyst,
The utilization rate of Hydrobon catalyst and hydrodenitrogenation catalyst can be significantly improved, the use of hydrotreating zone catalyst is extended
Service life, and then effectively extend the operation cycle of a whole set of hydrotreater.For the operation of Proper Match two reaction zones, add hydrogen
The average reaction temperature in pretreatment reaction area is 5~40 DEG C high compared with the average reaction temperature in hydrotreating reaction area, preferably high by 10~
30℃。
In method of the invention, a reactor is can be set in hydrotreating reaction area, and more reactors also can be set,
Usually setting 2~5, is preferably provided with 2~3 reactors.The number of each catalyst in reactor bed is generally 1~5,
It is preferred that 1~3, if more than two catalyst beds are arranged, quenching hydrogen can be squeezed between bed, with control reaction temperature
Degree, successively loads Hydrodemetalation catalyst, Hydrobon catalyst along the flow direction of reaction stream in hydrotreating reaction area
With hydrodesulfurization nitrogen catalyst.In the method for the present invention, in each catalyst bed the loadings of catalyst can according to feedstock property,
The requirement of selected catalyst and product property is specifically chosen.
To reach better effect, more than two changeable weighted BMO spaces reaction zones can be used.It is described changeable
Meaning refers to provided with multiple weighted BMO spaces reaction zones, and each weighted BMO spaces reaction zone can individually be connected into subsequent add
Hydrogen handles reaction zone, can also individually cut out from hydrotreating reaction area.
Hydrotreating method according to the present invention, be arranged multiple changeable weighted BMO spaces reaction zones purpose be in order to
The catalyst in each reactor in hydrotreating reaction area is set to obtain lasting hydrogenation protecting, therefore, Mei Gejia by switching
As long as the number and connection relationship of hydrogen pretreatment reaction zone setting reactor meet the purpose that switching uses.Preferably, institute
The quantity for stating weighted BMO spaces reaction zone is 2, and 1 reactor is arranged in the weighted BMO spaces reaction zone, preferably with
Mode in parallel connects, and two weighted BMO spaces reaction zones one and only one be in on-line machining state.Weighted BMO spaces
Sequence filling hydrogenation protecting agent, Hydrodemetalation catalyst and Hydrobon catalyst, all kinds of protective agents and catalysis in reaction zone
The gradation mode of agent can be determined according to the property of raw material by this field Conventional wisdom.
In method of the invention, described two weighted BMO spaces reaction zones one and only one be online it is specific
It is meant that, when the first weighted BMO spaces reaction zone is unable to satisfy the feed needs or the first weighted BMO spaces of downstream hydrogenation treatment region
The pressure drop of at least one catalyst bed reaches in reaction zone when there is hot spot in the pressure drop upper limit or catalyst bed, by first plus
All reactors in hydrogen pretreatment reaction zone are cut out, while the reactor of the second weighted BMO spaces reaction zone being cut.When
Two weighted BMO spaces reaction zones are unable to satisfy the feed needs or the second weighted BMO spaces reaction zone of downstream hydrogenation processing reaction zone
In the pressure drop of at least one catalyst bed reach and occur hot spot in the pressure drop upper limit or catalyst bed and can not continue to operate
When, protective agent and catalyst whole in all reactors are replaced after can stopping work with device.It can also be according to hydrotreating reaction
The reactor of the second weighted BMO spaces reaction zone is cut out the case where catalyst activity in area, while protective agent will have been replaced and urged
Reactor incision in first weighted BMO spaces reaction zone of agent, so recycles, until the catalyst in hydrotreating reaction area
It is unable to satisfy running requirements.
There is no particular limitation to flow direction of the raw material in hydrogenation protecting area and hydrotreating zone by the present invention, weighted BMO spaces
Each reactor in reaction zone and hydrotreating reaction area both can may be downflow reactor for up-flow reactor.
Catalytic cracking recycle oil in method of the invention, into hydrotreating reaction area and weighted BMO spaces reaction zone
It can be the catalytic cracking recycle oil and catalytic cracking that catalytic cracking reaction zone in the method for the present invention obtains with catalytic cracked oil pulp
Slurry oil also may include catalytic cracking recycle oil and catalytic cracked oil pulp that other catalytic cracking units obtain.The method of the present invention
The catalytic cracking recycle oil that middle catalytic cracking reaction zone obtains is partly recycled to first, hydrotreating reaction area reactor inlet,
Another part is recycled to weighted BMO spaces reaction zone after mixing with catalytic cracked oil pulp, be recycled to first, hydrotreating reaction area
The recycle oil of reactor inlet accounts for 20% or more of the catalytic cracking recycle oil weight that catalytic cracking reaction zone obtains, preferably 30 ~
70%, the recycle oil for being recycled to weighted BMO spaces reaction zone accounts for catalytic cracking recycle oil weight that catalytic cracking reaction zone obtains
10% or more, preferably 20 ~ 50%, be recycled to first reactor inlet in hydrotreating reaction area recycle oil and be recycled to plus hydrogen it is pre-
Processing reaction zone recycle oil total amount generally at least account for the 30% of the catalytic cracking recycle oil weight that catalytic cracking reaction zone obtains with
On, preferably 50 ~ 95%, the catalytic cracking recycle oil of remainder is recycled back to catalytic cracking reaction zone.Catalytic cracking reaction zone obtains
Catalytic cracked oil pulp be recycled to weighted BMO spaces reaction zone, the catalytic cracked oil pulp for being recycled to weighted BMO spaces reaction zone is general
At least account for 30% or more of the catalytic cracked oil pulp weight that catalytic cracking reaction zone obtains, preferably 50 ~ 80%, the catalysis of remainder
Cracking slurry oil outlet.
It can also include: completely or partially to be recycled to the catalytic cracking diesel oil that catalytic cracking reaction zone obtains in the present invention
The last one reactor inlet of hydrotreating reaction area, the catalytic cracking diesel oil for being recycled to hydrotreating reaction area generally at least account for
10% or more, preferably 20 ~ 80% of the catalytic cracking diesel oil fraction weight that catalytic cracking reaction zone obtains, the catalysis of remainder is split
Catalytic cracking reaction zone can be recycled back to or as desired as product outlet by changing diesel oil.More preferably, it can also be wrapped in the present invention
The process that catalytic cracking diesel oil is cut into light fraction and heavy distillat is included, the temperature of the cutting is 245 ~ 300 DEG C.The weight
Fraction introduces the last one reactor inlet of hydrotreating reaction area, the light fraction introduce hydrotreating reaction area the last one
In the middle part of reactor.
It, can be further if there is solid impurity in catalytic cracking recycle oil and catalytic cracked oil pulp in the method for the present invention
It is recycled after removing.Solid impurity content in the catalytic cracking recycle oil and catalytic cracked oil pulp of the removing solid impurity
Less than 30mg/g, preferably smaller than 15mg/g, more preferably less than 5mg/g.
In method of the invention, catalytic cracking unit be can be more than a set of or a set of, and every covering device includes at least one
Fractionating column need to be arranged in reactor, a regenerator, catalytic cracking unit, fractionation can be respectively set with every set catalytic cracking unit
Tower can also share fractionating column.Fractionating column by catalytic cracking reaction effluent be fractionated for dry gas, liquefied gas, catalytically cracked gasoline,
Catalytic cracking diesel oil, catalytic cracking recycle oil and catalytic cracked oil pulp etc., the cut point of each fraction can according to need specific true
It is fixed.
In method of the invention, the operating condition of catalytic cracking reaction zone is general are as follows: 470~650 DEG C of reaction temperature, reaction
0.5~5 second time, catalyst and feedstock oil weight ratio 3~10,650~800 DEG C of catalyst regeneration temperature.Catalytic Cracking Unit of Measure
Device is answered to be generally the combination of riser reactor or riser and bed reactor.Catalytic cracking catalyst includes zeolite, inorganic
Oxide and optional clay, the weight content of each component are respectively as follows: zeolite 5%~50%, inorganic oxide 5%~95%, clay 0
~70%.Zeolite as active component, can selected from y-type zeolite, rare earth Y type zeolite (REY), rare earth hydrogen y-type zeolite (REHY),
One or more of ultrastable (USY), ZSM series zeolite and ZRP zeolite.Inorganic oxide is selected from as binder
Silica (SiO2) and/or alchlor (AL2O3).The clay is selected from kaolin and/or more water as matrix, i.e. carrier
Kaolin.
In the prior art, according to Flow of Goods and Materials direction in heavy oil hydroprocessing units, despite the presence of the influence of cold hydrogen, still
Low early and high after trend is generally presented in reaction temperature, i.e., in from start of run to the whole cycle in operating latter stage, hydrogen is added to protect
Protect a few class catalyst beds such as catalyst, Hydrodemetalation catalyst, Hydrobon catalyst and/or hydrodenitrogenation catalyst
Average reaction temperature is successively raised.Meanwhile setting of the existing catalyst grade with system is with all anti-when operating latter stage
Device is answered to reach synchronous inactivation, synchronize and change for the purpose of agent.Therefore, during operation, when the pressure drop rise of first reactor or
Need horse back whole device out of service to replace when there is hot spot or when hydrogenation products are not able to satisfy downstream unit requirement
Some catalyst.Catalyst in the hydrodesulfurization swum in such a case the lower and/or denitrification reactor also " has lost substantially
It is living ".Therefore the operation cycle of package unit is limited by first catalyst reactor service life.And even for adding
It is a whole set of for hydrogen protection is using the hydroprocessing technique (such as CN1484684A and CN102453530A) of reactor handover operation
The operation cycle of device is similarly subjected to the limitation of first catalyst reactor service life.
After having carried out a large amount of research to existing hydrotreating method, present inventor is surprised to find that: existing
In technology, after residual hydrocracking device is stopped work because of hot spot and/or the pressure drop of hydrogenation protecting catalyst bed, device rear portion
(downstream) although the desulphurization catalyst and denitrification catalyst that use also have inactivated, deactivation cause is more because of catalysis
Caused by the deposited metal blocking in the aperture in agent duct, and the metal deposited inside catalyst duct is really and few.Concrete analysis
Its reason, applicant think: the metal " penetrating " in the middle and later periods of residual hydrogenation equipment operating, feedstock oil in the prior art
Hydrogenation protecting catalyst and catalyst for demetalation bed, and it has been directly entered the desulphurization catalyst and denitrification catalyst bed at rear portion
Layer.Since the aperture of desulphurization catalyst and/or denitrification catalyst is smaller, the metal of removing be cannot be introduced into inside duct so sinking
Product is near catalyst aperture, so as to cause the inactivation of desulphurization catalyst and denitrification catalyst.In this condition, add hydrogen de-
The inactivation of sulfur catalyst and/or hydrodenitrogenation catalyst be not because catalyst itself carbon distribution and caused by, but because
After feedstock oil penetrates hydrogenation protecting catalyst bed and Hydrodemetalation catalyst bed, taken off so that should undertake and more add hydrogen
The desulfurization of sulphur and/or denitrification functions and/or denitrification catalyst undertake caused by the function of hydrodemetallization.Meanwhile it setting originally
After catalyst of the meter for desulfurization, denitrogenation and/or de- carbon residue undertakes partial hydrogenation demetalization function, due to its catalyst pore structure
Limitation, cannot also realize demetalization function well, while also creating desulfurization, denitrogenation and/or the reduction of de- carbon residue ability,
And the waste of catalyst function is caused, so that the activity of hydrodesulfurization and/or hydrodenitrogenation catalyst cannot obtain adequately
It utilizes.
A whole set of residual hydrogenation equipment can be divided into weighted BMO spaces reaction by numerous studies discovery by the present inventor
Area and hydrotreating reaction area, wherein weighted BMO spaces reaction zone operates under relatively high reaction temperature, and hydrotreating is anti-
Area is answered to operate under relatively low reaction temperature.The gold of weighted BMO spaces reaction zone outlet material is controlled in technical solution first
Belong to content, i.e. most of metal impurities in weighted BMO spaces reaction zone removing feedstock oil, remaining a small amount of more difficult removing
Metal impurities, while realizing partial hydro-desulfurization.And the hydrotreating reaction that the reaction stream of weighted BMO spaces reaction zone enters
Area is to operate at relatively low temperature, i.e., carries out hydrodesulfurization at relatively low temperature and add hydrogen saturated reaction, this
Sample metal impurities can directly pass through desulphurization catalyst and/or denitrification catalyst in the case where being not involved in reaction, so as to avoid
Catalyst is because of permanent deactivation caused by metal deposit.Product is made to meet the feed needs of downstream unit by scheme optimization.
Compared with prior art, method of the invention changes existing residual hydrogenation equipment catalyst system and operation mode, i.e., will show
It is low early and high after to have the tendency that technology is presented according to logistics orienting response temperature, changes into before being presented according to logistics orienting response temperature
Low trend after height, method of the invention can make full use of the activity of all catalyst of residual hydrogenation equipment, to increase residual oil
The operational efficiency of hydrogenation plant improves its economy.The present inventor completes the present invention on this basis.
In the prior art, has the technical solution that catalytic cracking recycle oil is recycled to residual hydrogenation equipment.But this hair
Bright people passes through the study found that the viscosity of resid feed can be reduced by mixing a small amount of catalytic cracking recycle oil in resid feed, promotees
The impurity removal of slag input oil reacts.But with the raising of catalytic cracking recycle oil mixed ratio, when residual hydrogenation equipment charging
After viscosity reduces to a certain extent, the mixed ratio of catalytic cracking recycle oil is continued growing, to residual hydrogenation removing impurities qualitative response
Facilitation will not further increase.Simultaneously because containing the heavy metals such as a large amount of Ni, V, carbon residue height, asphalitine in residual oil
Height, can seriously affect catalytic cracking recycle oil adds hydrogen effect.Therefore catalytic cracking recycle oil is divided into two parts by the present invention, and one
Flux oil of the part as residual oil raw material, another part are recycled to hydrotreating zone and weighted BMO spaces area part reaction effluent
Hydrotreating is carried out under higher hydrogen partial pressure and lower reaction temperature after mixing.Reduction residual oil raw material was both can achieve in this way
Viscosity, promotes the purpose of residual hydrogenation removing impurities qualitative response, while the hydrofinishing of catalytic cracking recycle oil also may be implemented, and improves
Catalytic cracking recycle oil adds the effect of hydrogen.In addition, the catalytic cracking recycle oil of low temperature position is recycled to hydrotreating zone, be conducive to adjust
The temperature for saving weighted BMO spaces area high-temperature position reaction effluent is conducive to the reaction temperature for controlling hydrotreating zone, can save
The equipment investments such as heat exchanger.
By contrast with distillate hydrogenation device, the general rear portion catalyst bed carbon deposit of residual hydrocracking device is serious,
And it is more closer to reactor outlet carbon deposit.This is primarily due to colloid and oil adds hydrogen saturated velocity fast, and asphalitine adds
Hydrogen saturated velocity is slow, and is easy broken side chain, only the high aromatic core of surplus aromaticity, thus the environment higher and higher in saturation degree
Solubility is smaller and smaller in solvent, is finally very easy to deposition and forms carbon deposit on a catalyst.After catalytic cracking recycle oil is added,
Surrounding solvent will can be improved to the peptizing power of asphalitine, reduce its deposition on the catalyst of rear portion, extend making for catalyst
Use the service life.In addition the partial hydrogenation product of polycyclic aromatic hydrocarbon is very strong hydrogen supply agent in catalytic cracking recycle oil, can reduce residual oil heat
Free radical condensation, inhibits the generation of coke precursor.These can all greatly reduce the carbon deposit of catalyst, reduce deactivation rate,
Extend the operation cycle.
Compared with prior art, the method have the advantages that:
1, by the way that heavy oil hydroprocessing units are divided into weighted BMO spaces reaction zone and hydrotreating reaction area, in weighted BMO spaces
Reaction zone removes most of metal impurities in material, makes poison of the material to hydrotreating zone catalyst for entering hydrotreating zone
Evil is greatly lowered, and can make full use of the activity of all catalyst in hydrotreating zone, compared with prior art, heavy-oil hydrogenation dress
The operation cycle set can extend 30-100%, to increase the operational efficiency of device, improve economy.
2, reactor is protected using switchable type in weighted BMO spaces reaction zone, substantially increases the demetalization energy of device
Power, so as to process the higher raw material of tenor.
3, since weighted BMO spaces reaction zone is stripped of most of metal impurities in material, so that hydrotreating reaction area
The deactivation cause of middle desulphurization catalyst and/or denitrification catalyst becomes only carbon deposit mistake from previous metal deposit and coking deactivation
It is living, so that desulphurization catalyst and denitrification catalyst can carry out regeneration treatment after using a cycle, it is greatly saved and urges
Agent buying expenses.
4, weighted BMO spaces area uses liquid-phase hydrogenatin, on the one hand realizes the purpose for reducing catalyst bed temperature rise, can have
Effect avoids the generation of hot spot, at the same also significantly reduce between bed and/or between reactor quenching hydrogen injection rate, on the other hand pass through
It crosses plus the recycle oil of hydrogen is saturated part aromatic hydrocarbons, have the function of hydrogen supply, coke formation can be inhibited, avoid catalyst
Coking deactivation, and then extend the service life of catalyst.
5, weighted BMO spaces area is not provided with hydrogen gas circulating system, and reaction system is entrained into when largely recycling by liquid-phase product
Dissolved hydrogen come provide fresh feed carry out hydrogenation reaction required for hydrogen, can eliminate catalyst wetting Effects of Factors and
H in recycle hydrogen2S and NH3Influence, while also reduce single unit system circulation hydrogen system equipment investment.
It is 6, of the invention by the way that the first high-pressure separator is arranged between weighted BMO spaces reaction zone and hydrotreating reaction area,
On the one hand significantly reducing the impurity such as hydrogen sulfide and ammonia in recycle oil is greatly facilitated catalysis to the adverse effect of hydrogenation reaction
The progress of reaction, simultaneously because the diluting effect of recycle oil, is adapted to the demand of processing high impurity content raw material, improves work
The adaptability of skill process；On the other hand, so that being obtained into the impurity concentrations such as hydrogen sulfide and ammonia in the material in hydrotreating reaction area
To reduce, and then it is minimized the reaction temperature in hydrotreating reaction area, to further extend in hydrotreating reaction area
The operation cycle of catalyst.
7, the activity for making full use of the catalyst in hydrotreating reaction area, improves the treating capacity of device, or reduces
Equipment investment.The catalytic cracking recycle oil of low temperature position is recycled to hydrotreating zone, is conducive to adjust weighted BMO spaces area high-temperature position
The temperature of reaction effluent is conducive to the reaction temperature for controlling hydrotreating zone, can save the equipment investments such as heat exchanger.
8, catalytic cracking recycle oil and catalytic cracked oil pulp are recycled to weighted BMO spaces area and hydrotreating zone respectively, it can
The imurity-removal in hydrogenation process, aromatic hydrocarbons saturation become better catalytically cracked material composition, further improve catalytic cracking
High addition product yield.
9, in the method for the present invention, catalytic cracked oil pulp and partially catalyzed cracking recycle oil are recycled to as flux oil and add hydrogen pre-
Entrance of the treatment zone can reduce the viscosity of residual oil raw material, improve the flow distribution and mass transfer of raw material in the reactor, and reduction is diffused in
Influence during residual hydrocracking improves the deposition distributions of the metals in reaction system such as nickel, vanadium, extends making for catalyst
Use the service life.Catalytic cracking recycle oil is recycled to weighted BMO spaces area and hydrotreating zone, and surrounding solvent will can be improved to asphalitine
Peptizing power, reduce its deposition on the catalyst of rear portion, extend the service life of catalyst.In addition catalytic cracking recycle oil
The partial hydrogenation product of middle polycyclic aromatic hydrocarbon is very strong hydrogen supply agent, can reduce the condensation of residual oil hot radical, inhibit coke precursor
Generation.These can all greatly reduce the carbon deposit of catalyst, reduce deactivation rate, extend the operation cycle.
10, in the method for the present invention, catalytic cracking diesel oil is recycled to the last one reactor inlet of hydrotreating reaction area, can
Improve the deposition distributions of the metals in reaction system such as nickel, vanadium, extends the service life of catalyst；Moreover, by catalytic cracking bavin
Oil is recycled to the last one reactor inlet of hydrotreating reaction area, and can be avoided must be at last in the method for the prior art
The step of introducing cold hydrogen between a reactor and penultimate reactor, and the cold hydrogen substituted can be in hydrotreating reaction
First, area reactor inlet enters in reaction system the introduction volume for increasing hydrogen, increases hydrogen to oil volume ratio, improves reactor
The hydrogen partial pressure of entrance, to be conducive to the progress of subsequent reactions；The lower reaction temperature in hydrotreating reaction area, is conducive to be catalyzed
Aromatic hydrocarbons saturation in cracked diesel oil.
Detailed description of the invention
Fig. 1 is a kind of flow diagram of the method for the present invention.
Fig. 2 is another flow diagram of the method for the present invention.
Specific embodiment
Below in conjunction with attached drawing, detailed description of the preferred embodiments.It should be understood that this place is retouched
The specific embodiment stated is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
Attached drawing is the principle process schematic diagram of method provided by the present invention, and many necessaries are omitted in figure (as heated
Furnace, heat exchanger, pump, valve etc.).
A kind of process of the method for group technology processing low grade oils provided by the present invention is as follows:
It first comes from fresh feed residual oil, the catalytic cracking recycle oil from pipeline 40 and the catalytic cracked oil pulp of pipeline 8, come from
The new hydrogen of pipeline 22 and enters mixer 24 together through the first product liquid that pipeline 15 is recycled back to and formed and be saturated molten hydrogen logistics；It is full
Enter in the reactor 1 of the first weighted BMO spaces reaction zone with molten hydrogen stream passes via line 23 and pipeline 10, in the presence of a catalyst
Carry out hydrodesulfurization and hydrodemetallization reaction；Hydrogenation products are from 1 top of reactor of the first weighted BMO spaces reaction zone through pipe
Line 9 and pipeline 13 enter the first high-pressure separator 5 and carry out gas-liquid separation；Separating obtained first hydrogen-rich gas 14 is after further treatment
It is recycled after compressor compresses after isolating hydrogen；Separating obtained first product liquid a part is recycled back to through pipeline 15 to be added
Hydrogen pretreatment area, another part through pipeline 16 and the catalytic cracking recycle oil from pipeline 39, the supplement hydrogen from pipeline 25 and
After mixing hydrogen mixing from pipeline 21, the reactor 3, pipeline 17 and reactor 4 in hydrotreating reaction area are passed sequentially through, is being urged
Hydrodesulfurization and hydrodenitrogeneration reaction are carried out in the presence of agent, reaction effluent carries out gas into the second separator 6 through pipeline 18
Liquid separation, separator 6 generally include high-pressure separator and low pressure separator；Separating obtained second hydrogen-rich gas is taken out through pipeline 20
Out, it is recycled after the pressurization of compressor 7, obtained second liquid enters fractionating column 26 through the extraction of pipeline 19 and separated, and obtains
To gas, naphtha, hydrogenated diesel oil and residual hydrogenation tail oil, extracted out respectively through pipeline 27, pipeline 28, pipeline 29 and pipeline 30.
Residual hydrogenation tail oil from pipeline 30 enters catalytic cracking reaction zone 31, in the presence of catalytic cracking catalyst into
Row cracking reaction, after reaction oil gas be fractionated after obtain gas, catalytic gasoline, catalytic cracking diesel oil, catalytic cracking recycle oil and
Catalytic cracked oil pulp.Dry gas, liquefied gas and catalytic gasoline go out device through pipeline 32,33 and 34 respectively.Catalytic cracking diesel oil is through pipe
Line 35 is recycled back to catalytic cracking reaction zone or as desired as product outlet.Catalytic cracking recycle oil is divided into two parts, and one
Lease making pipeline 36 and pipeline 38 mixed with catalytic cracked oil pulp 37 after as flux oil through pipeline 40 with from the fresh original of pipeline 8
The new hydrogen (hydrogen) of material residue is oily, is recycled back to through pipeline 15 weighted BMO spaces area recycle oil and pipeline 22 enters mixer 24 together
It is formed and is saturated molten hydrogen logistics, another part is recycled to 3 entrance of hydrotreating reaction area reactor through pipeline 36 and pipeline 39, in slag
It is reacted under the action of oil hydrogenation catalysts.
Fig. 2 is another flow diagram for the method that a kind of group technology of the present invention handles low grade oils, not with Fig. 1
It is with place, catalytic cracking diesel oil is recycled to 4 entrance of hydrotreating reaction area reactor through pipeline 35.
When the reactor 1 of the first weighted BMO spaces reaction zone is unable to satisfy feed needs or the reaction of downstream hydrogenation treatment region
The pressure drop of at least one catalyst bed reaches in device 1 when there is hot spot in the pressure drop upper limit or catalyst bed, is cut out, and
The reactor 2(material for cutting the second weighted BMO spaces reaction zone enters reactor 2 through pipeline 12, through 11 outflow reactor of pipeline
2) hydroprocessing processes are continued to complete, while replacing the catalyst in the first weighted BMO spaces reaction zone reactor 1, are filled again
It is stand-by to enter fresh catalyst.When the reactor 2 of the second weighted BMO spaces reaction zone is unable to satisfy downstream hydrogenation processing reaction zone
The pressure drop of at least one catalyst bed reaches the pressure drop upper limit in feed needs or reactor 2 or the interior appearance of catalyst bed can not
It when continuing the hot spot of operation, is cut out, while cutting the reactor 1 of the first weighted BMO spaces reaction zone and adding hydrogen to continue to complete
Treatment process, while the catalyst in the reactor 2 of the second weighted BMO spaces reaction zone of replacement, reload fresh catalyst and wait for
With.So circulation, the service life of the catalyst until reaching hydrotreating zone.
It is limited below in conjunction with specific embodiment is further to method of the invention.Original used in Examples and Comparative Examples
The property of material oil is listed in table 1, and the property of catalyst for hydrotreatment of residual oil used is listed in table 2.In table 2, A is hydrogenation protecting catalysis
Agent, B are Hydrodemetalation catalyst, and C is Hydrobon catalyst, and D is hydrodenitrogeneration (carbon residue conversion) catalyst.Embodiment and
Catalytic cracking catalyst used in comparative example is identical, is 3,500,000 tons/year of heavy oil catalytically cracking equipments of Dalian Company
The catalyst used, for industrial equilibrium catalyst.Its fresh dose composition are as follows: 95wt%LBO-16 olefine lowering catalyst+5wt%
LBO-A improves octane enhancing additive.
1 raw material oil nature of table
2 catalyst property of table
Embodiment 1
According to process flow described in Fig. 1, weighted BMO spaces reaction zone includes the first weighted BMO spaces reaction of changeable operation
A reactor 1 is arranged in area and the second weighted BMO spaces reaction zone, the first weighted BMO spaces reaction zone, and the second weighted BMO spaces are anti-
Answer area that one reactor 2 is set, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series.According to Flow of Goods and Materials
Direction is filled in weighted BMO spaces reaction zone (in operation process only have a weighted BMO spaces reaction zone online) reactor and urges
Agent A, catalyst B and catalyst C, the admission space ratio of each catalyst are 2: 7: 1.It is filled in hydrotreating reaction area reactor 3
There are catalyst B and catalyst C, the admission space ratio of two kinds of catalyst is 1: 9, and loading catalyst D in reactor 4.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is compared with hydrotreating zone height, specific reaction condition and slag
Oily hydrogenation reaction the results are shown in Table 3, and Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 5, and catalytic cracking product is distributed and catalytically cracked gasoline property
It is shown in Table 6.Feedstock oil A is followed by mixer 24, reactor 1, the first high-pressure separator 5, reactor 3, reactor 4 and second point
From device 6, the separating obtained effluent a part of the first high-pressure separator 5 is recycled to mixer 24(recycle ratio 0.3:1), another part
For effluent followed by reactor 3 and reactor 4 and the second separator 6, reaction effluent enters Catalytic Cracking Unit of Measure after being fractionated
Area is answered, the catalytic cracked oil pulp of catalytic cracking reaction zone whole is recycled to the 40% of whole catalytic cracking recycle oils plus hydrogen is pre-
Reaction zone is handled, is recycled to hydrotreating reaction area reactor for the 40% of catalytic cracking reaction zone whole catalytic cracking recycle oil
3, the straight connecting device of catalytic cracking diesel oil, and metal (Ni+V) content for controlling weighted BMO spaces reaction zone outlet effluent is not high
In 12mg/g.In hydrogenated back end hydrogenation processing reaction zone effluent sulfur content be 0.21 weight %, it is nitrogen content 2018mg/g, residual
Charcoal value is 4.56 weight %, metal (Ni+V) content is 7.46mg/g.Operating 6 months after, the first weighted BMO spaces reaction zone it is anti-
Answer device 1 export effluent metal (Ni+V) content be more than at least one catalyst bed in 12mg/g or reactor 1 pressure drop
Reach in the pressure drop upper limit or catalyst bed and hot spot occur, cut out, and cuts the reaction of the second weighted BMO spaces reaction zone
(feedstock oil A is at this time followed by mixer 24, reactor 2, the first high-pressure separator to continue to complete hydroprocessing processes for device 2
5, reactor 3, reactor 4 and the second separator 6), device still even running, generate oil quality can satisfy downstream RFCC into
Material requires.When the second weighted BMO spaces reaction zone reactor 2 export effluent metal (Ni+V) content be more than 12mg/g or
The pressure drop of at least one catalyst bed, which reaches, in reactor 2 occurs that operation can not be continued in the pressure drop upper limit or catalyst bed
It when hot spot, is cut out, while the reactor 1 for cutting the first weighted BMO spaces reaction zone continues to complete hydroprocessing processes,
The catalyst in the reactor 2 of the second weighted BMO spaces reaction zone is replaced simultaneously, and it is stand-by to reload fresh catalyst.So follow
Ring, the final residual hydrogenation equipment have operated 24 months, since product quality variation is stopped work, operate present invention device 1
It is loaded and unloaded respectively agent 2 times with reactor 2.
Comparative example 1
According to process flow described in Fig. 1, weighted BMO spaces reaction zone includes the first weighted BMO spaces reaction of changeable operation
A reactor 1 is arranged in area and the second weighted BMO spaces reaction zone, the first weighted BMO spaces reaction zone, and the second weighted BMO spaces are anti-
Answer area that one reactor 2 is set, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series.According to Flow of Goods and Materials
Direction is filled in weighted BMO spaces reaction zone (in operation process only have a weighted BMO spaces reaction zone online) reactor and urges
Agent A, catalyst B and catalyst C, the admission space ratio of each catalyst are 2: 7: 1.It is filled in hydrotreating reaction area reactor 3
There are catalyst B and catalyst C, the admission space ratio of two kinds of catalyst is 1: 9, and loading catalyst D in reactor 4.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is lower than hydrotreating zone, specific reaction condition and slag
Oily hydrogenation reaction the results are shown in Table 3, and Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 5, and catalytic cracking product is distributed and catalytically cracked gasoline property
It is shown in Table 6.Feedstock oil A is followed by mixer 24, reactor 1, the first high-pressure separator 5, reactor 3, reactor 4 and second point
From device 6, the separating obtained effluent a part of the first high-pressure separator 5 is recycled to mixer 24(recycle ratio 0.3:1), another part
For effluent followed by reactor 3 and reactor 4 and the second separator 6, reaction effluent enters Catalytic Cracking Unit of Measure after being fractionated
Area is answered, the catalytic cracked oil pulp of catalytic cracking reaction zone whole is recycled to the 40% of whole catalytic cracking recycle oils plus hydrogen is pre-
Reaction zone is handled, is recycled to hydrotreating reaction area reactor for the 40% of catalytic cracking reaction zone whole catalytic cracking recycle oil
3, the straight connecting device of catalytic cracking diesel oil, and metal (Ni+V) content of weighted BMO spaces reaction zone outlet effluent is not controlled.
Sulfur content is 0.22 weight %, nitrogen content 2167mg/g, carbon residue 4.76 in hydrogenated back end hydrogenation processing reaction zone effluent
Weight %, metal (Ni+V) content are 9.67mg/g.After operating 10 months, in the reactor 1 of the first weighted BMO spaces reaction zone extremely
The pressure drop of a few catalyst bed, which reaches in the pressure drop upper limit or catalyst bed, there is hot spot, is cut out, and cut second
The reactor 2 of weighted BMO spaces reaction zone come continue to complete hydroprocessing processes (at this time feedstock oil A followed by mixer 24,
Reactor 2, the first high-pressure separator 5, reactor 3, reactor 4 and the second separator 6), device still even running generates oil
Quality can satisfy downstream RFCC feed needs.After switching reactor 2, which has operated 7.5 months again, due to
Product quality variation is stopped work, and the final device has operated 17.5 months.
Embodiment 2
According to process flow described in Fig. 1, weighted BMO spaces reaction zone includes the first weighted BMO spaces reaction of changeable operation
A reactor 1 is arranged in area and the second weighted BMO spaces reaction zone, the first weighted BMO spaces reaction zone, and the second weighted BMO spaces are anti-
Answer area that one reactor 2 is set, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series.According to Flow of Goods and Materials
Direction is filled in weighted BMO spaces reaction zone (in operation process only have a weighted BMO spaces reaction zone online) reactor and urges
Agent A, catalyst B and catalyst C, the admission space ratio of each catalyst are 3: 6: 1.It is filled in hydrotreating reaction area reactor 3
There are catalyst B and catalyst C, the admission space ratio of two kinds of catalyst is 3: 7, loading catalyst C and catalyst D in reactor 4,
The admission space ratio of two kinds of catalyst is 2: 8.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is compared with hydrotreating zone height, specific reaction condition and slag
Oily hydrogenation reaction the results are shown in Table 4, and Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 5, and catalytic cracking product is distributed and catalytically cracked gasoline property
It is shown in Table 6.Feedstock oil B is followed by mixer 24, reactor 1, the first high-pressure separator 5, reactor 3, reactor 4 and second point
From device 6, the separating obtained effluent a part of the first high-pressure separator 5 is recycled to mixer 24(recycle ratio 0.5:1), another part
For effluent followed by reactor 3 and reactor 4 and the second separator 6, reaction effluent enters Catalytic Cracking Unit of Measure after being fractionated
Area is answered, the catalytic cracked oil pulp of catalytic cracking reaction zone whole is recycled to the 25% of whole catalytic cracking recycle oils plus hydrogen is pre-
Reaction zone is handled, is recycled to hydrotreating reaction area reactor for the 25% of catalytic cracking reaction zone whole catalytic cracking recycle oil
3, the straight connecting device of catalytic cracking diesel oil, and metal (Ni+V) content for controlling weighted BMO spaces reaction zone outlet effluent is not high
In 20mg/g.In hydrogenated back end hydrogenation processing reaction zone effluent sulfur content be 0.23 weight %, it is nitrogen content 1558mg/g, residual
Charcoal value is 3.92 weight %, metal (Ni+V) content is 9.90mg/g.Operating 3 months after, the first weighted BMO spaces reaction zone it is anti-
Answer device 1 export effluent metal (Ni+V) content be more than at least one catalyst bed in 20mg/g or reactor 1 pressure drop
Reach in the pressure drop upper limit or catalyst bed and hot spot occur, cut out, and cuts the reaction of the second weighted BMO spaces reaction zone
(feedstock oil B is at this time followed by mixer 24, reactor 2, the first high-pressure separator to continue to complete hydroprocessing processes for device 2
5, reactor 3, reactor 4 and the second separator 6), device still even running, generate oil quality can satisfy downstream RFCC into
Material requires.When the second weighted BMO spaces reaction zone reactor 2 export effluent metal (Ni+V) content be more than 20mg/g or
The pressure drop of at least one catalyst bed, which reaches, in reactor 2 occurs that operation can not be continued in the pressure drop upper limit or catalyst bed
It when hot spot, is cut out, while the reactor 1 for cutting the first weighted BMO spaces reaction zone continues to complete hydroprocessing processes,
The catalyst in the reactor 2 of the second weighted BMO spaces reaction zone is replaced simultaneously, and it is stand-by to reload fresh catalyst.So follow
Ring, the final residual hydrogenation equipment have operated 12 months, since product quality variation is stopped work, operate present invention device 1
It is loaded and unloaded respectively agent 2 times with reactor 2.
Embodiment 3
According to process flow described in Fig. 1, weighted BMO spaces reaction zone includes the first weighted BMO spaces reaction of changeable operation
A reactor 1 is arranged in area and the second weighted BMO spaces reaction zone, the first weighted BMO spaces reaction zone, and the second weighted BMO spaces are anti-
Answer area that one reactor 2 is set, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series.According to Flow of Goods and Materials
Direction is filled in weighted BMO spaces reaction zone (in operation process only have a weighted BMO spaces reaction zone online) reactor and urges
Agent A, catalyst B and catalyst C, the admission space ratio of each catalyst are 4: 5: 1.It is filled in hydrotreating reaction area reactor 3
There are catalyst B and catalyst C, the admission space ratio of two kinds of catalyst is 1: 9, loading catalyst D in reactor 4.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is compared with hydrotreating zone height, specific reaction condition and slag
Oily hydrogenation reaction the results are shown in Table 4, and Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 5, and catalytic cracking product is distributed and catalytically cracked gasoline property
It is shown in Table 6.Feedstock oil C is followed by mixer 24, reactor 1, the first high-pressure separator 5, reactor 3, reactor 4 and second point
From device 6, the separating obtained effluent a part of the first high-pressure separator 5 is recycled to mixer 24(recycle ratio 0.7:1), another part
For effluent followed by reactor 3 and reactor 4 and the second separator 6, reaction effluent enters Catalytic Cracking Unit of Measure after being fractionated
Area is answered, the 80% of catalytic cracking reaction zone whole catalytic cracked oil pulp is recycled to the 20% of whole catalytic cracking recycle oils and adds hydrogen
Pretreatment reaction area is recycled to the reaction of hydrotreating reaction area for the 20% of catalytic cracking reaction zone whole catalytic cracking recycle oil
Device 3, the straight connecting device of catalytic cracking diesel oil, and control metal (Ni+V) content of weighted BMO spaces reaction zone outlet effluent not
Higher than 10mg/g.In hydrogenated back end hydrogenation processing reaction zone effluent sulfur content be 0.18 weight %, nitrogen content 2617mg/g,
Carbon residue is 3.65 weight %, metal (Ni+V) content is 5.77mg/g.After operating 4 months, the first weighted BMO spaces reaction zone
Metal (Ni+V) content of the outlet of reactor 1 effluent is more than the pressure of at least one catalyst bed in 10mg/g or reactor 1
Drop, which reaches in the pressure drop upper limit or catalyst bed, there is hot spot, is cut out, and cuts the anti-of the second weighted BMO spaces reaction zone
Answering device 2, (feedstock oil C is at this time followed by mixer 24, reactor 2, the separation of the first high pressure to continue to complete hydroprocessing processes
Device 5, reactor 3, reactor 4 and the second separator 6), device still even running, generating oil quality can satisfy downstream RFCC
Feed needs.It is more than 10mg/g when the reactor 2 of the second weighted BMO spaces reaction zone exports metal (Ni+V) content of effluent
Or the pressure drop of at least one catalyst bed reaches and occurs not continuing to operate in the pressure drop upper limit or catalyst bed in reactor 2
Hot spot when, cut out, while the reactor 1 for cutting the first weighted BMO spaces reaction zone continues to complete hydrotreating
Journey, while the catalyst in the reactor 2 of the second weighted BMO spaces reaction zone of replacement, it is stand-by to reload fresh catalyst.Such as
This circulation, the final residual hydrogenation equipment have operated 16 months, since product quality variation is stopped work, operate present invention
Device 1 and reactor 2 load and unload agent 2 times respectively.
Embodiment 4
According to process flow described in Fig. 2, weighted BMO spaces reaction zone includes the first weighted BMO spaces reaction of changeable operation
A reactor 1 is arranged in area and the second weighted BMO spaces reaction zone, the first weighted BMO spaces reaction zone, and the second weighted BMO spaces are anti-
Answer area that one reactor 2 is set, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series.According to Flow of Goods and Materials
Direction is filled in weighted BMO spaces reaction zone (in operation process only have a weighted BMO spaces reaction zone online) reactor and urges
Agent A, catalyst B and catalyst C, the admission space ratio of each catalyst are 3: 6: 1.It is filled in hydrotreating reaction area reactor 3
There are catalyst B and catalyst C, the admission space ratio of two kinds of catalyst is 1: 9, and loading catalyst D in reactor 4.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is compared with hydrotreating zone height, specific reaction condition and slag
Oily hydrogenation reaction the results are shown in Table 4, and Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 5, and catalytic cracking product is distributed and catalytically cracked gasoline property
It is shown in Table 6.Feedstock oil A is followed by mixer 24, reactor 1, the first high-pressure separator 5, reactor 3, reactor 4 and second point
From device 6, the separating obtained effluent a part of the first high-pressure separator 5 is recycled to mixer 24(recycle ratio 0.3:1), another part
For effluent followed by reactor 3 and reactor 4 and the second separator 6, reaction effluent enters Catalytic Cracking Unit of Measure after being fractionated
Area is answered, whole catalytic cracked oil pulp of catalytic cracking reaction zone is recycled to the 40% of whole catalytic cracking recycle oils and adds hydrogen
It is anti-to be recycled to hydrotreating reaction area for the 40% of whole catalytic cracking recycle oils of catalytic cracking reaction zone for pretreatment reaction area
Device 3 is answered, is recycled to 4 entrance of hydrotreating reaction area reactor for the 70% of catalytic cracking reaction zone whole catalytic cracking diesel oil, and
Metal (Ni+V) content for controlling weighted BMO spaces reaction zone outlet effluent is not higher than 12mg/g.Hydrogenated back end hydrogenation processing is anti-
Answer in area's effluent that sulfur content is 0.21 weight %, nitrogen content 2011mg/g, carbon residue are 4.51 weight %, metal (Ni+V) contains
Amount is 7.10mg/g.After operating 6 months, the reactor 1 of the first weighted BMO spaces reaction zone exports the metal (Ni+V) of effluent
Content is more than that the pressure drop of at least one catalyst bed in 12mg/g or reactor 1 reaches in the pressure drop upper limit or catalyst bed
Existing hot spot, is cut out, and cuts the reactor 2 of the second weighted BMO spaces reaction zone to continue to complete hydroprocessing processes (this
When feedstock oil A followed by mixer 24, reactor 2, the first high-pressure separator 5, reactor 3, reactor 4 and the second separator
6), device still even running, generating oil quality can satisfy downstream RFCC feed needs.When the second weighted BMO spaces reaction zone
Reactor 2 export effluent metal (Ni+V) content be more than at least one catalyst bed in 12mg/g or reactor 2
Pressure drop reaches in the pressure drop upper limit or catalyst bed when there is not continuing the hot spot of operation, is cut out, while cutting first
The reactor 1 of weighted BMO spaces reaction zone continues to complete hydroprocessing processes, while replacing the second weighted BMO spaces reaction zone
Reactor 2 in catalyst, it is stand-by to reload fresh catalyst.So circulation, the final residual hydrogenation equipment operate
It 24 months, since product quality variation is stopped work, operates present invention device 1 and reactor 2 loads and unloads agent 2 times respectively.
Embodiment 5
According to process flow described in Fig. 2, weighted BMO spaces reaction zone includes the first weighted BMO spaces reaction of changeable operation
A reactor 1 is arranged in area and the second weighted BMO spaces reaction zone, the first weighted BMO spaces reaction zone, and the second weighted BMO spaces are anti-
Answer area that one reactor 2 is set, hydrotreating reaction area includes the reactor 3 and reactor 4 being arranged in series.According to Flow of Goods and Materials
Direction is filled in weighted BMO spaces reaction zone (in operation process only have a weighted BMO spaces reaction zone online) reactor and urges
Agent A, catalyst B and catalyst C, the admission space ratio of each catalyst are 3: 6: 1.It is filled in hydrotreating reaction area reactor 3
There are catalyst B and catalyst C, the admission space ratio of two kinds of catalyst is 2: 8, loading catalyst C and catalyst D in reactor 4,
The admission space ratio of two kinds of catalyst is 2: 8.
In operation process, the reaction temperature of weighted BMO spaces reaction zone is compared with hydrotreating zone height, specific reaction condition and slag
Oily hydrogenation reaction the results are shown in Table 4, and Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 5, and catalytic cracking product is distributed and catalytically cracked gasoline property
It is shown in Table 6.Feedstock oil C is followed by mixer 24, reactor 1, the first high-pressure separator 5, reactor 3, reactor 4 and second point
From device 6, the separating obtained effluent a part of the first high-pressure separator 5 is recycled to mixer 24(recycle ratio 0.7:1), another part
For effluent followed by reactor 3 and reactor 4 and the second separator 6, reaction effluent enters Catalytic Cracking Unit of Measure after being fractionated
Area is answered, the 80% of catalytic cracking reaction zone whole catalytic cracked oil pulp is recycled to the 20% of whole catalytic cracking recycle oils and adds hydrogen
Pretreatment reaction area is recycled to the reaction of hydrotreating reaction area for the 20% of catalytic cracking reaction zone whole catalytic cracking recycle oil
Device 3 is cut into LCO light fraction and LCO heavy distillat for the 30% of catalytic cracking reaction zone whole catalytic cracking diesel oil (LCO), cutting
Point is 275 DEG C, and LCO heavy distillat is recycled to 4 entrance of hydrotreating reaction area reactor, and it is anti-that LCO light fraction is recycled to hydrotreating
4 middle part of area's reactor is answered, and metal (Ni+V+Fe+Ca) content for controlling weighted BMO spaces reaction zone outlet effluent is not higher than
10mg/g.Sulfur content is 0.16 weight %, nitrogen content 2603mg/g, carbon residue in hydrogenated back end hydrogenation processing reaction zone effluent
Value is 3.58 weight %, metal (Ni+V) content is 5.30mg/g, and metal Ca content is 0.65mg/g, and metal Fe content is
0.30mg/g.After operating 4 months, the reactor 1 of the first weighted BMO spaces reaction zone exports the metal (Ni+V+Fe+ of effluent
Ca) content is more than that the pressure drop of at least one catalyst bed in 10mg/g or reactor 1 reaches the pressure drop upper limit or catalyst bed
Inside there is hot spot, cut out, and cuts the reactor 2 of the second weighted BMO spaces reaction zone to continue to complete hydroprocessing processes
(feedstock oil C is at this time followed by mixer 24, reactor 2, the first high-pressure separator 5, reactor 3, reactor 4 and second point
From device 6), device still even running, generating oil quality can satisfy downstream RFCC feed needs.When the second weighted BMO spaces are anti-
Answering the reactor 2 in area to export metal (Ni+V+Fe+Ca) content of effluent is more than that at least one in 10mg/g or reactor 2 is urged
The pressure drop of agent bed reaches in the pressure drop upper limit or catalyst bed when there is not continuing the hot spot of operation, is cut out, together
When cut the reactor 1 of the first weighted BMO spaces reaction zone to continue to complete hydroprocessing processes, while replace second plus hydrogen it is pre-
The catalyst in the reactor 2 of reaction zone is handled, it is stand-by to reload fresh catalyst.So circulation, the final residual hydrogenation
Device has operated 16 months, since product quality variation is stopped work, operates present invention device 1 and reactor 2 loads and unloads respectively
Agent 2 times.
The condition and test result of 3 hydrotreating of table
The condition and test result of 4 hydrotreating of table
5 Hydrocarbon Content by Catalytic Cracking Operation condition of table
The distribution of 6 catalytic cracking product of table and catalytically cracked gasoline property
In order to further investigate the influence of technology of the invention to hydrotreating reaction area catalyst, respectively to embodiment 1
Catalyst C and catalyst D after operating with comparative example 1 are dissected, and the results are shown in Table 7 and table 8.
Wherein, catalyst sample dissects analysis method used: carrying out C using Japan's production EMZA-820V elemental analyser and contains
It is fixed to measure；Metal deposition capability is carried out using IRIS HR plasma emission spectrum (ICP) instrument of Thermo Fisher company, the U.S.
Measurement；Catalyst pore structure property analysis uses low temperature N2Absorption method, instrument are that ASAP2420 type Full-automatic physical adsorption instrument (divides
Analysis method is GB/T-19587).
7 catalyst C of table operating front and back dissects result
8 catalyst D of table dissects result
As seen from the above analysis, by changing residual hydrogenation equipment catalyst system and operation mode, i.e., by the prior art
Low early and high after trend (comparative example 1) is presented according to logistics orienting response temperature, changes into and is according to logistics orienting response temperature
The existing trend (embodiment 1) that the front is high and the back is low can make full use of the activity of all catalyst while guaranteeing product quality,
Since weighted BMO spaces reaction zone is stripped of most of metal impurities in material, so that desulfurization catalyst in hydrotreating reaction area
The deactivation cause of agent and/or denitrification catalyst is from becoming only carbon deposit using the metal deposit and coking deactivation of prior art technology
Inactivation, effectively increases the utilization rate of desulphurization catalyst and/or denitrification catalyst, while urge desulphurization catalyst and denitrogenation
Agent can carry out regeneration treatment after using a cycle, reuse, saved catalyst buying expenses, improved economy
Property.
Claims (12)
1. a kind of method of group technology processing low grade oils, including the following contents:
(1) at least one weighted BMO spaces reaction zone, a hydrotreating reaction area and a catalytic cracking reaction zone are provided；Add
Include hydrogenation protecting catalyst and Hydrodemetalation catalyst in hydrogen pretreatment reaction zone, includes adding hydrogen in hydrotreating reaction area
Desulphurization catalyst and hydrodenitrogenation catalyst include catalytic cracking catalyst in catalytic cracking reaction zone；
(2) inferior feedstock oil, the recycle oil in weighted BMO spaces area, catalytic cracked oil pulp, partially catalyzed cracking recycle oil and hydrogen
Enter mixer together to form the molten hydrogen logistics of saturation and gaseous hydrogen is discharged；
(3) the molten hydrogen logistics of saturation from step (2) enters weighted BMO spaces reaction zone, and liquid is carried out under the conditions of weighted BMO spaces
Metal impurities are removed 40wt%~90wt% by phase hydrogenation reaction, and sulphur is removed 20wt%~70wt%, obtain tenor reduction
Reaction effluent；
(4) reaction effluent obtained by step (3) is separated into the first high-pressure separator, obtains the first hydrogen-rich gas and the first liquid
Body；
(5) first liquid a part obtained by step (4) is recycled back to weighted BMO spaces reaction zone, another part and partially catalyzed cracking
Enter hydrotreating reaction area after recycle oil mixing, carries out hydrogenation reaction under hydroprocessing conditions；
(6) reaction effluent obtained by step (5) enters the progress gas-liquid separation of the second separator, obtains the second hydrogen-rich gas and second
Liquid；
(7) second liquid product obtained by step (6) enters fractionating column, obtains gas, naphtha, hydrogenated diesel oil and hydrogenation tail oil；
(8) hydrogenation tail oil obtained by step (7) enters catalytic cracking reaction zone, and it is anti-that cracking is carried out in the presence of catalytic cracking catalyst
It answers, reaction generates after oil is fractionated and obtains dry gas, liquefied gas, catalytically cracked gasoline, catalytic cracking diesel oil, catalytic cracking recycle oil
And catalytic cracked oil pulp；
(9) catalytic cracking recycle oil obtained by step (8) is divided into two parts, and a part is used as flux oil after mixing with catalytic cracked oil pulp
Mixer before being recycled back to weighted BMO spaces reactor, another part are recycled to first, hydrotreating reaction area reactor and enter
Mouthful；
Wherein, the average reaction temperature t1 of the weighted BMO spaces reaction zone is higher than the average response in the hydrotreating reaction area
5~40 DEG C of t2 high of temperature t2, preferably t1 ratio, 10~30 DEG C of t2 high of more preferable t1 ratio.
2. according to the method for claim 1, which is characterized in that it is anti-to provide more than two weighted BMO spaces in step (1)
Area is answered, which is usually the reaction zone that is arranged in parallel, can be switched operation.
3. according to the method for claim 1, which is characterized in that the tenor of the inferior feedstock oil is greater than 30mg/g.
4. according to method described in claim 1 or 3, which is characterized in that the inferior feedstock oil is selected from by topped crude, stone
One group of substance that the hydro carbons for the high asphalt content that dregs of fat oil, oil-sand, pitch, shale oil, liquefaction coal or reclaimed oil obtain is constituted.
5. according to the method for claim 1, which is characterized in that in weighted BMO spaces reaction zone, hydrogenation protecting catalyst
Admission space ratio with Hydrodemetalation catalyst is 5:95~95:5.
6. according to the method for claim 5, which is characterized in that include hydrodesulfurization in the weighted BMO spaces reaction zone
Catalyst, the loadings of Hydrobon catalyst are 5v%~30v% of Hydrodemetalation catalyst loadings.
7. method according to claim 1 or 2, which is characterized in that the weighted BMO spaces condition are as follows: reaction pressure is
5MPa~35MPa, average reaction temperature are 340 DEG C~430 DEG C, and volume space velocity is 0.1h when liquid-1~5.0h-1, liquid phase circulation matter
Amount is than being 0.1:1~10:1；The hydroprocessing condition are as follows: reaction pressure is 5MPa~35MPa, and average reaction temperature is
320 DEG C~420 DEG C, volume space velocity is 0.1h when liquid-1~5.0h-1, hydrogen to oil volume ratio is 200~1500.
8. according to the method for claim 1, which is characterized in that in the hydrotreating reaction area, hydrodesulfurization catalytic
The admission space of agent and hydrodenitrogenation catalyst ratio is 20:80~80:20.
9. according to the method for claim 8, which is characterized in that contain hydrodemetallization in the hydrotreating reaction area
Catalyst, the loadings of Hydrodemetalation catalyst account for 2v%~30v% of loaded catalyst in hydrotreating reaction area.
10. according to the method for claim 1, which is characterized in that the operating condition of the catalytic cracking reaction zone are as follows: reaction
470~650 DEG C of temperature, 0.5~5 second reaction time, catalyst and feedstock oil weight ratio 3~10, catalyst regeneration temperature 650
~800 DEG C.
11. according to the method for claim 1, which is characterized in that be recycled to first, hydrotreating reaction area reactor and enter
Mouth recycle oil accounts for 20% or more of catalytic cracking recycle oil weight obtained by catalytic cracking reaction zone, preferably 30 ~ 70%；It is recycled to and adds hydrogen
The recycle oil in pretreatment reaction area accounts for 10% or more of the catalytic cracking recycle oil weight that catalytic cracking reaction zone obtains, preferably 20 ~
50%；It is recycled to first, hydrotreating reaction area reactor inlet and is recycled to the recycle oil total amount of weighted BMO spaces reaction zone
Account for 30% or more of the catalytic cracking recycle oil weight that catalytic cracking reaction zone obtains, preferably 50 ~ 95%.
12. according to the method for claim 1, which is characterized in that be recycled to the cycle oil of weighted BMO spaces reaction zone
Slurry accounts for 30% or more of the catalytic cracked oil pulp weight that catalytic cracking reaction zone obtains, preferably 50 ~ 80%.
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