CN106701192B

CN106701192B - A kind of process for handling residual oil

Info

Publication number: CN106701192B
Application number: CN201510769151.8A
Authority: CN
Inventors: 刘铁斌; 耿新国; 翁延博; 李洪广
Original assignee: China Petroleum and Chemical Corp; Sinopec Fushun Research Institute of Petroleum and Petrochemicals
Current assignee: China Petroleum and Chemical Corp; Sinopec Fushun Research Institute of Petroleum and Petrochemicals
Priority date: 2015-11-12
Filing date: 2015-11-12
Publication date: 2018-03-16
Anticipated expiration: 2035-11-12
Also published as: CN106701192A

Abstract

The invention discloses a kind of process for handling residual oil, including weighted BMO spaces unit, coking plant, hydrotreating unit and catalytic cracking unit, the hydrotreating unit to include weighted BMO spaces reaction zone and hydrotreating reaction area；The process includes herein below：Generation oil evaporates to obtain light fraction and heavy distillat after the hydrogenated pretreatment unit reaction of residual oil raw material, heavy distillat obtains coker gasoline after entering coking plant processing, coker gas oil and wax tailings, successively by the weighted BMO spaces reaction zone connected and hydrotreating reaction area after light fraction and the mixing of wax tailings and hydrogen, the reaction effluent in hydrotreating reaction area carries out gas-liquid separation, gas phase is recycled back to weighted BMO spaces reaction zone and/or hydrotreating reaction area, liquid phase is directly entered catalytic cracking reaction zone and carries out catalytic cracking reaction, the isolated dry gas of catalytic cracking reaction effluent, liquefied gas, catalytically cracked gasoline cut, catalytic cracking diesel oil cut, heavy catalytic cycle oil and catalytic cracked oil pulp.The inventive method can be with the stable operation period of extension fixture.

Description

A kind of process for handling residual oil

Technical field

The present invention relates to a kind of heavy oil lightening method, is combined more particularly to one kind using coking-hydrogenation-catalytic cracking The method of PROCESS FOR TREATMENT heavy oil.

Background technology

At present, it will be in hold that domestic and international refined products market, which is particularly to the demand of the oil products such as steam coal bavin to the demand of motor petrol, The continuous trend risen, and it is then on a declining curve to the demand of the heavy oil products such as heavy fuel oil.Meanwhile crude oil in the world Matter is deteriorated increasingly, and environmental regulation is increasingly strict, and increasingly strict requirements are proposed to oil quality.Therefore, how with relatively warp Rational cost of helping realizes that heavy oil lighting and petrol and diesel oil product quality persistently upgrade as oil refining industry concern both at home and abroad Focus.

The main purpose of residual hydrocracking technique is by hydrotreating, makes sulphur in residual oil raw material, nitrogen, metal etc. miscellaneous Matter content is greatly reduced, the undesirable components hydro-conversion such as condensed-nuclei aromatics, colloid, asphalitine, improves hydrogen-carbon ratio, reduces carbon residue and contains Amount, make its cracking performance be improved significantly.Fixed bed residual hydrogenation technology is a kind of heavy oil deep processing technology, equipped with spy In the fixed bed reactors for determining catalyst, under the hydro condition of HTHP, desulfurization is carried out to normal pressure or decompression residuum, taken off Nitrogen, demetalization etc., it is one of important means of residual oil weight-lightening to obtain light-end products to greatest extent.Fixed bed residual oil adds Hydrogen technology is high with its liquid product yield, and good product quality, production chains are strong, and waste, waste material are few, environment-friendly, invest back The advantages that report rate is high, obtain more and more extensive application.

The setting of fixed bed residual hydrocracking process reaction partial reaction device is typically connected by multiple reactors or bed Use, the formulation of optimization catalyst is required, according to different physical according to original oily property, reaction condition and purpose product Matter, catalyst activity and all kinds of catalyst ratios carry out grading loading.Fixed bed residual hydrogenation technology although having many advantages, such as, But in process of production, but easily there is the phenomenon of reactor pressure drop increase.Industrial operation shows that reactor pressure drop increases One of an important factor for being confining device full production and long-term operation.Especially more reactor series connection, preposition is anti- Answer demetalization of the device due to assume responsibility for more than 70% to react load, metal sulfide is deposited on beds, into operation after Inevitably there is pressure drop rapid growth in phase, and reactor below is because demetalization load is substantially relatively low, pressure drop increase compared with Slowly.This have impact on the cycle of operation and the device of device there have been anterior reactor and the distribution of rear portion reactor load are uneven Stable operation.

CN103059928A discloses a kind of hydrotreater and its application and process for hydrogenating residual oil.The invention carries For a kind of and its processing unit, the device includes the hydrogenation insured unit once connected and main hydrotreating unit.Described adds Hydrogen protection location includes main hydrogenation protecting reactor in parallel and standby hydrogenation protecting reactor, and main hydrogenation protecting reactor Volume is more than stand-by protection reactor.In hydroprocessing processes, main hydrogenation protecting reactor and standby hydrogenation protecting reactor It is used alternatingly.Main hydrogenation protecting reactor and standby hydrogenation protecting reactor handover operation can be processed height by the process The residual oil of calcium high metal content, shortcoming are the reactors that left unused, and increase investment reduces reactor utilization rate, and can not Solves lead reactor pressure drop growing concern from not catching up with.

CN1393515A discloses a kind of method of residual hydrocracking.This method is in heavy resid hydrogenation reaction system First reactor set up one or more charging apertures, while change original catalyst grade and match somebody with somebody, when an anticatalyst bed When pressure drop designs 0.4~0.8 times of pressure drop for device, next charging aperture is used instead successively, while original charging aperture can enter circulation The miscella of oil or recycle oil and original oil, the service cycle of bed pressure drop and extension fixture can be effectively prevented with the technique, And the disposal ability of device can be increased, help to improve flow distribution.Shortcoming is the increase of inductor manufacturing cost, is made initial Pressure drop increases, and device inner volume utilization rate reduces etc..

CN103059931A discloses a kind of method of residual hydrocracking.This method is in hydrotreating reaction condition Under, residual oil raw material and hydrogen once by more reactors of series connection, when plant running 700~4000 is small after carry out shunting behaviour Make, reduce an anti-inlet amount or keep an anti-inlet amount constant, increase by one is anti-and last reactor among each reactor Inlet amount, increased feed residue intermediate reactor entrance inject.This method is delayed by changing each anti-feed loading The growth of pressure drop is solved, but can not fundamentally change the growth trend of lead reactor pressure drop, from the point of view of industrial actual motion, pressure drop The design upper limit can be quickly reached once increasing, and changes the stable operation that each anti-entrance charging is unfavorable for device.

The content of the invention

In view of the shortcomings of the prior art, the invention provides a kind of process for handling residual oil.This method technological process Simply, it is only necessary to which simple modifications are carried out to existing apparatus, it is possible to significantly extend the service cycle of whole device, and can make to urge The utilization ratio of agent, which is realized, to be maximized.

Existing residual hydrocracking technology, all reactors are using the technological process connected, it is therefore desirable to anti-in First Device is answered to load substantial amounts of protective agent to deposit impurity and the dirty thing in raw material, so operation can cause in First protection reactor For the antigravity system of filling because activity is relatively low, demetalization load is relatively low, has arrived plant running latter stage reactor in some cases Pressure drop is still very low so that the ability that is de-, holding metallic compound of integer catalyzer reduces.If improve its catalyst activity again The rapid growth of pressure drop can be caused, shortens the cycle of operation, and follow-up catalyst performance does not play also completely, keeps First The appropriate activity of protection reactor catalyst is difficult control, and exist during residual hydrogenation equipment whole service it is many because Fe in element such as urgent shutting down, feedstock property fluctuation or raw material, Ca impurity increases suddenly, therefore common practice is still Be to maintain the activity of the relatively low reaction of an anti-protection reactor catalyst, its main function intercept and the impurity in deposition raw material and Dirty thing, relatively low demetalization reaction is only carried out, be typically that the reactor reaction temperature rise is relatively low, pressure drop is tieed up in the whole service cycle Hold and in relatively low level, so require that loading substantial amounts of catalyst for demetalation in follow-up demetalization reactor is substantially carried out taking off Metal reaction and for accommodate hydrogenation and removing metallic compound and carbon distribution enough spaces are provided, so inevitably cause Substantial amounts of metal is deposited in the demetalization reactor, demetalization reaction load is larger, is typically the reactor reaction temperature rise highest, Although initial operating stage reactor pressure decrease is relatively low, the pressure drop to operation to the mid-term or later stage pressure drop reactor increases at first It is long, and growth is most fast, turns into the principal element for restricting the cycle of operation.

The present invention provides a kind of process for handling residual oil, including weighted BMO spaces unit, coking plant, hydrotreating Unit and catalytic cracking reaction zone, the hydrotreating unit include weighted BMO spaces reaction zone and hydrotreating reaction area, institute Stating process includes herein below：

（1）Feedstock oil enters weighted BMO spaces unit after being mixed with hydrogen, reaction generation oil be fractionated into obtaining light fraction and Heavy distillat, cutting point range are 500-650 DEG C；

（2）Step（1）Obtained heavy distillat enters coking plant, and coker gasoline, coker gas oil, coking wax are obtained after processing Oil and coke；

（3）Step（1）Obtained light fraction, step（2）Obtained wax tailings pass through successively after being mixed with hydrogen connects The weighted BMO spaces reaction zone of setting and hydrotreating reaction area, the reaction effluent in hydrotreating reaction area carry out gas-liquid point From isolated gas phase is recycled back to weighted BMO spaces reaction zone and/or hydrotreating reaction area, and isolated liquid phase is direct Catalytic cracking reaction, the isolated dry gas of catalytic cracking reaction effluent, liquefied gas, catalysis are carried out into catalytic cracking reaction zone Cracked naphtha, catalytic cracking diesel oil cut, heavy catalytic cycle oil and catalytic cracked oil pulp；The weighted BMO spaces are anti- Area is answered to include the weighted BMO spaces reactor that two more parallels are set, when any hydrogenation in the weighted BMO spaces reaction zone The pressure drop of preatreating reactors reaches the 50%~80% of the reactor design pressure drop upper limit, when preferably 60%~70%, the hydrogenation is pre- Treatment reactor is cut out from weighted BMO spaces reaction zone, and the weighted BMO spaces reactor is named as to the hydrogenation cut out and located in advance Reactor I is managed, and according to material successively by weighted BMO spaces reaction zone, the weighted BMO spaces reactor I cut out, hydrotreating The order of reaction zone is by weighted BMO spaces reactor that this cuts out and weighted BMO spaces reaction zone and hydrotreating reaction area to go here and there The mode of connection connects, and the now charging of the weighted BMO spaces reactor cut out is the weighted BMO spaces reaction cut out except this The reaction effluent of weighted BMO spaces reactor outside device, when the pressure drop of next weighted BMO spaces reactor reaches reactor The 50%~80% of the pressure drop upper limit is designed, when preferably 60%~70%, by the weighted BMO spaces reactor from weighted BMO spaces reaction zone In cut out, and the weighted BMO spaces reactor that this cuts out is named as to the weighted BMO spaces reactor II cut out, and according to material Successively by weighted BMO spaces reaction zone, cut out weighted BMO spaces reactor II, cut out weighted BMO spaces reactor I, plus The order of hydrogen processing reaction zone is by weighted BMO spaces reactor II that this cuts out and weighted BMO spaces reaction zone and the hydrogenation cut out Preatreating reactors I is connected in series to, and the weighted BMO spaces reactor II now cut out charging is weighted BMO spaces The reaction effluent of remaining weighted BMO spaces reactor of the reaction zone in addition to the weighted BMO spaces reactor cut out, according to upper Mode is stated, until all weighted BMO spaces reactors are all connected in series to.

In the inventive method, the weighted BMO spaces unit process condition is：Reaction temperature is 350 DEG C~400 DEG C, preferably For 360 DEG C~390 DEG C, reaction pressure is 10MPa~25MPa, preferably 15MPa~20MPa；Hydrogen to oil volume ratio be 300~ 1500, preferably 500~800；Volume space velocity is 0.15h during raw material fluid^-1~5.00h^-1, preferably 0.30h^-1~2.00h^-1。

In the inventive method, catalytically cracked gasoline cut that catalytic cracking reaction obtains, catalytic cracking diesel oil cut, catalysis One or more in cracking heavy-cycle oil can be recycled back to weighted BMO spaces reaction zone and carry out hydrogenation reaction.

In the inventive method, the catalytic cracked oil pulp that catalytic cracking reaction obtains can be recycled back at coking plant Reason.

Reach anti-in the inventive method, during all weighted BMO spaces reactor differences in the weighted BMO spaces reaction zone The 50%~80% of the device pressure drop design upper limit is answered, can be set by process conditions and the difference of beds property is hydrogenated with Reach the 50%~80% of the pressure drop design upper limit during each weighted BMO spaces reactor difference in pretreatment reaction area.It can specifically pass through Control different catalyst packing height in each weighted BMO spaces reactor, different inlet amounies, different feed properties, no With operating condition, can use under the conditions of identical filling height one kind in the means such as different Catalyst packing density or It is several to reach the 50%~80% of the pressure drop design upper limit during each weighted BMO spaces reactor difference to realize.

As described above, when the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel is urged using different During agent loading density, in the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel, maximum loading density For 400kg/m³~600kg/m³, preferably 450 kg/m³~550kg/m³；Minimum loading density is 300kg/m³~550kg/ m³, preferably 350kg/m³~450kg/m³.The Catalyst packing of the immediate two weighted BMO spaces reactors of loading density is close Degree difference is 30~200kg/m³, preferably 50~150kg/m³.It is first that the hydrogenation being cut out is pre- when other conditions are consistent The Catalyst packing density for the treatment of reactor is maximum, and the Catalyst packing density for the weighted BMO spaces reactor being finally cut out is most It is small.The different loading densities can by different types of catalyst grade it is equipped tamp it is existing, such as can by hydrogenation protecting agent, Hydrodemetalation catalyst, Hydrobon catalyst realize the catalyst in each weighted BMO spaces reactor in different proportions Loading density is different.

As described above, when the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel is entered using different During doses, the ratio between feed volume air speed of the immediate two weighted BMO spaces reactors of inlet amount is 1.1 ~ 3.0, is preferably 1.1~1.5。

As described above, when the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel is entered using different When expecting property, the tenor difference of the immediate two weighted BMO spaces reactors of feed properties is 5 ~ 50 μ g/g, is preferably 10~30µg/g。

As described above, when the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel uses different behaviour When making condition, can with the operating condition of the immediate two weighted BMO spaces reactors of control operation pressure and volume space velocity, Operation temperature difference is 2 ~ 30 DEG C, preferably 5 ~ 20 DEG C.

In the inventive method, the catalytically cracked gasoline cut, the catalytic cracking diesel oil that are recycled back to weighted BMO spaces reaction zone evaporate Divide, one or several that heavy catalytic cycle oil can enter in the weighted BMO spaces reactor being arranged in parallel, preferably by suitable Suitable ratio respectively enters different weighted BMO spaces reactors.

In the inventive method, the weighted BMO spaces reaction zone includes the weighted BMO spaces reaction that two more parallels are set Device, 3~6 weighted BMO spaces being arranged in parallel reactors are preferably included, more preferably including 3 or 4 hydrogenation being arranged in parallel Preatreating reactors.Described hydrotreating reaction area includes 1~5 hydrotreating reactor being arranged in series, and preferably includes 1 ~2 hydrotreating reactors being arranged in series.

In the inventive method, the operating condition of the weighted BMO spaces reaction zone is：Reaction temperature is 370 DEG C~420 DEG C, Preferably 380 DEG C~400 DEG C, reaction pressure is 10MPa~25MPa, preferably 15MPa~20MPa；Hydrogen to oil volume ratio is 300 ~1500, preferably 500~800；Volume space velocity is 0.15h during raw material fluid^-1~2.00h^-1, preferably 0.3h^-1~1.00h^-1.Reaction of the average reaction temperature of weighted BMO spaces reaction zone apparently higher than the residuum hydrogenating and metal-eliminating reactor of prior art Temperature, the residuum hydrogenating and metal-eliminating reaction temperature of prior art is usually 350 DEG C~390 DEG C.What this method middle front part was set adds Hydrogen pretreatment reaction zone eliminates the unfavorable factor that pressure drop increases restrictive cycle by the optimization of technological process, can be in high temperature Lower operation, in addition relatively high reaction temperature be advantageous to the performance of loaded catalyst system performance, be advantageous to macromolecular The removing of hydro-conversion and impurity.

In the inventive method, the operating condition in the hydrotreating reaction area is that reaction temperature is 370 DEG C~430 DEG C, excellent Elect 380 DEG C~410 DEG C as, reaction pressure is 10MPa~25MPa, preferably 15MPa~20MPa；Hydrogen to oil volume ratio be 300~ 1500, preferably 400~800；Volume space velocity is 0.15h during raw material fluid^-1~0.80h^-1, preferably 0.2h^-1~0.60h^-1。

In the inventive method, coking process is various coking process known to those skilled in the art of the present technique, and it can be Delayed coking, fluid coking or flexicoking etc..Operating condition is：Pressure is 1~3MPa, preferably 1~2MPa； Temperature is 450~550 DEG C, preferably 480~520 DEG C.Gas fraction is obtained in coking can go gas recovery system, burnt Changing gasoline fraction and fraction of coker gas oil can go respective device of re-refining to be handled respectively, and wax tailings deliver to the present invention Hydrogenation reaction system carry out hydrotreating.And coke can according to its impure amount number go to make electrode or deoxidation hydrogen manufacturing and Make fuel.

In the inventive method, catalytic cracking can use this area routine techniques.Catalytic cracking unit can be it is a set of or More than a set of, often cover catalytic cracking unit at least should need to set including a reactor and a regenerator, catalytic cracking unit Fractionating column, fractionating column can be set respectively with every set catalytic cracking unit, fractionating column can also be shared.Fractionating column is by Catalytic Cracking Unit of Measure Answer effluent fractionation for dry gas, liquefied gas, catalytically cracked gasoline cut, catalytic cracking diesel oil cut, catalytic cracking recycle oil and Catalytic cracked oil pulp etc..Catalytic cracking fractionating tower routinely knowledge can design.

In the inventive method, the operating condition of the catalytic cracking reaction zone is：Reaction temperature is 450~600 DEG C, preferably For 480~550 DEG C；Regeneration temperature be 600~800 DEG C, preferably 650~750 DEG C, agent weight of oil than 2~30, preferably 4~ 10；It it is 0.1~15 second, preferably 0.5~5 second with catalyst contact time；Pressure is 0.1~0.5MPa.Used catalysis Cracking catalyst includes being generally used for the catalyst of catalytic cracking, as silica-alumina catalyst, silica-magneia cataslyst, acid treatment carclazyte and X-type, Y types, ZSM-5, M type, preferably layer post equimolecular sieve Cracking catalyst, molecular sieve cracking catalyst, because molecule The activity height of Cracking catalyst is sieved, green coke is few, and gasoline yield is high, high conversion rate.The reactor of described catalytic cracking unit can To be the catalyst cracker of various types, preferably riser reactor or riser adds bed reactor.Technological process Generally：Feedstock oil injects from riser reactor bottom, is contacted with the high-temperature regenerated catalyst from regenerator, cracking reaction The oil gas of generation and the catalyst mixture of deposit coke move up along riser reactor, complete the catalysis of whole feedstock oil Cracking reaction.

In the inventive method, residual hydrogenation technology uses fixed bed residual hydrocracking technology, and the anterior hydrogenation is pre- Processing unit is made up of one or several reactors can load hydrogenation protecting agent, Hydrodemetalation catalyst, hydrodesulfurization are urged One or more in agent, hydrogenation can be loaded in each weighted BMO spaces reactor of the weighted BMO spaces reaction zone and is protected The one or more protected in agent, Hydrodemetalation catalyst, Hydrobon catalyst, hydrodenitrogeneration carbon residue reforming catalyst, institute State the one kind or several that can be loaded in hydrotreating reaction area in Hydrobon catalyst and hydrodenitrogeneration carbon residue reforming catalyst Kind, the hydrogenation protecting agent, Hydrodemetalation catalyst, Hydrobon catalyst, hydrodenitrogeneration carbon residue reforming catalyst are Catalyst used in fixed bed residual hydrocracking process.Above-mentioned catalyst is typically all with porous refractory inorganic oxide such as oxygen Change aluminium is carrier, and vib and/or group VIII metal such as W, Mo, Co, Ni etc. oxide are active component, optionally plus Enter the catalyst of the elements such as other various auxiliary agents such as P, Si, F, B, such as by Sinopec Group's catalyst point The FZC series catalyst for hydrotreatment of residual oil of company's production.

In the inventive method, described feed residue can be that reduced crude can also be decompression residuum, generally also contain Straight-run gas oil, decompressed wax oil, the one or more in secondary operation wax oil and FCC recycle oil.Described residual oil raw material property For：Sulfur content is not more than 4wt%, and nitrogen content is not more than 0.7wt%, and tenor (Ni+V) is not more than 120 μ g/g, and carbon residue is not More than 17wt%, asphalt content is not more than 5wt%.

Compared with prior art, the inventive method has the following advantages：

1st, in the inventive method, the weighted BMO spaces reaction zone includes more weighted BMO spaces reactors of parallel connection, So that whole catalyst system takes off/held metal ability and is increased dramatically.

2nd, the inventive method passes through to being catalyzed in each weighted BMO spaces reactor in weighted BMO spaces reaction zone Agent grading so that when the pressure drop of reactor rises to setting value, by the change of technological process, it is reacted from weighted BMO spaces Area is cut out, and change optimizes its feed properties, makes its pressure drop no longer rapid growth, but can be straight slowly to increase in control range Stopped work to device, and then the pressure drop of some weighted BMO spaces reactor is not restricted the cycle of operation of whole device.

3rd, the inventive method is to weighted BMO spaces reaction zone catalyst performance and technological parameter by optimizing and revising, and rear Continuous high activity desulfurization takes off the cooperation of carbon residue catalyst so that is taken off while de-/appearance metal ability of integer catalyzer is improved Sulphur takes off carbon residue performance and is guaranteed.

4th, the inventive method is by the way that each weighted BMO spaces reactor of weighted BMO spaces reaction zone is cut from series connection is parallel to The adjustment for changing mode of operation solves the problem of reactor pressure decrease rapid growth, while adds the operating flexibility and original of device Expect adaptability；

5th, the inventive method is by setting weighted BMO spaces reactor parallel form that the appearance gold of catalyst system is significantly increased Category amount so that the stability enhancing of system so that the growth of device pressure drop can be controlled, the extension fixture cycle of operation.

6th, the inventive method can at utmost realize that all kinds of catalyst synchronously inactivate, so as to improve the operation of device effect Rate, increase economic efficiency.

7th, in the inventive method, in the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel, according to Flow of Goods and Materials direction, hydrogenation protecting agent and Hydrodemetalation catalyst are loaded successively in weighted BMO spaces reactor, can also be Selectivity filling Hydrobon catalyst below Hydrodemetalation catalyst.Such catalyst loading pattern so that whole body System takes off/held metal ability and is increased dramatically, while the pressure for each preatreating reactors of adjustment matched somebody with somebody by catalyst grade Drop increases in control range.The catalyst system of weighted BMO spaces reaction zone each weighted BMO spaces reactor filling in parallel Based on de-/appearance metal function so that while demetalization performance boost, strengthen to macromolecular in raw material such as gum asphalt The ability of hydro-conversion, laid the foundation for successive depths desulfurization and the conversion of carbon residue so that hydrodesulfurizationreaction reaction zone be advantageous into One step deep reaction, therefore compared with routine techniques, it is whole although the ratio of Hydrodemetalation catalyst improves The hydro-conversion performance of the desulphurizing activated and carbon residue of body is not only improved on the contrary without reduction.

8th, in the inventive method, by residual hydrocracking, catalytic cracking and coking process organic assembling.This method can be big The utilization ratio for realizing catalyst service cycle that width extends residual hydrogenation equipment maximizes, and reduces residual hydrogenation equipment Operating severity, the service life of catalyst is extended, realize the high lightweight rate of residual oil.

9th, in group technology of the present invention, it is not required to set fractionating system in hydrotreating reaction area, hydrotreating generation oil is directly Into catalyst cracker, it is not required to set feed pump, while reduce a large amount of heat transmission equipments.Equipment investment is set to have very big drop It is low.

Brief description of the drawings

Fig. 1 is the process method flow chart of present invention processing residual oil.

Embodiment

Method provided by the present invention is further detailed below in conjunction with the accompanying drawings, but does not therefore limit this hair It is bright.

As shown in figure 1, the method for present invention processing residual oil includes herein below：Residual oil raw material 21 enters weighted BMO spaces list Member, light fraction 22 and heavy distillat 23 are obtained after reaction generation oil separation, heavy distillat 23 enters coking plant H, Jiao is obtained after processing It is mixed to change gasoline 24, coker gas oil 26, wax tailings 27 and coke 26, the light fraction 22, wax tailings 27 and hydrogen Material 28 enters at the weighted BMO spaces reaction zone and hydrogenation that are arranged in series through feeding line 1, feeding line 2 and feeding line 3 Reaction zone is managed, the weighted BMO spaces reaction zone includes three weighted BMO spaces reactors being arranged in parallel, and respectively hydrogenation is pre- Treatment reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C, the weighted BMO spaces reactor A, hydrogenation are pre- Treatment reactor B, weighted BMO spaces reactor C charging aperture connect with feeding line 1, feeding line 2 and feeding line 3 respectively Connect, three tunnels of outlet point of the weighted BMO spaces reactor A, charging aperture of the first via through pipeline 6 Yu weighted BMO spaces reactor B Connection, the second tunnel are connected through pipeline 7 with weighted BMO spaces reactor C charging aperture, and the 3rd tunnel is anti-through pipeline 10 and hydrotreating Answer device D connections；Three tunnels of the outlet of the weighted BMO spaces reactor B point, the first via is through pipeline 4 and weighted BMO spaces reactor A Charging aperture connection, the second tunnel obtains charging aperture with weighted BMO spaces reactor C through pipeline 5 and be connected, and the 3rd tunnel is through pipeline 11 and adds The D connections of hydrogen treatment reactor；Three tunnels of the outlet of the weighted BMO spaces reactor C point, the first via is through pipeline 8 and weighted BMO spaces The charging aperture connection of reactor A, the second tunnel are connected through pipeline 9 with the charging aperture of weighted BMO spaces reactor B, and the 3rd tunnel is through pipeline 12 are connected with hydrotreating reactor D；Valve 101 is provided with the pipeline 1, valve 102, institute are provided with the pipeline 2 State and valve 103 is provided with pipeline 3, valve 104 is provided with the pipeline 4, valve 105 is provided with the pipeline 5, it is described Valve 106 is provided with pipeline 6, valve 107 is provided with the pipeline 7, valve 108, the pipe are provided with the pipeline 8 Valve 109 is provided with line 9, valve 1010 is provided with the pipeline 10, valve 1011 is provided with the pipeline 11, it is described Valve 1012 is provided with pipeline 12, the generation oil 13 that the hydrotreating reactor obtains obtains after entering separator E separation Liquefied gas 20 and hydrogenated oil 14 are obtained, the hydrogenated oil 14 enters catalytic cracking reaction zone F, is catalyzed with high temperature regeneration Cracking catalyst contacts and carries out catalytic cracking reaction, and product is fractionated into obtaining gas 15, catalytically cracked gasoline cut after reaction 16th, catalytic cracking diesel oil cut 17, catalytic cracking recycle oil 18 and catalytic cracked oil pulp 19, gas 15 and catalytically cracked gasoline evaporate Dividing 16 dischargers, catalytic cracking diesel oil cut 17 and heavy catalytic cycle oil cut 18 return to weighted BMO spaces reaction zone, With residual oil raw material weighted BMO spaces reaction zone is mixed into be reacted, catalytic cracked oil pulp 19 can be recycled back to coking plant or Arranged outside person.

In the inventive method, the weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C can be inactivated in any order, altogether including following 6 kinds of processes

1st, inactivated according to weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C order

（1）When going into operation, pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, the valve 101 on pipeline 12, valve 102, Valve 103, valve 1010, valve 1011, valve 1012 are opened, pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, on pipeline 9 Valve 104, valve 105, valve 106, valve 107, valve 108, valve 109 close；

（2）When the pressure drop of weighted BMO spaces reactor A reaches critical value, valve 101, the pipeline of feeding line 1 are closed 11 valve 1011 and the valve 1012 of pipeline 12, the valve 104 on the valve 108 and pipeline 4 on pipeline 8 is opened, it is now complete Into once by being parallel to the handover operation of series connection；

（3）When the pressure drop of weighted BMO spaces reactor B reaches critical value, valve 102, the pipeline 8 of feeding line 2 are closed Valve 108, open pipeline 9 on valve 109, now complete the 2nd handover operation by being parallel to series connection；

（4）When weighted BMO spaces reactor C pressure drop reaches critical value, whole reaction system needs shutdown process.

2nd, inactivated according to the order of weighted BMO spaces reactor A, weighted BMO spaces reactor C, weighted BMO spaces reactor B

（3）When weighted BMO spaces reactor C pressure drop reaches critical value, valve 103, the pipeline 4 of feeding line 3 are closed Valve 104, open pipeline 5 on valve 105, now complete the 2nd handover operation by being parallel to series connection；

3rd, inactivated according to the order of weighted BMO spaces reactor B, weighted BMO spaces reactor C, weighted BMO spaces reactor A

（2）When the pressure drop of weighted BMO spaces reactor B reaches critical value, valve 102, the pipeline of feeding line 2 are closed 10 valve 1010 and the valve 1012 of pipeline 12, the valve 106 on the valve 109 and pipeline 6 on pipeline 9 is opened, it is now complete Into once by being parallel to the handover operation of series connection；

（3）When weighted BMO spaces reactor C pressure drop reaches critical value, valve 103, the pipeline 6 of feeding line 3 are closed Valve 106, open pipeline 7 on valve 107, now complete the 2nd handover operation by being parallel to series connection；

（4）When the pressure drop of weighted BMO spaces reactor A reaches critical value, whole reaction system needs shutdown process.

4th, inactivated according to weighted BMO spaces reactor B, weighted BMO spaces reactor A, weighted BMO spaces reactor C order

（3）When the pressure drop of weighted BMO spaces reactor A reaches critical value, valve 101, the pipeline 9 of feeding line 1 are closed Valve 109, open pipeline 8 on valve 108, now complete the 2nd handover operation by being parallel to series connection；

5th, inactivated according to the order of weighted BMO spaces reactor C, weighted BMO spaces reactor B, weighted BMO spaces reactor A

（2）When weighted BMO spaces reactor C pressure drop reaches critical value, valve 103, the pipeline of feeding line 3 are closed 10 valve 1010 and the valve 1011 of pipeline 11, the valve 105 on the valve 107 and pipeline 5 on pipeline 7 is opened, it is now complete Into once by being parallel to the handover operation of series connection；

（3）When the pressure drop of weighted BMO spaces reactor B reaches critical value, valve 102, the pipeline 7 of feeding line 2 are closed Valve 107, open pipeline 6 on valve 106, now complete the 2nd handover operation by being parallel to series connection；

6th, inactivated according to the order of weighted BMO spaces reactor C, weighted BMO spaces reactor A, weighted BMO spaces reactor B

（3）When the pressure drop of weighted BMO spaces reactor A reaches critical value, valve 101, the pipeline 5 of feeding line 1 are closed Valve 105, open pipeline 4 on valve 104, now complete the 2nd handover operation by being parallel to series connection；

（4）When the pressure drop of weighted BMO spaces reactor B reaches critical value, whole reaction system needs shutdown process.

Illustrate the effect of the present invention with reference to specific embodiment, it is used in embodiment of the present invention and comparative example Raw material includes three kinds, respectively raw material A, raw material B, raw material C, and specific nature is shown in Table 1, the dress of catalyst in the embodiment 1~4 Embankment formula is shown in Table 3, and the type of feed of catalyst is shown in Table 4 in the comparative example 1~4, and the reaction condition of the embodiment 1~4 is shown in Table 5, the reaction condition of the comparative example 1~4 are shown in Table 6, and the reaction result of the embodiment 1~4 and comparative example 1~4 is shown in Table 7. Using conventional tandem process in the comparative example 1-4, other are identical with the correspondence of embodiment 1~4 respectively.In the embodiment of the present invention Described weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C are pattern, size identical Reactor, reactor A, reactor B in the comparative example, reactor C are pattern, size identical reactor.

Embodiment 1

Described in embodiment 1 using raw material A property be shown in Table 1 mixed with hydrogen after enter weighted BMO spaces device, be hydrogenated with Pretreatment, reaction temperature are 377 DEG C, volume space velocity 0.4h^-1, reaction pressure 16MPa, reaction generation oil is by isolated Light fraction and heavy distillat, cut point are 620 DEG C.Heavy distillat is handled by coking plant, then be isolated to coker gasoline, Coker gas oil, wax tailings and coke.The operating condition of coking is 505 DEG C of reaction temperature, pressure 170000Pa.

By 30% catalytic cracking diesel oil of wax tailings and light fraction and catalytic cracking unit and whole catalytic cracking Heavy-cycle oil delivers to weighted BMO spaces reaction zone.The pre- place of the weighted BMO spaces reactor A, weighted BMO spaces reactor B, hydrogenation It is identical with inlet amount to manage reactor C catalyst inventory, feed properties, the weighted BMO spaces reactor A, hydrogenation are pre- Treatment reactor B, weighted BMO spaces reactor C, hydrotreating reactor D catalyst load in the way of in table 3, described Residual hydrogenation operating condition is shown in Table 5, and specific residual hydrogenation reaction result is shown in Table 7.Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 8, specifically urges Fluidized cracking catalysts property is shown in Table 9, and catalytic cracking product distribution of products property is shown in Table 10.

Embodiment 2

In embodiment 2, it is described using raw material B properties be shown in Table 1 mixed with hydrogen after added into weighted BMO spaces device Hydrogen pretreatment reacts, and reaction temperature is 375 DEG C, volume space velocity 0.40h^-1, reaction pressure 16MPa, reaction generation oil process Isolated light fraction and heavy distillat, cut point are 610 DEG C.Heavy distillat is handled by coking plant, then is isolated to Coker gasoline, coker gas oil, wax tailings and coke.The operating condition of coking is 505 DEG C of reaction temperature, and pressure is 170000Pa。

By wax tailings and light distillate and light fraction and 20% catalytic cracking diesel oil and whole of catalytic cracking unit Heavy catalytic cycle oil deliver to weighted BMO spaces reaction zone.The weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C catalyst inventory, feed properties are identical, and Feed space velocities are different, the pre- place of hydrogenation Volume space velocity is 0.20h when managing reactor A liquid^-1, volume space velocity is 0.32h during weighted BMO spaces reactor B liquid^-1, it is hydrogenated with pre- place Volume space velocity is 0.44h when managing reactor C liquid^-1.Weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces Identical catalyst loading pattern is used in reactor C, catalyst loading pattern is shown in Table 3, and the residual hydrogenation operating condition is shown in Table 5, specific residual hydrogenation reaction result are shown in Table 7.Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 8, and specific catalytic cracking catalyst property is shown in Table 9, catalytic cracking product distribution of products property are shown in Table 10.

Embodiment 3

In embodiment 3, it is hydrogenated with after respectively mixing raw material A, B, C with hydrogen into respective weighted BMO spaces device Pretreatment, reaction temperature is 380 DEG C, volume space velocity 0.4h^-1, reaction pressure 16MPa, reaction generation oil is by separating To light fraction and heavy distillat, cut point is 608 DEG C.Heavy distillat is handled by coking plant, then is isolated to coking vapour Oil, coker gas oil, wax tailings and coke.The operating condition of coking is 505 DEG C of reaction temperature, pressure 170000Pa.

The weighted BMO spaces reactor A uses the light fraction of the wax tailings and A of raw material A, weighted BMO spaces reactor B Evaporated using the light fraction of raw material B wax tailings and B, weighted BMO spaces reactor C using raw material C wax tailings and the light of C Point.The weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C inlet amount are identical, described Identical Catalyst packing side is used in weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C Formula, catalyst loading pattern are shown in Table 3, and the residual hydrogenation operating condition is shown in Table 5, and specific residual hydrogenation reaction result is shown in Table 7.Urge Change cracking operation condition and be shown in Table 8, specific catalytic cracking catalyst property is shown in Table 9, and catalytic cracking product distribution of products property is shown in Table 10。

Embodiment 4

In embodiment 4, it is described using raw material C properties be shown in Table 1 mixed with hydrogen after enter weighted BMO spaces device, added Hydrogen pretreatment, reaction temperature are 380 DEG C, volume space velocity 0.4h^-1, reaction pressure 16MPa, reaction generation oil is by separating To light fraction and heavy distillat, cut point is 600 DEG C.Heavy distillat is handled by coking plant, then is isolated to coking vapour Oil, coker gas oil, wax tailings and coke.The operating condition of coking is 505 DEG C of reaction temperature, pressure 170000Pa.

By 25% catalytic cracking diesel oil of wax tailings and light fraction and catalytic cracking unit and whole catalytic cracking Heavy-cycle oil delivers to weighted BMO spaces reaction zone.Three weighted BMO spaces reactor catalyst fillings and inlet amount and chargeability Matter is identical.The weighted BMO spaces reactor A average reaction temperature is 365 DEG C, weighted BMO spaces reactor B average response Temperature is 375 DEG C, weighted BMO spaces reactor C average reaction temperatures are 385 DEG C, hydrotreating reactor D average response temperature Spend for 383 DEG C, catalyst loading pattern is shown in Table 3, and the residual hydrogenation operating condition is shown in Table 5, specific residual hydrogenation reaction result It is shown in Table 7.Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 8, and specific catalytic cracking catalyst property is shown in Table 9, catalytic cracking product distribution of products Property is shown in Table 10.

Comparative example 1

Also 4 reactors, respectively reactor A, reactor B, reactor C, reactor D, reactor are used in comparative example 1 A, reactor B, reactor C are connected with reactor D in the form of being sequentially connected in series.Raw materials used A properties are shown in Table 1 in comparative example 1, The inlet amount and feed properties of reactor A are identical with the total feed and feed properties of embodiment 1.It is the reactor A, anti- Answer device B, reactor C and reactor D catalyst inventory weighted BMO spaces reactor A corresponding with embodiment, weighted BMO spaces Reactor B, weighted BMO spaces reactor C, hydrodesulphurisatioreactors reactors D are identical, but the loadings of various species catalyst are Difference, loaded in the way of in table 4.The catalytic cracking diesel oil that catalytic cracking unit obtains directly goes out device, catalytic cracking weight Recycle oil cracks in catalytic cracking unit inner loop.The residual hydrogenation operating condition is shown in Table 6, and specific reaction result is shown in Table 7. Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 8, and specific catalytic cracking catalyst property is shown in Table 9, and catalytic cracking product distribution of products property is shown in Table 10.

Comparative example 2

Also 4 reactors, respectively reactor A, reactor B, reactor C, reactor D, reactor are used in comparative example 2 A, reactor B, reactor C are connected with reactor D in the form of being sequentially connected in series.Raw material B is used in comparative example 2, property is shown in Table 1, reactor A entrance is identical with inlet amount and feed properties that embodiment 2 is total.The reactor A, reactor B, reactor C and reactor D catalyst inventory weighted BMO spaces reactor A corresponding with embodiment 2, weighted BMO spaces reactor B plus Hydrogen pretreatment reactor C, hydrodesulphurisatioreactors reactors D are identical, but the loadings of various species catalyst are different, according to table Mode in 4 is loaded, and the residual hydrogenation operating condition is shown in Table 6, and specific reaction result is shown in Table 7.Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 8, specific catalytic cracking catalyst property are shown in Table 9, and catalytic cracking product distribution of products property is shown in Table 10.Catalytic cracking unit obtains To catalytic cracking diesel oil directly go out device, heavy catalytic cycle oil cracks in catalytic cracking unit inner loop.

Comparative example 3

Also 4 reactors, respectively reactor A, reactor B, reactor C, reactor D, reactor are used in comparative example 3 A, reactor B, reactor C are connected with reactor D in the form of being sequentially connected in series.Comparative example 3 uses raw material A, raw material B, raw material C Equal proportion mixed material, reactor A, reactor B, reactor C and reactor D are using the form of series connection, reactor A in comparative example Entrance is identical with inlet amount and mixed feeding property that embodiment 3 is total.The reactor A, reactor B, reactor C and reactor D catalyst inventory weighted BMO spaces reactor A corresponding with embodiment, weighted BMO spaces reactor B, weighted BMO spaces reaction Device C, hydrodesulphurisatioreactors reactors D are identical, but the loadings of various species catalyst are different, are filled in the way of in table 4 Fill out, the residual hydrogenation operating condition is shown in Table 6, and specific reaction result is shown in Table 7.Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 8, specific catalysis Cracking catalyst property is shown in Table 9, and catalytic cracking product distribution of products property is shown in Table 10.The catalytic cracking that catalytic cracking unit obtains Diesel oil directly goes out device, and heavy catalytic cycle oil cracks in catalytic cracking unit inner loop.

Comparative example 4

Also 4 reactors, respectively reactor A, reactor B, reactor C, reactor D, reactor are used in comparative example 4 A, reactor B, reactor C are connected with reactor D in the form of being sequentially connected in series.Comparative example 4 uses raw material C, and property is shown in Table 1, Using the form of series connection, reactor A entrance and embodiment 4 are total by reactor A, reactor B, reactor C and reactor D in comparative example Inlet amount it is identical with feed properties.The reactor A, reactor B, reactor C and reactor D catalyst inventory and reality Apply example and correspond to weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C, hydrodesulphurisatioreactors reactors D It is identical, but the loadings of various species catalyst are different, loaded in the way of in table 4, the residual hydrogenation operation Condition is shown in Table 6, and specific reaction result is shown in Table 7.Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 8, and specific catalytic cracking catalyst property is shown in Table 9, catalytic cracking product distribution of products property is shown in Table 10.

The catalytic cracking diesel oil that catalytic cracking unit obtains directly goes out device, and heavy catalytic cycle oil fills in catalytic cracking Put inner loop cracking.

The residual oil raw material property of table 1

The catalytic cracking diesel oil of table 2 and heavy-cycle oil property

Catalyst loading pattern in the embodiment 1~4 of table 3

Catalyst loading pattern in the comparative example 1~4 of table 4

The residual hydrogenation reaction condition of the embodiment 1~4 of table 5

The residual hydrogenation reaction condition of the comparative example 1~4 of table 6

The steady running cycle of table 7 and residual hydrogenation generation oil nature

The catalytic cracking process condition of table 8

The catalytic cracking catalyst physico-chemical property of table 9

The catalytic cracking product distribution results of table 10 and catalytically cracked gasoline property

Claims

1. a kind of process for handling residual oil, weighted BMO spaces unit, coking plant, hydrotreating unit and catalytic cracking dress Put, the hydrotreating unit includes weighted BMO spaces reaction zone and hydrotreating reaction area, and methods described includes herein below：

（1）Feedstock oil enters weighted BMO spaces unit after being mixed with hydrogen, reaction generation oil is fractionated into obtaining light fraction and double distilled Point, cutting point range is 500-650 DEG C；

（2）Step（1）Obtained heavy distillat enters coking plant, obtained after processing coker gasoline, coker gas oil, wax tailings and Coke；

（3）Step（1）Obtained light fraction, step（2）Obtained wax tailings pass through successively after being mixed with hydrogen to be arranged in series Weighted BMO spaces reaction zone and hydrotreating reaction area, the reaction effluent in hydrotreating reaction area carry out gas-liquid separation, point Weighted BMO spaces reaction zone and/or hydrotreating reaction area are recycled back to from obtained gas phase, isolated liquid phase is directly entered Catalytic cracking reaction zone carries out catalytic cracking reaction, catalytic cracking reaction effluent isolated dry air-liquid in fractionating device Change gas, catalytically cracked gasoline cut, catalytic cracking diesel oil cut, heavy catalytic cycle oil and catalytic cracked oil pulp；It is described to add Hydrogen pretreatment reaction zone includes the weighted BMO spaces reactor that two more parallels are set, when in the weighted BMO spaces reaction zone When the pressure drop of First weighted BMO spaces reactor reaches the 50%~80% of the reactor design pressure drop upper limit, by the weighted BMO spaces Reactor is cut out from weighted BMO spaces reaction zone, and it is anti-that the weighted BMO spaces reactor is named as to the weighted BMO spaces cut out Device I is answered, and according to material successively by weighted BMO spaces reaction zone, the weighted BMO spaces reactor I cut out, hydrotreating reaction The order in area is by weighted BMO spaces reactor that this cuts out and weighted BMO spaces reaction zone and hydrotreating reaction area to connect Mode connects, the now charging of the weighted BMO spaces reactor cut out be the weighted BMO spaces reactor that cuts out except this it The reaction effluent of outer weighted BMO spaces reactor, when the pressure drop of next weighted BMO spaces reactor reaches reactor design The pressure drop upper limit 50%~80% when, the weighted BMO spaces reactor is cut out from weighted BMO spaces reaction zone, and this is cut out Weighted BMO spaces reactor be named as the weighted BMO spaces reactor II cut out, and pass through weighted BMO spaces successively according to material Reaction zone, the weighted BMO spaces reactor II cut out, the weighted BMO spaces reactor I cut out, the order in hydrotreating reaction area By weighted BMO spaces reactor II that this cuts out and weighted BMO spaces reaction zone and the weighted BMO spaces reactor I cut out to connect Mode connect, the weighted BMO spaces reactor II now cut out charging is that weighted BMO spaces reaction zone removes the hydrogenation cut out The reaction effluent of remaining weighted BMO spaces reactor outside preatreating reactors, in the manner described above, until all adds Hydrogen pretreatment reactor is all connected in series to.

2. in accordance with the method for claim 1, it is characterised in that：The weighted BMO spaces reaction zone includes two more parallels The weighted BMO spaces reactor of setting, when the pressure drop of First weighted BMO spaces reactor in the weighted BMO spaces reaction zone reaches When designing the 60%~70% of the pressure drop upper limit to reactor, the weighted BMO spaces reactor is cut from weighted BMO spaces reaction zone Go out, and the weighted BMO spaces reactor is named as to the weighted BMO spaces reactor I cut out, and according to material successively by being hydrogenated with The weighted BMO spaces that pretreatment reaction area, the weighted BMO spaces reactor I cut out, the order in hydrotreating reaction area cut out this Reactor is connected in series to weighted BMO spaces reaction zone and hydrotreating reaction area, now the hydrogenation cut out The charging of preatreating reactors is the reaction stream of the weighted BMO spaces reactor in addition to the weighted BMO spaces cut out the reactor Go out thing, when the pressure drop of next weighted BMO spaces reactor reach reactor design the pressure drop upper limit 60%~70% when, by this plus Hydrogen pretreatment reactor is cut out from weighted BMO spaces reaction zone, and the weighted BMO spaces reactor that this cuts out is named as and cut out Weighted BMO spaces reactor II, and reacted successively by weighted BMO spaces reaction zone, the weighted BMO spaces that cut out according to material The weighted BMO spaces reactor II that device II, the weighted BMO spaces reactor I cut out, the order in hydrotreating reaction area cut out this It is connected in series to weighted BMO spaces reaction zone and the weighted BMO spaces reactor I cut out, the hydrogenation now cut out is pre- Treatment reactor II charging is remaining hydrogenation of weighted BMO spaces reaction zone in addition to the weighted BMO spaces reactor cut out The reaction effluent of preatreating reactors, in the manner described above, until all weighted BMO spaces reactors are all with series connection Mode connect.

3. in accordance with the method for claim 1, it is characterised in that：All hydrogenation in the weighted BMO spaces reaction zone are located in advance Reach the 50%~80% of the reactor pressure decrease design upper limit when managing reactor difference.

4. in accordance with the method for claim 3, it is characterised in that：By process conditions, the difference with beds property is set It is different cause each weighted BMO spaces reactor difference of weighted BMO spaces reaction zone when reach reactor pressure decrease design the upper limit 50%~ 80%。

5. in accordance with the method for claim 4, it is characterised in that：It is different in each weighted BMO spaces reactor by controlling Catalyst packing height, different inlet amounies, different feed properties, different operating conditions, identical filling height condition The lower one or more using in different Catalyst packing density reach to realize during each weighted BMO spaces reactor difference The 50%~80% of the reactor pressure decrease design upper limit.

6. in accordance with the method for claim 5, it is characterised in that：When the weighted BMO spaces reaction zone each hydrogenation in parallel When preatreating reactors uses different Catalyst packing density, the weighted BMO spaces reaction zone each hydrogenation in parallel is located in advance Manage in reactor, maximum loading density is 400kg/m³~600kg/m³, minimum loading density is 300kg/m³~550kg/m³。

7. in accordance with the method for claim 5, it is characterised in that：When the weighted BMO spaces reaction zone each hydrogenation in parallel When preatreating reactors uses different Catalyst packing density, the weighted BMO spaces reaction zone each hydrogenation in parallel is located in advance Manage in reactor, maximum loading density is 450kg/m³~550kg/m³, minimum loading density is 350kg/m³~450kg/m³。

8. according to the method described in claim 6 or 7, it is characterised in that：The immediate pre- place of two hydrogenation of loading density The Catalyst packing density difference for managing reactor is 50~200kg/m³。

9. according to the method described in claim 6 or 7, it is characterised in that：The immediate pre- place of two hydrogenation of loading density The Catalyst packing density difference for managing reactor is 80~150kg/m³。

10. in accordance with the method for claim 5, it is characterised in that：Each when weighted BMO spaces reaction zone parallel connection adds When hydrogen pretreatment reactor uses different inlet amounies, the feed volume of the immediate two weighted BMO spaces reactors of inlet amount The ratio between air speed is 1.1 ~ 3.0.

11. according to the method described in claim 5 or 10, it is characterised in that：When in parallel each of the weighted BMO spaces reaction zone When platform weighted BMO spaces reactor uses different inlet amounies, the charging of the immediate two weighted BMO spaces reactors of inlet amount The ratio between volume space velocity is 1.1 ~ 1.5.

12. in accordance with the method for claim 5, it is characterised in that：Each when weighted BMO spaces reaction zone parallel connection adds When hydrogen pretreatment reactor uses different feed properties, the metal of the immediate two weighted BMO spaces reactors of feed properties Content difference is 5 ~ 50 μ g/g.

13. according to the method described in claim 5 or 12, it is characterised in that：When in parallel each of the weighted BMO spaces reaction zone When platform weighted BMO spaces reactor uses different feed properties, the immediate two weighted BMO spaces reactors of feed properties Tenor difference is 10 ~ 30 μ g/g.

14. in accordance with the method for claim 5, it is characterised in that：Each when weighted BMO spaces reaction zone parallel connection adds When hydrogen pretreatment reactor uses different operating conditions, control operation pressure and the immediate pre- place of two hydrogenation of volume space velocity In the operating condition for managing reactor, operation temperature difference is 2 ~ 30 DEG C.

15. according to the method described in claim 5 or 14, it is characterised in that：When in parallel each of the weighted BMO spaces reaction zone When platform weighted BMO spaces reactor uses different operating conditions, control operation pressure and immediate two hydrogenation of volume space velocity In the operating condition of preatreating reactors, operation temperature difference is 5 ~ 20 DEG C.

16. in accordance with the method for claim 1, it is characterised in that：The catalytic cracking vapour that the catalytic cracking reaction zone obtains One or more in oil distillate, catalytic cracking diesel oil cut, heavy catalytic cycle oil are recycled back to weighted BMO spaces reaction zone.

17. in accordance with the method for claim 1, it is characterised in that：The cycle oil that the catalytic cracking reaction zone obtains Slurry is recycled back to coking plant and handled.

18. in accordance with the method for claim 16, it is characterised in that：It is recycled back to the catalytic cracking vapour of weighted BMO spaces reaction zone One in the weighted BMO spaces reactor that oil distillate, catalytic cracking diesel oil cut, heavy catalytic cycle oil entrance are arranged in parallel Platform or several.

19. in accordance with the method for claim 1, it is characterised in that：The weighted BMO spaces reaction zone includes more than two simultaneously Join the weighted BMO spaces reactor set.

20. according to the method described in claim 1 or 19, it is characterised in that：The weighted BMO spaces reaction zone includes 3~6 The weighted BMO spaces reactor being arranged in parallel.

21. according to the method described in claim 1 or 19, it is characterised in that：The weighted BMO spaces reaction zone includes 3 or 4 The weighted BMO spaces reactor that platform is arranged in parallel.

22. in accordance with the method for claim 1, it is characterised in that：Described hydrotreating reaction area includes 1~5 series connection The hydrotreating reactor of setting.

23. according to the method described in claim 1 or 22, it is characterised in that：Described hydrotreating reaction area includes 1~2 The hydrotreating reactor being arranged in series.

24. in accordance with the method for claim 1, it is characterised in that：The operating condition of the weighted BMO spaces reaction zone is：Instead It is 370 DEG C~420 DEG C to answer temperature, and reaction pressure be 10MPa~25MPa, and hydrogen to oil volume ratio is 300~1500, during raw material fluid Volume space velocity is 0.15h^-1~2.00h^-1。

25. in accordance with the method for claim 24, it is characterised in that：The operating condition of the weighted BMO spaces reaction zone is： Reaction temperature is 380 DEG C~400 DEG C, and reaction pressure be 15MPa~20MPa, and hydrogen to oil volume ratio is 500~800, during raw material fluid Volume space velocity is 0.3h^-1~1.00h^-1。

26. in accordance with the method for claim 1, it is characterised in that：The operating condition in the hydrotreating reaction area is：Reaction Temperature is 370 DEG C~430 DEG C, and reaction pressure be 10MPa~25MPa, and hydrogen to oil volume ratio is 300~1500, body during raw material fluid Product air speed is 0.15h^-1~0.80h^-1。

27. in accordance with the method for claim 26, it is characterised in that：The operating condition in the hydrotreating reaction area is reaction Temperature is 380 DEG C~410 DEG C, and reaction pressure be 15MPa~20MPa, and hydrogen to oil volume ratio is 400~800, volume during raw material fluid Air speed is 0.2h^-1~0.60h^-1。

28. in accordance with the method for claim 1, it is characterised in that：Described feedstock oil is reduced crude or decompression residuum, Or contain straight-run gas oil, and decompressed wax oil, the one or more in secondary operation wax oil and FCC recycle oil.

29. in accordance with the method for claim 1, it is characterised in that：The operating condition of the catalytic cracking reaction zone is：Reaction Temperature is 450~600 DEG C, and regeneration temperature is 600~800 DEG C, agent weight of oil than 2~30, with catalyst contact time for 0.1~ 15 seconds, pressure was 0.1~0.5MPa.

30. in accordance with the method for claim 1, it is characterised in that：The operating condition of the catalytic cracking reaction zone is：Reaction Temperature is 480~550 DEG C；Regeneration temperature is 650~750 DEG C, and agent weight of oil is than 4~10；With catalyst contact time be 0.5~ 5 seconds；Pressure is 0.1~0.5MPa.

31. in accordance with the method for claim 1, it is characterised in that：The coker operations condition is：Pressure be 1~ 3MPa, temperature are 450~550 DEG C.

32. according to the method described in claim 31, it is characterised in that：The coker operations condition is：Pressure be 1~ 2MPa；Temperature is 480~520 DEG C.