CN106701187A - Method for treating residual oil - Google Patents
Method for treating residual oil Download PDFInfo
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- CN106701187A CN106701187A CN201510769138.2A CN201510769138A CN106701187A CN 106701187 A CN106701187 A CN 106701187A CN 201510769138 A CN201510769138 A CN 201510769138A CN 106701187 A CN106701187 A CN 106701187A
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- weighted bmo
- bmo spaces
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
- C10G2300/1007—Used oils
Abstract
The invention discloses a method for treating residual oil. A coking device, a hydrogenation pretreatment reaction area, a hydrogenation treatment reaction area and a catalytic cracking reaction area are provided, the method comprises the following steps: performing fractionation on a residual oil raw material so as to obtain light fraction and heavy fraction, feeding the heavy fraction into the coking device for treatment so as to obtain coked gasoline, coked diesel oil and coked wax oil, mixing the light fraction with the coked wax oil and hydrogen, passing through the hydrogenation pretreatment reaction area and the hydrogenation treatment reaction area which are connected in series, performing gas-liquid separation on a reaction effluent of the hydrogenation treatment reaction area, circulating vapor phase back to the hydrogenation pretreatment reaction area and/or the hydrogenation treatment reaction area, directly feeding liquid phase into the catalytic cracking reaction area for a catalytic cracking reaction, and separating a catalytic cracking reaction effluent, thereby obtaining a dry gas, a liquefied gas, catalytic cracking gasoline fraction, catalytic cracking area diesel oil fraction, catalytic cracking area recirculation oil and catalytic cracking area oil slurry. By adopting the method disclosed by the invention, the stable operation period of a device can be prolonged.
Description
Technical field
The present invention relates to a kind of method that heavy oil lightening method, more particularly to a kind of use coking-hydrogenation-catalytic cracking combined technological process heavy oil.
Background technology
At present, it will be in the lasting trend for rising that domestic and international refined products market is particularly to the demand of motor petrol to the demand of the oil products such as steam coal bavin, and then on a declining curve to the demand of the heavy oil products such as heavy fuel oil.Meanwhile, oil property is deteriorated increasingly in the world, and environmental regulation is increasingly strict, and increasingly strict requirements are proposed to oil quality.Therefore, how to realize that heavy oil lighting and petrol and diesel oil product quality are persistently upgraded with more economical rational cost has turned into oil refining industry focus of attention both at home and abroad.
The main purpose of residual hydrocracking technique is by hydrotreating, the sulphur in residual oil raw material, nitrogen, metal impurities content is greatly reduced, the undesirable components hydro-conversion such as condensed-nuclei aromatics, colloid, asphalitine improves hydrogen-carbon ratio, reduce carbon residue content, make its cracking performance be improved significantly.Fixed bed residual hydrogenation technology is a kind of heavy oil deep processing technology, in the fixed bed reactors equipped with special catalyst, under the hydro condition of HTHP, desulfurization, denitrogenation, demetalization etc. are carried out to normal pressure or decompression residuum, it is one of important means of residual oil weight-lightening to obtain light-end products to greatest extent.Fixed bed residual hydrogenation technology is high with its liquid product yield, good product quality, and production chains are strong, and waste, waste material are few, environment-friendly, the advantages of rate of return on investment is high, is increasingly widely applied.
The setting of fixed bed residual hydrocracking process reaction partial reaction device is typically used in series by multiple reactors or bed, and the property, reaction condition and purpose product requirement according to original oil optimize the formulation of catalyst, carry out grading loading according to different physical properties, catalyst activity and all kinds of catalyst ratios.Although fixed bed residual hydrogenation technology has many advantages, such as, in process of production, but easily there is the phenomenon of reactor pressure drop increase.Industrial operation shows that reactor pressure drop increase is one of key factor of confining device full production and long-term operation.Especially many reactor series connection, load is reacted in demetalization of the preposition reactor due to assume responsibility for more than 70%, metal sulfide is deposited on beds, having arrived the operation middle and later periods inevitably there is pressure drop rapid growth, and reactor below is substantially relatively low due to demetalization load, pressure drop increases slower.This has occurred as soon as anterior reactor and reactor load distribution in rear portion is uneven, have impact on the stable operation of the cycle of operation and device of device.
CN103059928A discloses a kind of hydrotreater and its application and process for hydrogenating residual oil.The invention provides a kind of and its processing unit, and the device includes the hydrogenation insured unit and main hydrotreating unit once connected.Described hydrogenation protecting unit includes main hydrogenation protecting reactor and standby hydrogenation protecting reactor in parallel, and main hydrogenation protecting reactor volume is more than stand-by protection reactor.In hydroprocessing processes, main hydrogenation protecting reactor is used alternatingly with standby hydrogenation protecting reactor.The process is by main hydrogenation protecting reactor and standby hydrogenation protecting reactor handover operation; the residual oil of high calcium high metal content can be processed; have the disadvantage the reactor that left unused, increase investment and reduce reactor utilization rate, and lead reactor pressure drop growing concern can not be solved from not catching up with.
CN1393515A discloses a kind of method of residual hydrocracking.The method is that first reactor in heavy resid hydrogenation reaction system sets up one or more charging apertures, change original catalyst grade simultaneously to match somebody with somebody, when an anticatalyst bed pressure drop designs 0.4~0.8 times of pressure drop for device, use next charging aperture instead successively, original charging aperture can enter the miscella of recycle oil or recycle oil and original oil simultaneously, 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.Have the disadvantage that inductor manufacturing cost increases, increase initial drop, device inner volume utilization rate reduction etc..
CN103059931A discloses a kind of method of residual hydrocracking.The method is at hydrotreating reaction conditions, residual oil raw material and hydrogen many reactors once by connecting, when plant running carries out triage operator after 700~4000 hours, reduce an anti-inlet amount or keep an anti-inlet amount constant, increase the inlet amount of an each reactor instead and in the middle of last reactor, increased feed residue injects in the entrance of intermediate reactor.The method alleviates the growth of pressure drop by changing each anti-feed loading, but can not fundamentally change the growth trend of lead reactor pressure drop, from the point of view of industrial actual motion, pressure drop can quickly reach the design upper limit once growth, and change 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 method for processing residual oil.The method technological process is simple, it is only necessary to carry out simple modifications to existing apparatus, it is possible to significantly extend the service cycle of whole device, it is possible to make the utilization ratio of catalyst realize maximizing.
Existing residual hydrocracking technology; all reactors are using the technological process connected; therefore need to load substantial amounts of protective agent in First reactor to deposit the impurity in raw material and dirty thing; so operation can cause First to protect the antigravity system of filling in reactor because activity is relatively low; demetalization load is relatively low; plant running latter stage reactor pressure decrease has been arrived in some cases still very low so that the ability reduction that is de-, holding metallic compound of integer catalyzer.If improving its catalyst activity can cause the rapid growth of pressure drop again,Shorten the cycle of operation,And follow-up catalyst performance is not played also completely,The activity for keeping First protection reactor catalyst appropriate is difficult control,And there is for example urgent shutting down of several factors during residual hydrogenation equipment whole service,Feedstock property fluctuates,Or Fe in raw material,Ca impurity increases suddenly,Therefore common practice is still to maintain the activity of the relatively low reaction of an anti-protection reactor catalyst,Its Main Function intercepts and deposits impurity and dirty thing in raw material,Only carry out relatively low demetalization reaction,The typically reactor reaction temperature rise is relatively low,Pressure drop maintains relatively low level in the whole service cycle,So require to be substantially carried out demetalization reaction in the follow-up demetalization reactor substantial amounts of catalyst for demetalation of filling and provide enough spaces to accommodate the metallic compound and carbon distribution of hydrogenation and removing,So inevitably cause to deposit substantial amounts of metal in the demetalization reactor,Demetalization reaction load is larger,The typically reactor reaction temperature rise highest,Although initial operating stage reactor pressure decrease is relatively low,But increase at first to operation to the pressure drop of mid-term or the later stage pressure drop reactor,And increase most fast,Principal element as the restriction cycle of operation.
The present invention provides a kind of method for processing residual oil, including coking plant, weighted BMO spaces reaction zone, hydrotreating reaction area and catalytic cracking reaction zone；Methods described includes herein below：
（1）Feedstock oil is fractionated into obtaining light fraction and heavy distillat, and cut point is 500~650 DEG C；
（2）The heavy distillat enters coking plant, and coker gasoline, coker gas oil, wax tailings and coke are obtained after treatment；
（3）Step（1）Light fraction, the step for obtaining（2）The wax tailings for obtaining sequentially pass through the weighted BMO spaces reaction zone and hydrotreating reaction area being arranged in series after mixing with hydrogen, the reaction effluent in hydrotreating reaction area carries out gas-liquid separation, isolated gas phase loops back weighted BMO spaces reaction zone and/or hydrotreating reaction area, isolated 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 weighted BMO spaces reaction zone includes the weighted BMO spaces reactor that two more parallels are set,When the pressure drop of any weighted BMO spaces reactor in the weighted BMO spaces reaction zone reaches the 50%~80% of the reactor design pressure drop upper limit,It is preferred that when 60%~70%,The weighted BMO spaces reactor is cut out from weighted BMO spaces reaction zone,And the weighted BMO spaces reactor is named as the weighted BMO spaces reactor I for cutting out,And sequentially pass through weighted BMO spaces reaction zone according to material,The weighted BMO spaces reactor I for cutting out,With weighted BMO spaces reaction zone and hydrotreating reaction area be connected in series to the weighted BMO spaces reactor for cutting out by the order in hydrotreating reaction area,The charging of the weighted BMO spaces reactor that now this cuts out is the reaction effluent of the weighted BMO spaces reactor in addition to the weighted BMO spaces for the cutting out reactor,When the pressure drop of next weighted BMO spaces reactor reaches the 50%~80% of the reactor design pressure drop upper limit,It is preferred that when 60%~70%,The weighted BMO spaces reactor is cut out from weighted BMO spaces reaction zone,And the weighted BMO spaces reactor for cutting out is named as the weighted BMO spaces reactor II for cutting out,And sequentially pass through weighted BMO spaces reaction zone according to material,The weighted BMO spaces reactor II for cutting out,The weighted BMO spaces reactor I for cutting out,With weighted BMO spaces reaction zone and the weighted BMO spaces reactor I for cutting out be connected in series to the weighted BMO spaces reactor II for cutting out by the order in hydrotreating reaction area,The charging of the weighted BMO spaces reactor II for now cutting out is the reaction effluent of remaining weighted BMO spaces reactor of the weighted BMO spaces reaction zone in addition to the weighted BMO spaces reactor for having cut out,In the manner described above,Until all of weighted BMO spaces reactor is all connected in series to.
In the inventive method, one or more in catalytically cracked gasoline cut, catalytic cracking diesel oil cut, heavy catalytic cycle oil that catalytic cracking reaction is obtained can loop back weighted BMO spaces reaction zone carries out hydrogenation reaction.
In the inventive method, the catalytic cracked oil pulp that catalytic cracking reaction is obtained can loop back coking plant and be processed.
In the inventive method, all weighted BMO spaces reactors in the weighted BMO spaces reaction zone reach the 50%~80% of the reactor pressure decrease design upper limit when different, can cause to reach pressure drop designs the upper limit 50%~80% when each weighted BMO spaces reactor of weighted BMO spaces reaction zone is different by process conditions setting and the difference of beds property.Specifically can be by controlling catalyst packing heights different in each weighted BMO spaces reactor, different inlet amounies, different feed properties, different operating conditions, reaches the 50%~80% of the pressure drop design upper limit when can realize that each weighted BMO spaces reactor is different using one or more in the means such as different Catalyst packing density under the conditions of identical filling height.
As described above, when the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel uses different Catalyst packing density, in the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel, maximum loading density is 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 density difference of the immediate two weighted BMO spaces reactors of loading density is 30~200kg/m3, preferably 50~150kg/m3.When other conditions are consistent, the Catalyst packing density of the weighted BMO spaces reactor that will be cut out first is maximum, and the Catalyst packing density of the weighted BMO spaces reactor being finally cut out is minimum.The different loading densities can be tamped now by the way that different types of catalyst grade is equipped, such as can in different proportions realize that the Catalyst packing density in each weighted BMO spaces reactor is different by hydrogenation protecting agent, Hydrodemetalation catalyst, Hydrobon catalyst.
As described above, when the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel uses different inlet amounies, the ratio between feed volume air speed of the immediate two weighted BMO spaces reactors of inlet amount is 1.1 ~ 3.0, preferably 1.1 ~ 1.5.
As described above, when the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel uses different feed properties, the tenor difference of the immediate two weighted BMO spaces reactors of feed properties is 5 ~ 50 μ g/g, preferably 10 ~ 30 μ g/g.
As described above, when the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel uses different operating conditions, can be so that in the operating condition of the immediate two weighted BMO spaces reactors of control operation pressure and volume space velocity, operation temperature difference be 2 ~ 30 DEG C, preferably 5 ~ 20 DEG C.
In the inventive method, one or several that the catalytically cracked gasoline cut of weighted BMO spaces reaction zone, catalytic cracking diesel oil cut, heavy catalytic cycle oil can enter in the weighted BMO spaces reactor being arranged in parallel is looped back, preferably different weighted BMO spaces reactors is respectively enterd in suitable ratio.
In the inventive method, the weighted BMO spaces reaction zone includes the weighted BMO spaces reactor that two more parallels are set, and 3~6 weighted BMO spaces reactors being arranged in parallel is preferably included, more preferably including the 3 or 4 weighted BMO spaces reactors being arranged in parallel.Described hydrotreating reaction area includes 1~5 hydrotreating reactor being arranged in series, and preferably includes 1~2 hydrotreating reactor 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, and 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.Apparently higher than the reaction temperature of the residuum hydrogenating and metal-eliminating reactor of prior art, the residuum hydrogenating and metal-eliminating reaction temperature of prior art is usually 350 DEG C~390 DEG C to the average reaction temperature of weighted BMO spaces reaction zone.The optimization that the weighted BMO spaces reaction zone that this method middle front part is set passes through technological process, eliminate the unfavorable factor that pressure drop increases restrictive cycle, can operate at high temperature, reaction temperature relatively high is conducive to the performance of loaded catalyst system performance in addition, is conducive to the removing of the hydro-conversion and impurity of macromolecular.
In the inventive method, the operating condition in the hydrotreating reaction area is that reaction temperature is 370 DEG C~430 DEG C, and preferably 380 DEG C~410 DEG C, reaction pressure is 10MPa~25MPa, preferably 15MPa~20MPa；Hydrogen to oil volume ratio is 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 familiar 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, and coker naphtha and fraction of coker gas oil can respectively go respective device of re-refining to be processed, and wax tailings deliver to hydrogenation reaction system of the invention and carry out hydrotreating.And coke can go to make electrode or deoxidation hydrogen manufacturing and make fuel according to the number of its impure amount.
In the inventive method, catalytic cracking can use this area routine techniques.Catalytic cracking unit can be that more than a set of or a set of, often covering catalytic cracking unit should at least include a reactor and a regenerator, and catalytic cracking unit need to set fractionating column, can be respectively provided with fractionating column with every set catalytic cracking unit, it is also possible to share fractionating column.The fractionation of catalytic cracking reaction effluent is dry gas, liquefied gas, catalytically cracked gasoline cut, catalytic cracking diesel oil cut, catalytic cracking recycle oil and catalytic cracked oil pulp etc. by fractionating column.Catalytic cracking fractionating tower can routinely knowledge design.
In the inventive method, the operating condition of the catalytic cracking reaction zone is：Reaction temperature is 450~600 DEG C, preferably 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.The catalytic cracking catalyst for being used includes being generally used for the catalyst of catalytic cracking, such as silica-alumina catalyst, silica-magneia cataslyst, the carclazyte of acid treatment and X-type, Y types, ZSM-5, M type, layer post equimolecular sieve Cracking catalyst, preferably molecular sieve cracking catalyst, because the activity of molecular sieve cracking catalyst is high, green coke is few, gasoline yield is high, high conversion rate.The reactor of described catalytic cracking unit can be the catalyst cracker of various types, and preferably riser reactor or riser adds bed reactor.Technological process is generally：Feedstock oil is injected from riser reactor bottom, is contacted with the high-temperature regenerated catalyst from regenerator, and the oil gas of cracking reaction generation and the catalyst mixture of deposit coke are moved up along riser reactor, complete the catalytic cracking reaction of whole feedstock oil.
In the inventive method, residual hydrogenation technology uses fixed bed residual hydrocracking technology, hydrogenation protecting agent can be loaded in each weighted BMO spaces reactor of the weighted BMO spaces reaction zone, Hydrodemetalation catalyst, Hydrobon catalyst, one or more in hydrodenitrogeneration carbon residue reforming catalyst, one or more in Hydrobon catalyst and hydrodenitrogeneration carbon residue reforming catalyst can be loaded in the hydrotreating reaction area, the hydrogenation protecting agent, Hydrodemetalation catalyst, Hydrobon catalyst, hydrodenitrogeneration carbon residue reforming catalyst is the catalyst used by fixed bed residual hydrocracking process.Above-mentioned catalyst is typically all with porous refractory inorganic oxide such as aluminum oxide as carrier, the oxide of vib and/or group VIII metal such as W, Mo, Co, Ni etc. is active component, it is selectively added the catalyst of the elements such as other various auxiliary agents such as P, Si, F, B, the FZC series catalyst for hydrotreatment of residual oil for for example being produced by catalyst branch company of Sinopec Group.
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, one or more in secondary operation wax oil and FCC recycle oil.Described residual oil raw material property is：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%, and 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 many weighted BMO spaces reactors of parallel connection so that whole catalyst system takes off/holds metal ability and is increased dramatically.
2nd, the inventive method is matched somebody with somebody by carrying out catalyst grade in each weighted BMO spaces reactor in weighted BMO spaces reaction zone, during so that the pressure drop of reactor rising to setting value, by the change of technological process, it is cut out from weighted BMO spaces reaction zone, change optimizes its feed properties, make its pressure drop no longer rapid growth, but can increase until device is stopped work with slow in control range, and then the pressure drop of certain weighted BMO spaces reactor is not restricted cycle of operation of whole device.
3rd, the inventive method is optimized and revised by weighted BMO spaces reaction zone catalyst performance and technological parameter, with the cooperation of the de- carbon residue catalyst of follow-up high activity desulfurization so that the de- carbon residue performance of desulfurization is guaranteed while the de-/appearance metal ability of integer catalyzer is improved.
4th, the inventive method solves the problem of reactor pressure decrease rapid growth by by each weighted BMO spaces reactor of weighted BMO spaces reaction zone from the adjustment for being parallel to series connection handover operation mode, while increased the operating flexibility and raw material adaptability of device；
5th, the appearance amount of metal of catalyst system is significantly increased by setting weighted BMO spaces reactor parallel form for the inventive method 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 are synchronously inactivated, so as to improve the operational efficiency of device, 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 in weighted BMO spaces reactor successively, Hydrobon catalyst can also be selectively loaded below Hydrodemetalation catalyst.Such catalyst loading pattern so that whole system takes off/holds metal ability and is increased dramatically, while the pressure drop for causing each preatreating reactors by the adjustment that catalyst grade is matched somebody with somebody increases in control range.The catalyst system of weighted BMO spaces reaction zone each weighted BMO spaces reactor filling in parallel is based on de-/appearance metal function, so that while demetalization performance boost, strengthen the ability to the hydro-conversion of such as gum asphalt of macromolecular in raw material, it is that successive depths desulfurization and the conversion of carbon residue lay the foundation, so that hydrodesulfurizationreaction reaction zone is conducive to further deep reaction, therefore compared with routine techniques, although the ratio of Hydrodemetalation catalyst improves, but the hydro-conversion performance of the desulphurizing activated and carbon residue of entirety is not reduced not only and is improved on the contrary.
8th, in the inventive method, by residual hydrocracking, catalytic cracking and coking process organic assembling.The utilization ratio for realizing catalyst service cycle that the method can significantly extend residual hydrogenation equipment is maximized, and reduces the operating severity of residual hydrogenation equipment, extends the service life of catalyst, realizes the lightweight rate high 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 entered catalyst cracker, is not required to set feed pump, while reducing a large amount of heat transmission equipments.Equipment investment is set to be greatly reduced.
Brief description of the drawings
Fig. 1 is the method flow diagram of present invention treatment residual oil.
Specific embodiment
Method provided by the present invention is further detailed below in conjunction with the accompanying drawings, but is not thereby limited the invention.
As shown in figure 1, the method for present invention treatment residual oil includes herein below：Residual oil raw material 21 obtains light fraction 23 and heavy distillat 22 after being fractionated into device G fractionation,Heavy distillat 22 enters coking plant H,Coker gasoline 24 is obtained after treatment,Coker gas oil 26,Wax tailings 26 and coke 26,The light fraction 23,Wax tailings 26 are with the mixed material of hydrogen 28 through feeding line 1,Feeding line 2 and feeding line 3 enter the weighted BMO spaces reaction zone and hydrotreating reaction area being arranged in series,The weighted BMO spaces reaction zone includes three weighted BMO spaces reactors being arranged in parallel,Respectively weighted BMO spaces reactor A,Weighted BMO spaces reactor B,Weighted BMO spaces reactor C,The weighted BMO spaces reactor A,Weighted BMO spaces reactor B,The charging aperture of weighted BMO spaces reactor C respectively with feeding line 1,Feeding line 2 and feeding line 3 are connected,Three tunnels of the outlet of the weighted BMO spaces reactor A point,The first via is connected through pipeline 6 with the charging aperture of weighted BMO spaces reactor B,Second tunnel is connected through pipeline 7 with the charging aperture of weighted BMO spaces reactor C,3rd tunnel is connected through pipeline 10 with hydrotreating reactor D；Three tunnels of the outlet of the weighted BMO spaces reactor B point, the first via is connected through pipeline 4 with the charging aperture of weighted BMO spaces reactor A, and the second tunnel obtains charging aperture and is connected through pipeline 5 with weighted BMO spaces reactor C, and the 3rd tunnel is connected through pipeline 11 with hydrotreating reactor D；Three tunnels of the outlet of the weighted BMO spaces reactor C point, the first via is connected through pipeline 8 with the charging aperture of weighted BMO spaces reactor A, and the second tunnel is connected through pipeline 9 with the charging aperture of weighted BMO spaces reactor B, and the 3rd tunnel is connected through pipeline 12 with hydrotreating reactor D；Valve 101 is provided with the pipeline 1,Valve 102 is provided with the pipeline 2,Valve 103 is provided with the pipeline 3,Valve 104 is provided with the pipeline 4,Valve 105 is provided with the pipeline 5,Valve 106 is provided with the pipeline 6,Valve 107 is provided with the pipeline 7,Valve 108 is provided with the pipeline 8,Valve 109 is provided with the pipeline 9,Valve 1010 is provided with the pipeline 10,Valve 1011 is provided with the pipeline 11,Valve 1012 is provided with the pipeline 12,The generation oil 13 that the hydrotreating reactor is obtained obtains liquefied gas 20 and hydrogenated oil 14 after being separated into separator E,The hydrogenated oil 14 enters catalytic cracking reaction zone F,Catalytic cracking reaction is contacted and carried out with high temperature regeneration catalytic cracking catalyst,Product is fractionated into obtaining gas 15 after reaction,Catalytically cracked gasoline cut 16,Catalytic cracking diesel oil cut 17,Catalytic cracking recycle oil 18 and catalytic cracked oil pulp 19,Gas 15 and the discharger of catalytically cracked gasoline cut 16,Catalytic cracking diesel oil cut 17 and heavy catalytic cycle oil cut 18 return to weighted BMO spaces reaction zone,Weighted BMO spaces reaction zone is mixed into residual oil raw material to be reacted,Catalytic cracked oil pulp 19 can loop back coking plant or outer row.
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 the order of weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C
（1）When going into operation, valve 101, valve 102 on pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, pipeline 12, valve 103, valve 1010, valve 1011, valve 1012 are opened, and valve 104, valve 105 on pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, pipeline 9, valve 106, valve 107, valve 108, valve 109 are closed；
（2）When the pressure drop of weighted BMO spaces reactor A reaches critical value, close the valve 1012 of the valve 101, the valve 1011 of pipeline 11 and pipeline 12 of feeding line 1, the valve 104 on the valve 108 and pipeline 4 on pipeline 8 is opened, is now completed 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 valve 108 of pipeline 8 of feeding line 2 are closed, open the valve 109 on pipeline 9, now complete the 2nd handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor C 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
（1）When going into operation, valve 101, valve 102 on pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, pipeline 12, valve 103, valve 1010, valve 1011, valve 1012 are opened, and valve 104, valve 105 on pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, pipeline 9, valve 106, valve 107, valve 108, valve 109 are closed；
（2）When the pressure drop of weighted BMO spaces reactor A reaches critical value, close the valve 1012 of the valve 101, the valve 1011 of pipeline 11 and pipeline 12 of feeding line 1, the valve 104 on the valve 108 and pipeline 4 on pipeline 8 is opened, is now completed once by being parallel to the handover operation of series connection；
（3）When the pressure drop of weighted BMO spaces reactor C reaches critical value, valve 103, the valve 104 of pipeline 4 of feeding line 3 are closed, open the valve 105 on pipeline 5, now complete the 2nd handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor C reaches critical value, whole reaction system needs shutdown process.
3rd, inactivated according to the order of weighted BMO spaces reactor B, weighted BMO spaces reactor C, weighted BMO spaces reactor A
（1）When going into operation, valve 101, valve 102 on pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, pipeline 12, valve 103, valve 1010, valve 1011, valve 1012 are opened, and valve 104, valve 105 on pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, pipeline 9, valve 106, valve 107, valve 108, valve 109 are closed；
（2）When the pressure drop of weighted BMO spaces reactor B reaches critical value, close the valve 1012 of the valve 102, the valve 1010 of pipeline 10 and pipeline 12 of feeding line 2, the valve 106 on the valve 109 and pipeline 6 on pipeline 9 is opened, is now completed once by being parallel to the handover operation of series connection；
（3）When the pressure drop of weighted BMO spaces reactor C reaches critical value, valve 103, the valve 106 of pipeline 6 of feeding line 3 are closed, open the valve 107 on pipeline 7, 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 the order of weighted BMO spaces reactor B, weighted BMO spaces reactor A, weighted BMO spaces reactor C
（1）When going into operation, valve 101, valve 102 on pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, pipeline 12, valve 103, valve 1010, valve 1011, valve 1012 are opened, and valve 104, valve 105 on pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, pipeline 9, valve 106, valve 107, valve 108, valve 109 are closed；
（2）When the pressure drop of weighted BMO spaces reactor B reaches critical value, close the valve 1012 of the valve 102, the valve 1010 of pipeline 10 and pipeline 12 of feeding line 2, the valve 106 on the valve 109 and pipeline 6 on pipeline 9 is opened, is now completed once by being parallel to the handover operation of series connection；
（3）When the pressure drop of weighted BMO spaces reactor A reaches critical value, valve 101, the valve 109 of pipeline 9 of feeding line 1 are closed, open the valve 108 on pipeline 8, now complete the 2nd handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor C reaches critical value, whole reaction system needs shutdown process.
5th, inactivated according to the order of weighted BMO spaces reactor C, weighted BMO spaces reactor B, weighted BMO spaces reactor A
（1）When going into operation, valve 101, valve 102 on pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, pipeline 12, valve 103, valve 1010, valve 1011, valve 1012 are opened, and valve 104, valve 105 on pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, pipeline 9, valve 106, valve 107, valve 108, valve 109 are closed；
（2）When the pressure drop of weighted BMO spaces reactor C reaches critical value, close the valve 1011 of the valve 103, the valve 1010 of pipeline 10 and pipeline 11 of feeding line 3, the valve 105 on the valve 107 and pipeline 5 on pipeline 7 is opened, is now completed 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 valve 107 of pipeline 7 of feeding line 2 are closed, open the valve 106 on pipeline 6, 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.
6th, inactivated according to the order of weighted BMO spaces reactor C, weighted BMO spaces reactor A, weighted BMO spaces reactor B
（1）When going into operation, valve 101, valve 102 on pipeline 1, pipeline 2, pipeline 3, pipeline 10, pipeline 11, pipeline 12, valve 103, valve 1010, valve 1011, valve 1012 are opened, and valve 104, valve 105 on pipeline 4, pipeline 5, pipeline 6, pipeline 7, pipeline 8, pipeline 9, valve 106, valve 107, valve 108, valve 109 are closed；
（2）When the pressure drop of weighted BMO spaces reactor C reaches critical value, close the valve 1011 of the valve 103, the valve 1010 of pipeline 10 and pipeline 11 of feeding line 3, the valve 105 on the valve 107 and pipeline 5 on pipeline 7 is opened, is now completed once by being parallel to the handover operation of series connection；
（3）When the pressure drop of weighted BMO spaces reactor A reaches critical value, valve 101, the valve 105 of pipeline 5 of feeding line 1 are closed, open the valve 104 on pipeline 4, 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.
Effect of the invention is illustrated with reference to specific embodiment, it is raw materials used including three kinds in embodiment of the present invention and comparative example, respectively raw material A, raw material B, raw material C, specific nature is shown in Table 1, the type of feed of catalyst is shown in Table 3 in the embodiment 1~4, 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 is 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.Weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C described in the embodiment of the present invention are pattern, size identical reactor, reactor A, reactor B, reactor C in the comparative example are pattern, size identical reactor.
Embodiment 1
Raw material A is used described in embodiment 1（Property is shown in Table 1）By isolated light fraction and heavy distillat, cut point is 600 DEG C.Heavy distillat is processed 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.
50% catalytic cracking diesel oil and the heavy catalytic cycle oil of whole that wax tailings and light fraction and catalytic cracking unit are looped back deliver to weighted BMO spaces reaction zone.The weighted BMO spaces reactor A, weighted BMO spaces reactor B, the catalyst inventory of weighted BMO spaces reactor C, feed properties are identical with inlet amount, the weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C, the catalyst of hydrotreating reactor D are loaded according to the mode in table 3, the 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, and specific catalytic cracking catalyst property is shown in Table 9, and catalytic cracking product distribution of products property is shown in Table 10.
Embodiment 2
In embodiment 2, the use raw material B properties are shown in Table 1 by isolated light fraction and heavy distillat, and cut point is 610 DEG C.Heavy distillat is processed 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.
30% catalytic cracking diesel oil and the heavy catalytic cycle oil of whole of wax tailings and light fraction and catalytic cracking unit are delivered into weighted BMO spaces reaction zone.The weighted BMO spaces reactor A, weighted BMO spaces reactor B, the catalyst inventory of weighted BMO spaces reactor C, feed properties are identical, and Feed space velocities are different, and volume space velocity is 0.20h during the weighted BMO spaces reactor A liquid-1, volume space velocity is 0.32h during weighted BMO spaces reactor B liquid-1, volume space velocity is 0.44h during weighted BMO spaces reactor C liquid-1.Identical catalyst loading pattern, catalyst loading pattern is used to be shown in Table 3 in weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C, the 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, and specific catalytic cracking catalyst property is shown in Table 9, and catalytic cracking product distribution of products property is shown in Table 10.
Embodiment 3
In embodiment 3, raw material A, B, C are carried out into isolated light fraction and heavy distillat respectively, cut point is to be 600 DEG C.Raw material A, B, C heavy distillat are processed respectively through coking plant, then are 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.
The weighted BMO spaces reactor A is using the light fraction of raw material A and wax tailings, the weighted BMO spaces reactor B of A using the light fraction of raw material B and wax tailings, the weighted BMO spaces reactor C of B using the light fraction of raw material C and the wax tailings of C.The weighted BMO spaces reactor A, weighted BMO spaces reactor B, the inlet amount of weighted BMO spaces reactor C are identical, identical catalyst loading pattern is used in the weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C, catalyst loading pattern is shown in Table 3, the 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, and 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, the use raw material C properties are shown in Table 1 by isolated light fraction and heavy distillat, and cut point is 610 DEG C.Heavy distillat is processed 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.
30% catalytic cracking diesel oil and the heavy catalytic cycle oil of whole of wax tailings and light fraction and catalytic cracking unit are delivered into weighted BMO spaces reaction zone.Three weighted BMO spaces reactor catalyst fillings and inlet amount are identical with feed properties.The weighted BMO spaces reactor A average reaction temperature is 365 DEG C, weighted BMO spaces reactor B average reaction temperature is 375 DEG C, weighted BMO spaces reactor C average reaction temperatures are 385 DEG C, the average reaction temperature of hydrotreating reactor D is 383 DEG C, catalyst loading pattern is shown in Table 3, the 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, 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 1
4 reactors, respectively reactor A, reactor B, reactor C, reactor D are also adopted by comparative example 1, reactor A, reactor B, reactor C and reactor D are connected in the form of being sequentially connected in series.Raw materials used A properties are shown in Table 1 in comparative example 1, and the inlet amount and feed properties of reactor A are identical with the total feed and feed properties of embodiment 1.The catalyst inventory of the reactor A, reactor B, reactor C and reactor D is identical with the corresponding weighted BMO spaces reactor A of embodiment, weighted BMO spaces reactor B, weighted BMO spaces reactor C, hydrodesulphurisatioreactors reactors D, but the loadings of various species catalyst are different, loaded according to the mode in table 4.The catalytic cracking diesel oil that catalytic cracking unit is obtained directly goes out device, and heavy catalytic cycle oil is cracked 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
4 reactors, respectively reactor A, reactor B, reactor C, reactor D are also adopted by comparative example 2, reactor A, reactor B, reactor C and reactor D are connected in the form of being sequentially connected in series.Raw material B is used in comparative example 2, property is shown in Table 1, and the reactor A entrance inlet amount total with embodiment 2 and feed properties are identical.The catalyst inventory weighted BMO spaces reactor A corresponding with embodiment 2 of the reactor A, reactor B, reactor C and reactor D, weighted BMO spaces reactor B, weighted BMO spaces reactor C, hydrodesulphurisatioreactors reactors D are identical, but the loadings of various species catalyst are different, loaded according to the mode in table 4, 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.The catalytic cracking diesel oil that catalytic cracking unit is obtained directly goes out device, and heavy catalytic cycle oil is cracked in catalytic cracking unit inner loop.
Comparative example 3
4 reactors, respectively reactor A, reactor B, reactor C, reactor D are also adopted by comparative example 3, reactor A, reactor B, reactor C and reactor D are connected 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 materials, and reactor A, reactor B, reactor C and reactor D are in the form of series connection in comparative example, and the reactor A entrance inlet amount total with embodiment 3 and mixed feeding property are identical.The catalyst inventory of the reactor A, reactor B, reactor C and reactor D is identical with the corresponding weighted BMO spaces reactor A of embodiment, weighted BMO spaces reactor B, weighted BMO spaces reactor C, hydrodesulphurisatioreactors reactors D, but the loadings of various species catalyst are different, loaded according to the mode in table 4, 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.The catalytic cracking diesel oil that catalytic cracking unit is obtained directly goes out device, and heavy catalytic cycle oil is cracked in catalytic cracking unit inner loop.
Comparative example 4
4 reactors, respectively reactor A, reactor B, reactor C, reactor D are also adopted by comparative example 4, reactor A, reactor B, reactor C and reactor D are connected in the form of being sequentially connected in series.Comparative example 4 uses raw material C, and property is shown in Table 1, and reactor A, reactor B, reactor C and reactor D are in the form of series connection in comparative example, and the reactor A entrance inlet amount total with embodiment 4 and feed properties are identical.The catalyst inventory of the reactor A, reactor B, reactor C and reactor D is identical with the corresponding weighted BMO spaces reactor A of embodiment, weighted BMO spaces reactor B, weighted BMO spaces reactor C, hydrodesulphurisatioreactors reactors D, but the loadings of various species catalyst are different, loaded according to the mode in table 4, 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.
The catalytic cracking diesel oil that catalytic cracking unit is obtained directly goes out device, and heavy catalytic cycle oil is cracked in catalytic cracking unit inner loop.
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 (21)
1. a kind of method for processing residual oil, including coking plant, weighted BMO spaces reaction zone, hydrotreating reaction area and catalytic cracking reaction zone；Methods described includes herein below：
（1）Feedstock oil is fractionated into obtaining light fraction and heavy distillat, and cutting point range is 500-650 DEG C；
（2）Step（1）The heavy distillat for obtaining enters coking plant, and coker gasoline, coker gas oil, wax tailings and coke are obtained after treatment；
（3）Step（1）Light fraction, the step for obtaining（2）The wax tailings for obtaining sequentially pass through the weighted BMO spaces reaction zone and hydrotreating reaction area being arranged in series after mixing with hydrogen, the reaction effluent in hydrotreating reaction area carries out gas-liquid separation, isolated gas phase loops back weighted BMO spaces reaction zone and/or hydrotreating reaction area, isolated liquid phase is directly entered catalytic cracking reaction zone and carries out catalytic cracking reaction, catalytic cracking reaction effluent isolated dry gas, liquefied gas, catalytically cracked gasoline cut, catalytic cracking diesel oil cut, heavy catalytic cycle oil and catalytic cracked oil pulp in fractionating device；The weighted BMO spaces reaction zone includes the weighted BMO spaces reactor that two more parallels are set,When the pressure drop of First weighted BMO spaces reactor in the weighted BMO spaces reaction zone reaches the 50%~80% of the reactor design pressure drop upper limit,It is preferred that when 60%~70%,The weighted BMO spaces reactor is cut out from weighted BMO spaces reaction zone,And the weighted BMO spaces reactor is named as the weighted BMO spaces reactor I for cutting out,And sequentially pass through weighted BMO spaces reaction zone according to material,The weighted BMO spaces reactor I for cutting out,With weighted BMO spaces reaction zone and hydrotreating reaction area be connected in series to the weighted BMO spaces reactor for cutting out by the order in hydrotreating reaction area,The charging of the weighted BMO spaces reactor that now this cuts out is the reaction effluent of the weighted BMO spaces reactor in addition to the weighted BMO spaces for the cutting out reactor,When the pressure drop of next weighted BMO spaces reactor reaches the 50%~80% of the reactor design pressure drop upper limit,It is preferred that when 60%~70%,The weighted BMO spaces reactor is cut out from weighted BMO spaces reaction zone,And the weighted BMO spaces reactor for cutting out is named as the weighted BMO spaces reactor II for cutting out,And sequentially pass through weighted BMO spaces reaction zone according to material,The weighted BMO spaces reactor II for cutting out,The weighted BMO spaces reactor I for cutting out,With weighted BMO spaces reaction zone and the weighted BMO spaces reactor I for cutting out be connected in series to the weighted BMO spaces reactor II for cutting out by the order in hydrotreating reaction area,The charging of the weighted BMO spaces reactor II for now cutting out is the reaction effluent of remaining weighted BMO spaces reactor of the weighted BMO spaces reaction zone in addition to the weighted BMO spaces reactor for having cut out,In the manner described above,Until all of weighted BMO spaces reactor is all connected in series to.
2. in accordance with the method for claim 1, it is characterised in that：All weighted BMO spaces reactors in the weighted BMO spaces reaction zone reach the 50%~80% of the reactor pressure decrease design upper limit when different.
3. in accordance with the method for claim 2, it is characterised in that：To set caused with the difference of beds property by process conditions and reach reactor pressure decrease designs the upper limit 50%~80% when each weighted BMO spaces reactor of weighted BMO spaces reaction zone is different.
4. in accordance with the method for claim 3, it is characterised in that：By controlling catalyst packing heights different in each weighted BMO spaces reactor, different inlet amounies, different feed properties, different operating conditions, reaches the 50%~80% of the reactor pressure decrease design upper limit when realizing that each weighted BMO spaces reactor is different using one or more in different Catalyst packing density under the conditions of identical filling height.
5. in accordance with the method for claim 4, it is characterised in that：When the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel uses different Catalyst packing density, in the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel, maximum loading density is 400kg/m3~600kg/m3, preferably 450kg/m3~550kg/m3, minimum loading density is 300kg/m3~550kg/m3, preferably 350kg/m3~450kg/m3。
6. in accordance with the method for claim 5, it is characterised in that：The Catalyst packing density difference of the immediate two weighted BMO spaces reactors of loading density is 50~200kg/m3, preferably 80~150kg/m3。
7. in accordance with the method for claim 4, it is characterised in that：When the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel uses different inlet amounies, the ratio between feed volume air speed of the immediate two weighted BMO spaces reactors of inlet amount is 1.1 ~ 3.0, preferably 1.1 ~ 1.5.
8. in accordance with the method for claim 4, it is characterised in that：When the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel uses different feed properties, the tenor difference of the immediate two weighted BMO spaces reactors of feed properties is 5 ~ 50 μ g/g, preferably 10 ~ 30 μ g/g.
9. in accordance with the method for claim 4, it is characterised in that：When the weighted BMO spaces reaction zone each weighted BMO spaces reactor in parallel uses different operating conditions, in the operating condition of control operation pressure and the immediate two weighted BMO spaces reactors of volume space velocity, operation temperature difference is 2 ~ 30 DEG C, preferably 5 ~ 20 DEG C.
10. in accordance with the method for claim 1, it is characterised in that：One or more in catalytically cracked gasoline cut, catalytic cracking diesel oil cut, heavy catalytic cycle oil that the catalytic cracking reaction zone obtains loop back weighted BMO spaces reaction zone.
11. in accordance with the method for claim 1, it is characterised in that：The catalytic cracked oil pulp that the catalytic cracking reaction zone obtains loops back coking plant and is processed.
12. in accordance with the method for claim 10, it is characterised in that：Loop back one or several that the catalytically cracked gasoline cut of weighted BMO spaces reaction zone, catalytic cracking diesel oil cut, heavy catalytic cycle oil enter in the weighted BMO spaces reactor being arranged in parallel.
13. in accordance with the method for claim 1, it is characterised in that：The weighted BMO spaces reaction zone includes the weighted BMO spaces reactor that two more parallels are set, and 3~6 weighted BMO spaces reactors being arranged in parallel is preferably included, more preferably including the 3 or 4 weighted BMO spaces reactors being arranged in parallel.
14. in accordance with the method for claim 1, it is characterised in that：Described hydrotreating reaction area includes 1~5 hydrotreating reactor being arranged in series, and preferably includes 1~2 hydrotreating reactor being arranged in series.
15. in accordance with the method for claim 1, it is characterised in that：The operating condition of the weighted BMO spaces reaction zone is：Reaction temperature is 370 DEG C~420 DEG C, and reaction pressure is 10MPa~25MPa, and hydrogen to oil volume ratio is 300~1500, and volume space velocity is 0.15h during raw material fluid-1~2.00h-1。
16. in accordance with the method for claim 13, 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 is 15MPa~20MPa, and hydrogen to oil volume ratio is 500~800, and volume space velocity is 0.3h during raw material fluid-1~1.00h-1。
17. 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 is 10MPa~25MPa, and hydrogen to oil volume ratio is 300~1500, and volume space velocity is 0.15h during raw material fluid-1~0.80h-1。
18. in accordance with the method for claim 17, it is characterised in that：The operating condition in the hydrotreating reaction area is that reaction temperature is 380 DEG C~410 DEG C, and reaction pressure is 15MPa~20MPa, and hydrogen to oil volume ratio is 400~800, and volume space velocity is 0.2h during raw material fluid-1~0.60h-1。
19. in accordance with the method for claim 1, it is characterised in that：Described feed residue is reduced crude or decompression residuum, or contains straight-run gas oil, decompressed wax oil, one or more in secondary operation wax oil and FCC recycle oil.
20. 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, preferably 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.
21. in accordance with the method for claim 1, it is characterised in that：The coker operations condition is：Pressure is 1~3MPa, preferably 1~2MPa；Temperature is 450~550 DEG C, preferably 480~520 DEG C.
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