CN106701189B - A kind of hydrogenation and catalystic cracking combined process for residual oil - Google Patents
A kind of hydrogenation and catalystic cracking combined process for residual oil Download PDFInfo
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- CN106701189B CN106701189B CN201510769346.2A CN201510769346A CN106701189B CN 106701189 B CN106701189 B CN 106701189B CN 201510769346 A CN201510769346 A CN 201510769346A CN 106701189 B CN106701189 B CN 106701189B
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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
Abstract
The invention discloses a kind of hydrogenation and catalystic cracking combined process for residual oil, including weighted BMO spaces reaction zone, hydrotreating reaction area and catalytic cracking reaction zone；The process includes the following contents：Residual oil raw material and at least partly catalytic cracking diesel oil fraction pass through the weighted BMO spaces reaction zone being arranged in series and hydrotreating reaction area successively after being mixed with 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 fraction, catalytic cracking diesel oil fraction, heavy catalytic cycle oil and catalytic cracked oil pulp, wherein, some or all of catalytic cracking diesel oil is recycled back to weighted BMO spaces reaction zone and carries out hydrotreating reaction.The method of the present invention can extend the cycle of operation of device.
Description
Technical field
The present invention relates to a kind of heavy oil lightening methods, add hydrogen-catalyzed combination process more particularly to a kind of use
The method of heavy oil.
Background technology
Currently, it will be in hold that demand of the refined products market to oil products such as steam coal bavins, which is especially the demand to motor petrol, both at home and abroad
The continuous trend risen, and the demand to heavy oil products such as heavy fuel oils is then on a declining curve.Meanwhile crude oil in the world
Matter is deteriorated increasingly, and environmental regulation is increasingly stringent, and increasingly strict requirement is proposed to oil quality.Therefore, how relatively to pass through
Rational cost of helping realizes that heavy oil lighting and petrol and diesel oil product quality persistently upgrade and has become oil refining industry concern both at home and abroad
Focus.
The main purpose of residual hydrocracking technique is to keep sulphur, nitrogen, metal in residual oil raw material etc. miscellaneous by hydrotreating
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 high temperature and pressure, desulfurization is carried out to normal pressure or decompression residuum, is taken off
Nitrogen, demetalization etc. are one of the important means of residual oil weight-lightenings to obtain light-end products to the maximum extent.Fixed bed residual oil adds
Hydrogen technology is with its liquid product yield height, and good product quality, production chains are strong, and waste, waste material are few, environmental-friendly, invest back
The advantages that report rate is high, has been more and more widely used.
The setting of fixed bed residual hydrocracking process reaction partial reaction device is generally connected by multiple reactors or bed
It uses, requires to optimize the dosage form of catalyst according to the property of original oil, reaction condition and purpose product, according to different physical
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 it is susceptible to the phenomenon that reactor pressure drop increases.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-
Device is answered to react load due to assuming responsibility for 70% or more demetalization, metal sulfide is deposited on catalyst bed, to after in operation
Inevitably there is pressure drop rapid growth in phase, and subsequent reactor is since demetalization load is obviously relatively low, pressure drop increase compared with
Slowly.This affects the cycle of operation and the device of device there have been front 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, which includes primary concatenated plus hydrogen insured unit and main hydrotreating unit.Described adds
Hydrogen protection location includes main hydrogenation protecting reactor in parallel and spare hydrogenation protecting reactor, and main hydrogenation protecting reactor
Volume is more than stand-by protection reactor.In hydroprocessing processes, main hydrogenation protecting reactor and spare hydrogenation protecting reactor
It is used alternatingly.Main hydrogenation protecting reactor and spare hydrogenation protecting reactor handover operation can be processed height by the process
The residual oil of calcium high metal content, the disadvantage is that the reactor that left unused, increasing investment reduces reactor utilization rate, and cannot
Lead reactor pressure drop growing concern is solved 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 add one or more feed inlets, change simultaneously original catalyst grade and match, when an anticatalyst bed
When pressure drop designs 0.4~0.8 times of pressure drop for device, next feed inlet is used instead successively, while original feed inlet can be into cycle
The miscella of oil or recycle oil and original oil can be effectively prevented bed pressure drop with the technique and extend the operation cycle of device,
And the processing capacity of device can be increased, help to improve flow distribution.The disadvantage is that inductor manufacturing cost increases, make 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 concatenated more reactors, when device operation 700~4000 is small after carry out shunting behaviour
Make, reduce an anti-inlet amount or keep an anti-inlet amount constant, increase that one is anti-and the last one 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 cannot 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.
Invention content
In view of the deficiencies of the prior art, the present invention provides a kind of hydrogenation and catalystic cracking combined process for residual oil.
This method technological process is simple, it is only necessary to carry out simple modifications to existing apparatus, so that it may substantially to extend the operating of whole device
Period, and the utilization ratio of catalyst can be made to realize and maximized.
Existing residual hydrocracking technology, all reactors use concatenated technological process, it is therefore desirable to anti-in First
Device is answered to load a large amount of protective agent to deposit the impurity and dirt in raw material, operation in this way can cause in First protection reactor
For the antigravity system of filling since activity is relatively low, demetalization load is relatively low, has arrived device end-of-run reactor in some cases
Pressure drop is still very low so that the ability that is de-, holding metallic compound of monolithic catalyst reduces.If improving its catalyst activity again
The rapid growth of pressure drop can be caused, the cycle of operation is shortened, and subsequent catalyst performance plays completely not yet, keeps First
Protect reactor catalyst it is appropriate activity be difficult control, and during residual hydrogenation equipment whole service there are 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 an anti-protection lower reaction of reactor catalyst, main function intercept and the impurity in deposition raw material and
Dirt only carries out lower demetalization reaction, and typically the reactor reaction temperature rises relatively low, and pressure drop is tieed up in the whole service period
It holds in lower level, this requires that being substantially carried out in a large amount of catalyst for demetalation of subsequent demetalization reactor filling de-
Metal reaction and for accommodate hydrogenation and removing metallic compound and carbon distribution enough spaces are provided, inevitably cause in this way
A large amount of metal is deposited in the demetalization reactor, demetalization reaction load is larger, and typically the reactor reaction temperature rises 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, becomes the principal element for restricting the cycle of operation.
A kind of hydrogenation and catalystic cracking combined process for residual oil of present invention offer, including weighted BMO spaces reaction zone,
Hydrotreating reaction area and catalytic cracking reaction zone；The process includes the following contents：It residual oil raw material and at least partly urges
Change after cracked diesel oil fraction is mixed with hydrogen and pass through the weighted BMO spaces reaction zone being arranged in series and hydrotreating reaction area successively,
The reaction effluent in hydrotreating reaction area carries out gas-liquid separation, and isolated gas phase is recycled back to weighted BMO spaces reaction zone
And/or hydrotreating reaction area, isolated liquid phase are directly entered catalytic cracking reaction zone and carry out catalytic cracking reaction, catalysis
The isolated dry gas of cracking reaction effluent, liquefied gas, catalytically cracked gasoline fraction, catalytic cracking diesel oil fraction, catalytic cracking
Heavy-cycle oil and catalytic cracked oil pulp, wherein some or all of catalytic cracking diesel oil be recycled back to weighted BMO spaces reaction zone into
Row hydrogenation reaction；The weighted BMO spaces reaction zone includes the weighted BMO spaces reactor of two more parallels setting, when described
In weighted BMO spaces reaction zone the pressure drop of any weighted BMO spaces reactor reach the reactor design pressure drop upper limit 50%~
80%, when preferably 60%~70%, which is cut out from weighted BMO spaces reaction zone, and add hydrogen pre- this
Treatment reactor is named as the weighted BMO spaces reactor I cut out, and passes through weighted BMO spaces reaction zone successively according to material, cuts
The sequence of the weighted BMO spaces reactor I, hydrotreating reaction area that go out by the weighted BMO spaces reactor cut out with plus hydrogen it is pre-
Processing reaction zone and hydrotreating reaction area are connected in series to, at this time the weighted BMO spaces reactor cut out
Charging is the reaction effluent of the weighted BMO spaces reactor in addition to the weighted BMO spaces cut out the reactor, is added when next
The pressure drop of hydrogen pretreatment reactor reaches the 50%~80% of the reactor design pressure drop upper limit, when preferably 60%~70%, by this plus hydrogen
Preatreating reactors is cut out from weighted BMO spaces reaction zone, and the weighted BMO spaces reactor that this cuts out is named as and is cut out
Weighted BMO spaces reactor II, and according to material successively by weighted BMO spaces reaction zone, the weighted BMO spaces reactor cut out
II, the weighted BMO spaces reactor I cut out, hydrotreating reaction area sequence by the weighted BMO spaces reactor II cut out with
Weighted BMO spaces reaction zone and the weighted BMO spaces reactor I cut out are connected in series to, and cut out at this time plus hydrogen is located in advance
The charging for managing reactor II is that remaining of weighted BMO spaces reaction zone in addition to the weighted BMO spaces reactor cut out adds hydrogen pre-
The reaction effluent for the treatment of reactor, in the manner described above, until all weighted BMO spaces reactors are all with concatenated
Mode connects.
In hydrogenation and catalystic cracking combined process for residual oil of the present invention, the institute in the weighted BMO spaces reaction zone
Reach the 50%~80% of the reactor pressure decrease design upper limit when having weighted BMO spaces reactor difference, can be arranged by process conditions
Reach pressure drop when so that each weighted BMO spaces reactor of weighted BMO spaces reaction zone is different with the difference of catalyst bed property
Design the 50%~80% of the upper limit.It specifically can be high by controlling Catalyst packing different in each weighted BMO spaces reactor
It spends, different inlet amounies, different feed properties, different operating conditions, may be used not under the conditions of identical filling height
One or more of means such as same Catalyst packing density reach pressure to realize when each weighted BMO spaces reactor difference
The 50%~80% of the drop design upper limit.
As described above, each weighted BMO spaces reactor when weighted BMO spaces reaction zone parallel connection is urged using different
When agent loading density, in each weighted BMO spaces reactor of the weighted BMO spaces reaction zone parallel connection, 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.First by the catalyst for the weighted BMO spaces reactor being cut out
Loading density is maximum, and the Catalyst packing density for the weighted BMO spaces reactor being finally cut out is minimum.The different fillings are close
Degree 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 realizes that the Catalyst packing density in each weighted BMO spaces reactor is different in different proportions.
As described above, when the weighted BMO spaces reaction zone parallel connection each weighted BMO spaces reactor use it is different into
When doses, 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 parallel connection each weighted BMO spaces reactor use it is different into
When expecting property, the tenor difference of the immediate two weighted BMO spaces reactors of feed properties is 5 ~ 50 μ g/g, preferably
10~30µg/g。
As described above, each weighted BMO spaces reactor when weighted BMO spaces reaction zone parallel connection uses different behaviour
When making condition, it can control in operating pressure and the operating condition of the immediate two weighted BMO spaces reactors of volume space velocity,
Operation temperature difference is 2 ~ 30 DEG C, preferably 5 ~ 20 DEG C.
In hydrogenation and catalystic cracking combined process for residual oil of the present invention, into the catalysis of weighted BMO spaces reaction zone
Cracked diesel oil fraction can be that catalytic cracking reaction zone obtains in hydrogenation and catalystic cracking combined process for residual oil of the present invention
Catalytic cracking diesel oil fraction, can also include the obtained catalytic cracking diesel oil fraction of other catalytic cracking units.Slag of the present invention
The catalytic cracking diesel oil fraction that catalytic cracking reaction zone obtains in oily hydrogenation and catalystic cracking combined process can be whole
Or part enters weighted BMO spaces reaction zone, the catalytic cracking diesel oil fraction into weighted BMO spaces reaction zone is generally at least accounted for and is urged
30% or more of the diesel oil distillate weight that change cracking reaction area obtains, preferably 50% or more.
In hydrogenation and catalystic cracking combined process for residual oil of the present invention, it is recycled back to urging for weighted BMO spaces reaction zone
Change one or several that cracked diesel oil fraction can enter in the weighted BMO spaces reactor being arranged in parallel, preferably presses suitable ratio
Example respectively enters different weighted BMO spaces reactors.
In hydrogenation and catalystic cracking combined process for residual oil of the present invention, the weighted BMO spaces reaction zone includes two
The weighted BMO spaces reactor of platform more parallel setting, preferably includes 3~6 weighted BMO spaces reactors being arranged in parallel, more
Preferably include the 3 or 4 weighted BMO spaces reactors being arranged in parallel.The hydrotreating reaction area includes 1~5 series connection
The hydrotreating reactor of setting preferably includes 1~2 hydrotreating reactor being arranged in series.
In hydrogenation and catalystic cracking combined process for residual oil of the present invention, the operation of the weighted BMO spaces reaction zone
Condition is：Reaction temperature is 370 DEG C~420 DEG C, and preferably 380 DEG C~400 DEG C, reaction pressure is 10MPa~25MPa, preferably
For 15MPa~20MPa；Hydrogen to oil volume ratio is 300~1500, preferably 500~800；Volume space velocity is when raw material fluid
0.15h-1~2.00h-1, preferably 0.3h-1~1.00h-1.The average reaction temperature of weighted BMO spaces reaction zone is apparently higher than existing
There are the reaction temperature of the residuum hydrogenating and metal-eliminating reactor of technology, the residuum hydrogenating and metal-eliminating reaction temperature of the prior art to be usually
350 DEG C~390 DEG C.The weighted BMO spaces reaction zone of this method middle front part setting eliminates pressure drop by the optimization of technological process
The unfavorable factor for increasing restrictive cycle, can operate, what in addition relatively high reaction temperature was conducive to be loaded urges at high temperature
The performance of agent system performance is conducive to the removing of the hydro-conversion and impurity of macromolecular.
In hydrogenation and catalystic cracking combined process for residual oil of the present invention, the operation item in the hydrotreating reaction area
Part 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 when raw material fluid-1
~0.80h-1, preferably 0.2h-1~0.60h-1。
In hydrogenation and catalystic cracking combined process for residual oil of the present invention, this field routine may be used in catalytic cracking
Technology.Catalytic cracking unit can be more than a set of or a set of often cover catalytic cracking unit at least and should include a reactor and
Fractionating column need to be arranged in one regenerator, catalytic cracking unit, fractionating column can be respectively set with every set catalytic cracking unit, can also
Share fractionating column.The fractionation of catalytic cracking reaction effluent is dry gas, liquefied gas, catalytically cracked gasoline fraction, catalysis by fractionating column
Cracked diesel oil fraction, catalytic cracking recycle oil and catalytic cracked oil pulp etc..Catalytic cracking fractionating tower can routinely knowledge design.
In hydrogenation and catalystic cracking combined process for residual oil of the present invention, the operation item of the catalytic cracking reaction zone
Part 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 is than 2~30, and 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 catalytic cracking catalyst includes the catalyst commonly used in catalytic cracking, as sial is urged
Agent, silica-magneia cataslyst, the carclazyte of acid processing and X-type, Y types, ZSM-5, M type, layer column equimolecular sieve Cracking catalyst, best
It is molecular sieve cracking catalyst, this is because the activity of molecular sieve cracking catalyst is high, green coke is few, and gasoline yield is high, conversion ratio
It is high.The reactor of the catalytic cracking unit can be the catalyst cracker of various types, preferably promote tube reaction
Device or riser add bed reactor.Technological process is generally：Feedstock oil is injected from riser reactor bottom, and from regeneration
The high-temperature regenerated catalyst of device contacts, and the catalyst mixture of oil gas and deposit coke that cracking reaction generates is along promotion tube reaction
Device moves up, and completes the catalytic cracking reaction of entire feedstock oil.
In hydrogenation and catalystic cracking combined process for residual oil of the present invention, residual hydrogenation technology uses fixed bed residual oil
Hydrotreating techniques, can load in each weighted BMO spaces reactor of the weighted BMO spaces reaction zone hydrogenation protecting agent,
One or more of Hydrodemetalation catalyst, Hydrobon catalyst, hydrodenitrogeneration carbon residue reforming catalyst, described plus hydrogen
One or more of Hydrobon catalyst and hydrodenitrogeneration carbon residue reforming catalyst can be loaded in processing reaction zone, it is described
Hydrogenation protecting agent, Hydrodemetalation catalyst, Hydrobon catalyst, hydrodenitrogeneration carbon residue reforming catalyst are fixed bed slag
Catalyst used in oily hydroprocessing processes.It is to carry that above-mentioned catalyst, which is typically all with porous refractory inorganic oxide such as aluminium oxide,
The oxide of body, group VIB and/or group VIII metal such as W, Mo, Co, Ni etc. are active component, are selectively added other each
The catalyst of the elements such as kind auxiliary agent such as P, Si, F, B, such as produced by Sinopec Group's catalyst branch
FZC series catalyst for hydrotreatment of residual oil.
In hydrogenation and catalystic cracking combined process for residual oil of the present invention, the feed residue can be normal pressure slag
Oil can also be decompression residuum, usually also contain straight-run gas oil, decompressed wax oil, and one in secondary operation wax oil and FCC recycle oil
Kind is several.The residual oil raw material property is：Sulfur content is not more than 4wt%, and nitrogen content is not more than 0.7wt%, tenor (Ni
+ V) it is not more than 120 μ g/g, carbon residue is not more than 17wt%, and asphalt content is not more than 5wt%.
Compared with prior art, hydrogenation and catalystic cracking combined process for residual oil of the present invention has the following advantages：
1, in the method for the present invention, the weighted BMO spaces reaction zone includes more weighted BMO spaces reactors of parallel connection,
So that entire catalyst system takes off/holds metal ability and is increased dramatically.
2, the method for the present invention 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
It stops work to device, and then the pressure drop of some weighted BMO spaces reactor is made not restrict cycle of operation of whole device.
3, the method for the present invention is by optimizing and revising weighted BMO spaces reaction zone catalyst performance and technological parameter, and rear
Continuous high activity desulfurization takes off the cooperation of carbon residue catalyst so that de- while the de-/appearance metal ability for improving monolithic catalyst
Sulphur takes off carbon residue performance and is guaranteed.
4, the method for the present invention is by cutting each weighted BMO spaces reactor of weighted BMO spaces reaction zone from series connection is parallel to
The adjustment for changing mode of operation solves the problems, such as reactor pressure decrease rapid growth, while increasing the operating flexibility and original of device
Expect adaptability；
5, the appearance gold of catalyst system is significantly increased by the way that weighted BMO spaces reactor parallel form is arranged for the method for the present invention
Category amount so that the stability of system enhances so that the growth of device pressure drop can be controlled, and the device cycle of operation is extended.
6, the method for the present invention can utmostly realize that all kinds of catalyst synchronize inactivation, to improve the operation effect of device
Rate is increased economic efficiency.
7, in the method for the present invention, in each weighted BMO spaces reactor of the weighted BMO spaces reaction zone parallel connection, according to
Hydrogenation protecting agent and Hydrodemetalation catalyst are loaded in weighted BMO spaces reactor in Flow of Goods and Materials direction successively, can also be
Selectivity filling Hydrobon catalyst below Hydrodemetalation catalyst.Such catalyst loading pattern so that entire body
System takes off/holds metal ability and is increased dramatically, while making the pressure of each preatreating reactors by the adjustment that catalyst grade is matched
Drop increases in control range.The catalyst system of each weighted BMO spaces reactor filling of weighted BMO spaces reaction zone parallel connection
Based on de-/appearance metal function so that while demetalization performance boost, strengthen to such as gum asphalt of macromolecular in raw material
The ability of hydro-conversion lays the foundation for successive depths desulfurization and the conversion of carbon residue so that hydrodesulfurizationreaction reaction zone be conducive 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 without reducing instead.
8, in the method for the present invention, catalytic cracking diesel oil fraction can reduce the viscosity of residual oil raw material, improve raw material in reaction system
Flow distribution in system and mass transfer reduce the influence being diffused in during residual hydrocracking, improve the poisonous metals such as nickel, vanadium
Deposition distribution in catalytic reaction system extends the service life of catalyst；Meanwhile the reduction of viscosity makes mixed raw material oil
Conveying and filtering are more prone to.Catalytic cracking diesel oil fraction imurity-removal, aromatic hydrocarbons can be saturated during Residue Hydrotreating Technology, at
It is formed for better catalytically cracked material, further improves catalytic cracking high value added product yield.
9, it in group technology of the present invention, is not required to set fractionating system in hydrotreating reaction area, hydrotreating generates oil directly
Into catalyst cracker, it is not required to set feed pump, while reducing a large amount of heat transmission equipments.Equipment investment is set to have prodigious drop
It is low.
Description of the drawings
Fig. 1 is hydrogenation and catalystic cracking combined process for residual oil flow chart of the present invention.
Specific implementation mode
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, hydrogenation and catalystic cracking combined process for residual oil of the present invention includes the following contents：Residual oil is former
Material enters the weighted BMO spaces being arranged in series with the mixed material G of hydrogen through feeding line 1, feeding line 2 and feeding line 3
Reaction zone and hydrotreating reaction area, the weighted BMO spaces reaction zone include three weighted BMO spaces being arranged in parallel reactions
Device, 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, weighted BMO spaces reactor C feed inlet respectively with feeding line 1, feeding line 2
It is connected with feeding line 3, three tunnels of outlet point of the weighted BMO spaces reactor A, the first via is anti-through pipeline 6 and weighted BMO spaces
The feed inlet of device B is answered to connect, the second tunnel is connect through pipeline 7 with the feed inlet of weighted BMO spaces reactor C, and third road is through pipeline 10
It is connect with hydrotreating reactor D；The outlet of the weighted BMO spaces reactor B point three tunnels, the first via through pipeline 4 with add hydrogen pre-
The feed inlet for the treatment of reactor A connects, and the second tunnel obtains feed inlet with weighted BMO spaces reactor C through pipeline 5 and connect, third road warp
Pipeline 11 is connect with hydrotreating reactor D；The outlet of the weighted BMO spaces reactor C point three tunnels, the first via through pipeline 8 with
The feed inlet of weighted BMO spaces reactor A connects, and the second tunnel is connect through pipeline 9 with the feed inlet of weighted BMO spaces reactor B, the
Three tunnels are connect through pipeline 12 with hydrotreating reactor D；It is provided with valve 101 on the pipeline 1, is provided on the pipeline 2
Valve 102 is provided with valve 103 on the pipeline 3, valve 104 is provided on the pipeline 4, valve is provided on the pipeline 5
Door 105 is provided with valve 106 on the pipeline 6, valve 107 is provided on the pipeline 7, valve is provided on the pipeline 8
108, valve 109 is provided on the pipeline 9, and valve 1010 is provided on the pipeline 10, valve is provided on the pipeline 11
Door 1011 is provided with valve 1012 on the pipeline 12, and the generation oil 13 that the hydrotreating reactor obtains enters separator E
Liquefied gas 20 and hydrogenated oil 14 are obtained after separation, the hydrogenated oil 14 enters catalytic cracking reaction zone F, with height
Warm regeneration catalyzing Cracking catalyst contacts and carries out catalytic cracking reaction, and product is fractionated into obtain gas 15, is catalyzed and splits after reaction
Change gasoline fraction 16, catalytic cracking diesel oil fraction 17, catalytic cracking recycle oil 18 and catalytic cracked oil pulp 19, gas 15 and catalysis
16 discharger of cracked naphtha, catalytic cracking diesel oil fraction 17 return to weighted BMO spaces reaction zone, are mixed with residual oil raw material
It is reacted into weighted BMO spaces reaction zone, catalytic cracking recycle oil 18 is recycled back to catalytic cracking unit circular response, catalysis
19 discharger of cracking slurry oil utilizes after carrying out suitable treatment.
In hydrogenation and catalystic cracking combined process for residual oil of the present invention, the weighted BMO spaces reactor A,
Weighted BMO spaces reactor B, weighted BMO spaces reactor C can be inactivated in any order, include following 6 kinds of processes altogether
1, it is inactivated according to the sequence of weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C
（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 open the valve 104 on the valve 108 and pipeline 4 on pipeline 8, complete at this time
At once by being parallel to concatenated handover operation；
（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, at this time complete the 2nd time by being parallel to concatenated handover operation；
（4）When the pressure drop of weighted BMO spaces reactor C reaches critical value, entire reaction system needs shutdown process.
2, it is inactivated according to the sequence of weighted BMO spaces reactor A, weighted BMO spaces reactor C, weighted BMO spaces reactor B
（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 open the valve 104 on the valve 108 and pipeline 4 on pipeline 8, complete at this time
At once by being parallel to concatenated handover operation；
（3）When the pressure drop of weighted BMO spaces reactor C reaches critical value, valve 103, the pipeline 4 of feeding line 3 are closed
Valve 104, open pipeline 5 on valve 105, at this time complete the 2nd time by being parallel to concatenated handover operation；
（4）When the pressure drop of weighted BMO spaces reactor C reaches critical value, entire reaction system needs shutdown process.
3, it is inactivated according to the sequence of weighted BMO spaces reactor B, weighted BMO spaces reactor C, weighted BMO spaces reactor A
（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 B reaches critical value, valve 102, the pipeline of feeding line 2 are closed
10 valve 1010 and the valve 1012 of pipeline 12 open the valve 106 on the valve 109 and pipeline 6 on pipeline 9, complete at this time
At once by being parallel to concatenated handover operation；
（3）When the pressure drop of weighted BMO spaces reactor C reaches critical value, valve 103, the pipeline 6 of feeding line 3 are closed
Valve 106, open pipeline 7 on valve 107, at this time complete the 2nd time by being parallel to concatenated handover operation；
（4）When the pressure drop of weighted BMO spaces reactor A reaches critical value, entire reaction system needs shutdown process.
4, it is inactivated according to the sequence of weighted BMO spaces reactor B, weighted BMO spaces reactor A, weighted BMO spaces reactor C
（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 B reaches critical value, valve 102, the pipeline of feeding line 2 are closed
10 valve 1010 and the valve 1012 of pipeline 12 open the valve 106 on the valve 109 and pipeline 6 on pipeline 9, complete at this time
At once by being parallel to concatenated handover operation；
（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, at this time complete the 2nd time by being parallel to concatenated handover operation；
（4）When the pressure drop of weighted BMO spaces reactor C reaches critical value, entire reaction system needs shutdown process.
5, it is inactivated according to the sequence of weighted BMO spaces reactor C, weighted BMO spaces reactor B, weighted BMO spaces reactor A
（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 C reaches critical value, valve 103, the pipeline of feeding line 3 are closed
10 valve 1010 and the valve 1011 of pipeline 11 open the valve 105 on the valve 107 and pipeline 5 on pipeline 7, complete at this time
At once by being parallel to concatenated handover operation；
（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, at this time complete the 2nd time by being parallel to concatenated handover operation；
（4）When the pressure drop of weighted BMO spaces reactor A reaches critical value, entire reaction system needs shutdown process.
6, it is inactivated according to the sequence of weighted BMO spaces reactor C, weighted BMO spaces reactor A, weighted BMO spaces reactor B
（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 C reaches critical value, valve 103, the pipeline of feeding line 3 are closed
10 valve 1010 and the valve 1011 of pipeline 11 open the valve 105 on the valve 107 and pipeline 5 on pipeline 7, complete at this time
At once by being parallel to concatenated handover operation；
（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, at this time complete the 2nd time by being parallel to concatenated handover operation；
（4）When the pressure drop of weighted BMO spaces reactor B reaches critical value, entire reaction system needs shutdown process.
The effect for illustrating 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 Examples 1 to 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 Examples 1 to 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 Examples 1 to 4 and comparative example 1~4 is shown in Table 7.
Using conventional tandem process in the comparative example 1-4, other are corresponding identical as Examples 1 to 4 respectively.In the embodiment of the present invention
The weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C are pattern, and size is identical
Reactor, reactor A, reactor B, reactor C in the comparative example are pattern, the identical reactor of size.
Embodiment 1
Weighted BMO spaces reactor A, weighted BMO spaces reactor B described in embodiment 1, weighted BMO spaces reactor C residual oil
Charging is all shown in Table 1 using raw material A property, and the catalytic cracking diesel oil of catalytic cracking unit whole is all recycled to weighted BMO spaces
Reaction zone, property are shown in Table 2.Wherein distribute to weighted BMO spaces reactor A catalytic cracking diesel oil ratio be 10%, distribute to plus
The catalytic cracking diesel oil ratio of hydrogen pretreatment reactor B is 30%, distributes to the catalytic cracking diesel oil of weighted BMO spaces reactor C
Ratio is 60%.The weighted BMO spaces reactor A, weighted BMO spaces reactor B, the catalyst of weighted BMO spaces reactor C are total
Loading amount, feed properties are identical with inlet amount, and the weighted BMO spaces reactor A, weighted BMO spaces reactor B plus hydrogen are pre-
Treatment reactor C, hydrotreating reactor D catalyst loaded in the way of in table 3, 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 2
In embodiment 2, in the weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C
Residual oil raw material B is all used, the catalytic cracking diesel oil of catalytic cracking unit whole is all recycled to weighted BMO spaces reaction zone,
Middle weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C are distributed and are obtained urging for same ratio
Change cracked diesel oil.Each anti-Feed space velocities are different, and volume space velocity is 0.20h when the weighted BMO spaces reactor A liquid-1, add hydrogen pre-
Volume space velocity is 0.32h when treatment reactor B liquid-1, volume space velocity is 0.44h when weighted BMO spaces reactor C liquid-1.Add hydrogen pre-
Identical catalyst loading pattern is used in treatment reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C, is urged
Agent type of feed is 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.Catalysis is split
Change operating 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 3
It is former using being used in raw material A, weighted BMO spaces reactor B in the weighted BMO spaces reactor A in embodiment 3
Expect that raw material C, residual oil raw material property used is used to be shown in Table 1 in B, weighted BMO spaces reactor C, by urging for catalytic cracking unit whole
Change cracked diesel oil and be all recycled to weighted BMO spaces reaction zone, wherein weighted BMO spaces reactor A, weighted BMO spaces reactor B,
Weighted BMO spaces reactor C, which is distributed, obtains the catalytic cracking diesel oil of same ratio.The weighted BMO spaces reactor A plus hydrogen
Preatreating reactors B, the inlet amount of weighted BMO spaces reactor C are identical, the weighted BMO spaces reactor A, weighted BMO spaces
Identical catalyst loading pattern, catalyst loading pattern is used to be shown in Table 3 in reactor B, weighted BMO spaces reactor C, it is 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 4
In embodiment 4, in the weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C
Using raw material C as charging, the catalytic cracking diesel oil of catalytic cracking unit whole is all recycled to weighted BMO spaces reaction zone,
Wherein weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C are distributed and are obtained same ratio
Catalytic cracking diesel oil.Three weighted BMO spaces reactor feed amounts are identical.The weighted BMO spaces reactor A average response
Temperature is 365 DEG C, weighted BMO spaces reactor B average reaction temperature is 375 DEG C, weighted BMO spaces reactor C average response temperature
Degree is 385 DEG C, the average reaction temperature of hydrotreating reactor D is 383 DEG C, and catalyst loading pattern is shown in Table 3, and the residual oil adds
Hydrogen 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, 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
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 of embodiment 1 and feed properties.It is the reactor A, anti-
Answer the catalyst inventory of device B, reactor C and reactor D 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 is loaded in the way of in table 4.The catalytic cracking diesel oil that catalytic cracking unit obtains directly goes out device.The residual oil adds
Hydrogen 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
Matter 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, property is used to be shown in Table in comparative example 2
1, reactor A entrance is identical with inlet amount and feed properties that embodiment 2 is total.The reactor A, reactor B, reactor
The catalyst inventory weighted BMO spaces reactor A corresponding with embodiment 2 of C and reactor D, adds weighted BMO spaces reactor B
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.
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 raw material, reactor A, reactor B, reactor C and reactor D use concatenated form, reactor A in comparative example
Entrance is identical as the inlet amount that embodiment 3 is total and mixed feeding property.The reactor A, reactor B, reactor C and reactor
The catalyst inventory weighted BMO spaces reactor A corresponding with embodiment of D, 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
It fills 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 to be catalyzed
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.
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, property to be shown in Table 1,
Reactor A, reactor B, reactor C and reactor D use concatenated form, reactor A entrance total with embodiment 4 in comparative example
Inlet amount it is identical with feed properties.The catalyst inventory and reality of the reactor A, reactor B, reactor C and reactor D
It applies example and corresponds 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.
1 residual oil raw material property of table
2 catalytic cracking diesel oil property of table
Catalyst loading pattern in 3 Examples 1 to 4 of table
Catalyst loading pattern in 4 comparative example 1~4 of table
The residual hydrogenation reaction condition of 5 Examples 1 to 4 of table
The residual hydrogenation reaction condition of 6 comparative example 1~4 of table
7 steady running period of table and residual hydrogenation generate oil nature
8 catalytic cracking process condition of table
9 catalytic cracking catalyst physico-chemical property of table
10 catalytic cracking product distribution results of table and catalytically cracked gasoline property
Claims (28)
1. a kind of hydrogenation and catalystic cracking combined process for residual oil, including weighted BMO spaces reaction zone, hydrotreating reaction
Area and catalytic cracking reaction zone；The process includes the following contents：Residual oil raw material and at least partly catalytic cracking diesel oil evaporates
Weighted BMO spaces reaction zone Jing Guo being arranged in series and hydrotreating reaction area successively after point being mixed with hydrogen, hydrotreating reaction
The reaction effluent in area carries out gas-liquid separation, and isolated gas phase is recycled back to weighted BMO spaces reaction zone and/or hydrotreating
Reaction zone, isolated liquid phase are directly entered catalytic cracking reaction zone and carry out catalytic cracking reaction, catalytic cracking reaction outflow
It the isolated dry gas of object, liquefied gas, catalytically cracked gasoline fraction, catalytic cracking diesel oil fraction, heavy catalytic cycle oil and urges
Change cracking slurry oil, wherein some or all of catalytic cracking diesel oil is recycled back to weighted BMO spaces reaction zone and carries out hydrogenation reaction；Institute
The weighted BMO spaces reactor that weighted BMO spaces reaction zone includes the setting of two more parallels is stated, when the weighted BMO spaces react
It is when the pressure drop of any weighted BMO spaces reactor reaches the 50%~80% of the reactor design pressure drop upper limit in area, this plus hydrogen is pre-
Treatment reactor is cut out from weighted BMO spaces reaction zone, and the weighted BMO spaces reactor is named as to cut out plus hydrogen and is located in advance
Reactor I is managed, and passes through weighted BMO spaces reaction zone, the weighted BMO spaces reactor I cut out, hydrotreating successively according to material
The sequence of reaction zone is by weighted BMO spaces reactor that this cuts out with weighted BMO spaces reaction zone and hydrotreating reaction area to go here and there
The mode of connection connects, and the charging of the weighted BMO spaces reactor cut out at this time is except the weighted BMO spaces cut out react
The reaction effluent of weighted BMO spaces reactor except device, when the pressure drop of next weighted BMO spaces reactor reaches reactor
When designing the 50%~80% of the pressure drop upper limit, which is cut out from weighted BMO spaces reaction zone, and should
The weighted BMO spaces reactor cut out is named as the weighted BMO spaces reactor II cut out, and according to material successively by adding hydrogen pre-
Processing reaction zone, the weighted BMO spaces reactor II cut out, the weighted BMO spaces reactor I cut out, hydrotreating reaction area
Sequence 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 with
Concatenated mode connects, and the charging of the weighted BMO spaces reactor II cut out at this time is weighted BMO spaces reaction zone except having cut out
The reaction effluent of remaining weighted BMO spaces reactor except weighted BMO spaces reactor, in the manner described above, until all
Weighted BMO spaces reactor be all connected in series to.
2. according to the method for claim 1, it is characterised in that：When any adds hydrogen pre- in the weighted BMO spaces reaction zone
When the pressure drop for the treatment of reactor reaches the 60%~70% of the reactor design pressure drop upper limit, by the weighted BMO spaces reactor from adding hydrogen
Pretreatment reaction is cut out in area, and the weighted BMO spaces reactor is named as to the weighted BMO spaces reactor I cut out, and according to
Material successively pass through weighted BMO spaces reaction zone, the weighted BMO spaces reactor I cut out, hydrotreating reaction area sequence should
The weighted BMO spaces reactor cut out is connected in series to weighted BMO spaces reaction zone and hydrotreating reaction area,
The charging of the weighted BMO spaces reactor cut out at this time is that in addition to the weighted BMO spaces cut out the reactor plus hydrogen is located in advance
The reaction effluent for managing reactor, when the pressure drop of next weighted BMO spaces reactor reaches the reactor design pressure drop upper limit
When 60%~70%, which is cut out from weighted BMO spaces reaction zone, and adds hydrogen to locate in advance by what this cut out
Reason reactor is named as the weighted BMO spaces reactor II cut out, and passes through weighted BMO spaces reaction zone successively according to material, cuts
The weighted BMO spaces reactor II that goes out, the weighted BMO spaces reactor I that cuts out, hydrotreating reaction area sequence this is cut out
Weighted BMO spaces reactor II connects in series with weighted BMO spaces reaction zone and the weighted BMO spaces reactor I cut out
It connects, it is anti-that the charging of the weighted BMO spaces reactor II cut out at this time is that weighted BMO spaces reaction zone removes the weighted BMO spaces cut out
The reaction effluent of remaining weighted BMO spaces reactor except device is answered, in the manner described above, until all weighted BMO spaces
Reactor is all connected in series to.
3. according to the method for claim 1, it is characterised in that：All plus hydrogen in the weighted BMO spaces reaction zone is located in advance
Reach the 50%~80% of the reactor pressure decrease design upper limit when managing reactor difference.
4. according to the method for claim 3, it is characterised in that：Pass through the difference of process conditions setting and catalyst bed property
It is different so that when each weighted BMO spaces reactor difference of weighted BMO spaces reaction zone reach the reactor pressure decrease design upper limit 50%~
80%。
5. according to 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
It is lower to be reached when each weighted BMO spaces reactor difference to realize using one or more of different Catalyst packing density
Reactor pressure decrease designs the 50%~80% of the upper limit.
6. according to the method for claim 5, it is characterised in that：When the weighted BMO spaces reaction zone each plus hydrogen in parallel
When preatreating reactors uses different Catalyst packing density, the weighted BMO spaces reaction zone each plus hydrogen in parallel is located in advance
It manages in reactor, maximum loading density is 400kg/m3~600kg/m3, minimum loading density is 300kg/m3~550kg/m3。
7. according to the method for claim 6, it is characterised in that：When the weighted BMO spaces reaction zone each plus hydrogen in parallel
When preatreating reactors uses different Catalyst packing density, the weighted BMO spaces reaction zone each plus hydrogen in parallel is located in advance
It manages 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：Immediate two of the loading density plus hydrogen are located in advance
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：Immediate two of the loading density plus hydrogen are located in advance
The Catalyst packing density difference for managing reactor is 80~150kg/m3。
10. according to 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. according to 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. according to 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, controls operating pressure and immediate two of volume space velocity plus hydrogen is located in advance
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, operating pressure and immediate two of volume space velocity plus hydrogen are controlled
In the operating condition of preatreating reactors, operation temperature difference is 5 ~ 20 DEG C.
16. according to the method for claim 1, it is characterised in that：Into the catalytic cracking diesel oil of weighted BMO spaces reaction zone
Fraction is the catalytic cracking diesel oil that catalytic cracking reaction zone obtains in the hydrogenation and catalystic cracking combined process for residual oil
Fraction, or the catalytic cracking diesel oil fraction that is obtained including other catalytic cracking units.
17. according to the method for claim 1, it is characterised in that：It is recycled back to the catalytic cracking bavin of weighted BMO spaces reaction zone
Oil distillate enters one or several in the weighted BMO spaces reactor being arranged in parallel.
18. according to the method for claim 1, it is characterised in that：The weighted BMO spaces reaction zone includes 3~6 parallel connections
The weighted BMO spaces reactor of setting.
19. according to the method described in claim 1 or 18, 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.
20. according to the method for claim 1, it is characterised in that：The hydrotreating reaction area includes 1~5 series connection
The hydrotreating reactor of setting.
21. according to the method described in claims 1 or 20, it is characterised in that：The hydrotreating reaction area includes 1~2
The hydrotreating reactor being arranged in series.
22. according to 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 is 10MPa~25MPa, and hydrogen to oil volume ratio is 300~1500, when raw material fluid
Volume space velocity is 0.15h-1~2.00h-1。
23. according to the method described in claims 1 or 22, it is characterised in that：The operating condition of the weighted BMO spaces reaction zone
For：Reaction temperature is 380 DEG C~400 DEG C, and reaction pressure is 15MPa~20MPa, and hydrogen to oil volume ratio is 500~800, feedstock oil
Volume space velocity is 0.3h when liquid-1~1.00h-1。
24. according to 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, body when raw material fluid
Product air speed is 0.15h-1~0.80h-1。
25. according to the method described in claims 1 or 24, 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 is 15MPa~20MPa, and hydrogen to oil volume ratio is 400~800, when raw material fluid
Volume space velocity is 0.2h-1~0.60h-1。
26. according to the method for claim 1, it is characterised in that：The feed residue is reduced crude or decompression slag
Oil, or contain straight-run gas oil, decompressed wax oil, one or more of secondary operation wax oil and FCC recycle oil.
27. according to 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.
28. according to 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, and regeneration temperature is 650~750 DEG C, agent weight of oil than 4~10, with catalyst contact time for 0.5~
5 seconds, pressure was 0.1~0.5MPa.
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| CN102041095A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Resid hydrotreating and catalytic cracking combined processing method |
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