CN106701175B - A kind of low grade oils processing method - Google Patents
A kind of low grade oils processing method Download PDFInfo
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- CN106701175B CN106701175B CN201510769249.3A CN201510769249A CN106701175B CN 106701175 B CN106701175 B CN 106701175B CN 201510769249 A CN201510769249 A CN 201510769249A CN 106701175 B CN106701175 B CN 106701175B
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Abstract
The invention discloses a kind of low grade oils processing method, including weighted BMO spaces reaction zone, hydrotreating reaction area and catalytic cracking reaction zone；The process includes the following contents：Successively by the weighted BMO spaces reaction zone of series connection and hydrotreating reaction area after residual oil raw material and hydrogen mixing, 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, the hydrotreating reaction area that is partly or entirely recycled back to of catalytic cracking diesel oil and heavy catalytic cycle oil carries out hydrotreating reaction area.The method of the present invention can extend the stabilization operation period 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
At present, the demand that demand of the domestic and international refined products market to oil products such as steam coal bavins is particularly to motor petrol will be in hold
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 with relatively warp
The rational cost of helping realizes heavy oil lighting and petrol and diesel oil product quality persistently upgrades and become what oil refining industry both at home and abroad was paid close attention to
Focus.
The main purpose of residual hydrocracking technique is by hydrotreating, makes sulphur, nitrogen, metal in residual oil raw material etc. miscellaneous
Matter content is greatly reduced, the undesirable components hydro-conversion such as condensed-nuclei aromatics, colloid, asphalitine, improves hydrogen-carbon ratio, reduces carbon residue and contains
Amount, make its cracking performance be improved significantly.Fixed bed residual hydrogenation technology is a kind of heavy oil deep processing technology, equipped with spy
In the fixed bed reactors for determining catalyst, under the hydro condition of 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, the dosage form of catalyst is optimized, according to different physical according to the requirement of the property of original oil, reaction condition and purpose product
Matter, catalyst activity and all kinds of catalyst ratios carry out grading loading.Fixed bed residual hydrogenation technology although having many advantages, such as,
But the phenomenon that in process of production, being but susceptible to reactor pressure drop increase.Industrial operation shows reactor pressure drop increase
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 more than 70% demetalization, metal sulfide is deposited on catalyst bed, into operation after
Inevitably there is pressure drop rapid growth in phase, and reactor below is since demetalization load is significantly relatively low, pressure drop increase compared with
Slowly.This affects the cycle of operation and the device of device there have been forepart 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, what which included once connecting adds 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, shortcoming are the reactors that left unused, and 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, while change 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 service cycle of device,
And the processing capacity of device can be increased, help to improve flow distribution.Shortcoming is that inductor manufacture cost increases, and is made initial
Pressure drop increases, and device inner volume utilization rate reduces etc..
CN103059931A discloses a kind of method of residual hydrocracking.This method is in hydrotreating reaction condition
Under, residual oil raw material and hydrogen once by more reactors of series connection, when 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 low grade oils processing methods.This method technique stream
Journey is simple, it is only necessary to carry out simple modifications to existing apparatus, it is possible to substantially extend the service cycle of whole device, and can make
The utilization ratio of catalyst, which is realized, to be maximized.
Existing residual hydrocracking technology, all reactors are using the technological process connected, it is therefore desirable to anti-in First
Device is answered to load a large amount of protective agent to deposit the impurity in raw material and dirty object, 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 improve its catalyst activity again
The rapid growth of pressure drop can be caused, shortens the cycle of operation, and subsequent catalyst performance plays completely not yet, keeps First
The appropriate activity of protection reactor catalyst is 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 the relatively low reaction of an anti-protection reactor catalyst, main function intercept and the impurity in deposition raw material and
Dirty object only carries out relatively low demetalization reaction, and the typically reactor reaction temperature rises relatively low, and pressure drop is tieed up in the whole service period
It holds in relatively low level, is substantially carried out taking off this requires that loading a large amount of catalyst for demetalation in subsequent demetalization reactor
Metal reaction and metallic compound and carbon distribution to accommodate hydrogenation and removing provide enough spaces, 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.
The present invention provides a kind of low grade oils processing method, including weighted BMO spaces reaction zone, hydrotreating reaction
Area and catalytic cracking reaction zone；The process includes the following contents：Residual oil raw material, at least part catalytic cracking diesel oil fraction
Through the weighted BMO spaces reaction zone being arranged in series after being mixed at least part heavy catalytic cycle oil with hydrogen successively and add
Hydrogen handles reaction zone, and the reaction effluent in hydrotreating reaction area carries out gas-liquid separation, and isolated gas phase is recycled back to plus hydrogen
Pretreatment reaction area and/or hydrotreating reaction area, isolated liquid phase are directly entered catalytic cracking reaction zone and are catalyzed
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, being partly or entirely recycled back to for catalytic cracking diesel oil adds hydrogen pre-
It handles reaction zone and carries out hydrogenation reaction, heavy catalytic cycle oil is partly or entirely recycled back to the progress of weighted BMO spaces reaction zone
Hydrogenation reaction；The weighted BMO spaces reaction zone includes the weighted BMO spaces reactor of two more parallel settings, adds when described
The pressure drop of any weighted BMO spaces reactor reaches the 50%~80% of the reactor design pressure drop upper limit in hydrogen pretreatment reaction zone,
It is preferred that when 60%~70%, which is cut out from weighted BMO spaces reaction zone, and by the weighted BMO spaces
Reactor is named as the weighted BMO spaces reactor I cut out, and according to material successively by weighted BMO spaces reaction zone, cut out
Weighted BMO spaces reactor I, hydrotreating reaction area sequence by the weighted BMO spaces reactor cut out and weighted BMO spaces
Reaction zone and hydrotreating reaction area are connected in series to, at this time the charging of weighted BMO spaces reactor cut out
It is the reaction effluent of the weighted BMO spaces reactor in addition to the weighted BMO spaces cut out the reactor, adds hydrogen pre- when next
The pressure drop for the treatment of reactor reaches the 50%~80% of the reactor design pressure drop upper limit, and when preferably 60%~70%, this plus hydrogen are located in advance
Reason reactor is cut out from weighted BMO spaces reaction zone, and the weighted BMO spaces reactor that this cuts out is named as to cut out plus hydrogen
Preatreating reactors II, and according to material successively by weighted BMO spaces reaction zone, cut out weighted BMO spaces reactor II, cut
The weighted BMO spaces reactor I that goes out, the sequence in hydrotreating reaction area by the weighted BMO spaces reactor II cut out with plus hydrogen
Pretreatment reaction area and the weighted BMO spaces reactor I cut out are connected in series to, and the weighted BMO spaces cut out at this time are anti-
The charging for answering device II is remaining weighted BMO spaces of weighted BMO spaces reaction zone in addition to the weighted BMO spaces reactor cut out
The reaction effluent of reactor, in the manner described above, until all weighted BMO spaces reactor is all in series
Connection.
In low grade oils processing method of the present invention, all weighted BMO spaces in the weighted BMO spaces reaction zone are anti-
Reach the 50%~80% of the reactor pressure decrease design upper limit when answering device difference, can be set and catalyst bed by process conditions
The difference of matter to reach during each weighted BMO spaces reactor difference of weighted BMO spaces reaction zone the pressure drop design upper limit 50%~
80%.Specifically can be by controlling different catalyst packing height in each weighted BMO spaces reactor, different inlet amounies,
It is close that different Catalyst packings may be used under the conditions of identical filling height in different feed properties, different operating conditions
Degree when one or more of means come realize reach during each weighted BMO spaces reactor difference pressure drop design the upper limit 50%~
80%。
As described above, each weighted BMO spaces reactor when weighted BMO spaces reaction zone parallel connection is urged using different
During 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.It is first that be cut out plus hydrogen is pre- when other conditions are consistent
The Catalyst packing density for the treatment of reactor is maximum, and the Catalyst packing density for the weighted BMO spaces reactor being finally cut out is most
It is small.The difference loading density can be equipped with by different types of catalyst grade tamps it is existing, such as can by hydrogenation protecting agent,
Hydrodemetalation catalyst, Hydrobon catalyst realize the catalyst in each weighted BMO spaces reactor in different proportions
Loading density is different.
As described above, when weighted BMO spaces reaction zone parallel connection each weighted BMO spaces reactor using it is different into
During doses, the ratio between feed volume air speed of the immediate two weighted BMO spaces reactors of inlet amount is 1.1 ~ 3.0, preferably
1.1~1.5。
As described above, when weighted BMO spaces reaction zone parallel connection each weighted BMO spaces reactor using 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 low grade oils processing method of the present invention, catalytic cracking diesel oil fraction into weighted BMO spaces reaction zone,
Heavy catalytic cycle oil fraction can be Catalytic Cracking Unit of Measure in hydrogenation and catalystic cracking combined process for residual oil of the present invention
Catalytic cracking diesel oil fraction, the heavy catalytic cycle oil fraction that area obtains are answered, can also be obtained including other catalytic cracking units
Catalytic cracking diesel oil fraction, the heavy catalytic cycle oil fraction arrived.It is catalyzed and splits in low grade oils processing method of the present invention
Weighted BMO spaces reaction zone can completely or partially be entered by changing the catalytic cracking diesel oil fraction that reaction zone obtains, and be located in advance into hydrogen is added
The catalytic cracking diesel oil fraction of reason reaction zone generally at least account for the 30% of diesel oil distillate weight that catalytic cracking reaction zone obtains with
On, preferably more than 50%.The catalytic cracking diesel oil fraction of remainder can be recycled back to catalytic cracking reaction zone or do as needed
To be arranged outside product.At least more than the 40% of the heavy catalytic cycle oil weight that catalytic cracking reaction zone obtains enters plus hydrogen is located in advance
Reaction zone is managed, preferably more than 80% enters weighted BMO spaces reaction zone, and remaining heavy catalytic cycle oil is recycled back to catalytic cracking
Reaction zone.It is arranged outside catalytic cracked oil pulp for other suitabilities, such as producing pitch.
In low grade oils processing method of the present invention, it is recycled back to the catalytic cracking diesel oil fraction of weighted BMO spaces reaction zone
One or several in the weighted BMO spaces reactor being arranged in parallel can be entered, preferably respectively enter difference in suitable ratio
Weighted BMO spaces reactor.Being recycled back to the heavy catalytic cycle oil fraction of weighted BMO spaces reaction zone can set into parallel connection
One or several in the weighted BMO spaces reactor put, it is anti-preferably different weighted BMO spaces to be respectively enterd in suitable ratio
Answer device.
In low grade oils processing method of the present invention, the weighted BMO spaces reaction zone includes two more parallels and sets
Weighted BMO spaces reactor, preferably include 3~6 weighted BMO spaces reactors being arranged in parallel, more preferably include 3 or 4
The weighted BMO spaces reactor that platform is arranged in parallel.The hydrotreating reaction area includes 1~5 hydrotreating being arranged in series
Reactor preferably includes 1~2 hydrotreating reactor being arranged in series.
In low grade oils processing method of the present invention, the operating condition of the weighted BMO spaces reaction zone is：Reaction temperature
It is 370 DEG C~420 DEG C to spend, preferably 380 DEG C~400 DEG C, and 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.The residual oil that the average reaction temperature of weighted BMO spaces reaction zone is apparently higher than the prior art adds
The reaction temperature of hydrogen demetalization reactor, the residuum hydrogenating and metal-eliminating reaction temperature of the prior art is usually 350 DEG C~390 DEG C.
The weighted BMO spaces reaction zone of this method middle front part setting eliminates pressure drop and increases restrictive cycle by the optimization of technological process
Unfavorable factor can operate at high temperature, and in addition relatively high reaction temperature is conducive to loaded catalyst system performance
It plays, is conducive to the removing of the hydro-conversion and impurity of macromolecular.
In low grade oils processing method of the present invention, the operating condition in the hydrotreating reaction area is that reaction temperature is
370 DEG C~430 DEG C, preferably 380 DEG C~410 DEG C, reaction pressure is 10MPa~25MPa, preferably 15MPa~20MPa；Hydrogen
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 low grade oils processing method of the present invention, this field routine techniques may be used in catalytic cracking.Catalytic cracking
Device can be more than a set of or a set of, and a reactor and a regenerator should at least be included by often covering catalytic cracking unit, be urged
Fractionating column need to be set by changing cracking unit, can be set fractionating column respectively with every set catalytic cracking unit, can also be shared fractionating column.Point
Evaporate tower by catalytic cracking reaction effluent fractionation for dry gas, liquefied gas, catalytically cracked gasoline fraction, catalytic cracking diesel oil fraction,
Catalytic cracking recycle oil and catalytic cracked oil pulp etc..Catalytic cracking fractionating tower can routinely knowledge design.
In low grade oils processing method of the present invention, the operating condition of the catalytic cracking reaction zone is：Reaction temperature
It 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 for 0.1~
0.5MPa.Used catalytic cracking catalyst includes the catalyst commonly used in catalytic cracking, as silica-alumina catalyst, silicon magnesium are urged
Agent, the carclazyte of acid processing and X-type, Y types, ZSM-5, M type, preferably layer column equimolecular sieve Cracking catalyst, 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, high conversion rate.The catalysis
The reactor of cracking unit can be the catalyst cracker of various types, preferably riser reactor or riser extra bed
Layer reactor.Technological process is generally：Feedstock oil is injected from riser reactor bottom, is urged with the high temperature regeneration from regenerator
Agent contacts, and the oil gas of cracking reaction generation and the catalyst mixture of deposit coke are moved up along riser reactor, complete
Into the catalytic cracking reaction of entire feedstock oil.
In low grade oils processing method of the present invention, residual hydrogenation technology uses fixed bed residual hydrocracking technology,
Hydrogenation protecting agent, hydrodemetallisation catalyst can be loaded in each weighted BMO spaces reactor of the weighted BMO spaces reaction zone
One or more of agent, Hydrobon catalyst, hydrodenitrogeneration carbon residue reforming catalyst, can in the hydrotreating reaction area
To load one or more of Hydrobon catalyst and hydrodenitrogeneration carbon residue reforming catalyst, the hydrogenation protecting agent adds
Hydrogen catalyst for demetalation, Hydrobon catalyst, hydrodenitrogeneration carbon residue reforming catalyst are fixed bed residual hydrocracking
The catalyst of Cheng Suoyong.Above-mentioned catalyst is typically all the group VIB using porous refractory inorganic oxide such as aluminium oxide as carrier
And/or the oxide of group VIII metal such as W, Mo, Co, Ni etc. be active component, be selectively added other various auxiliary agents such as P,
The catalyst of the elements such as Si, F, B, such as the FZC series by the production of catalyst branch company of Sinopec Group
Catalyst for hydrotreatment of residual oil.
In low grade oils processing method of the present invention, the feed residue can be that reduced crude can also be decompression
Residual oil usually also contains straight-run gas oil, decompressed wax oil, one or more of secondary operation wax oil and FCC recycle oil.It is described
Residual oil raw material property be：Sulfur content is not more than 4wt%, and nitrogen content is not more than 0.7wt%, and tenor (Ni+V) is no more than 120
μ g/g, carbon residue are not more than 17wt%, and asphalt content is not more than 5wt%.
Compared with prior art, low grade oils processing method of the present invention has the following advantages：
1st, in the method for the present invention, the weighted BMO spaces reaction zone includes more weighted BMO spaces reactors in parallel,
So that entire catalyst system takes off/holds metal ability and is increased dramatically.
2nd, 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 the cycle of operation of whole device.
3rd, 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 is taken off while the de-/appearance metal ability for improving monolithic catalyst
Sulphur takes off carbon residue performance and is guaranteed.
4th, the method for the present invention is by the way that each weighted BMO spaces reactor of weighted BMO spaces reaction zone is cut from series connection is parallel to
The adjustment for changing mode of operation solves the problems, such as reactor pressure decrease rapid growth, while increases the operating flexibility and original of device
Expect adaptability；
5th, the method for the present invention is by setting weighted BMO spaces reactor parallel form that the appearance gold of catalyst system is significantly increased
Category amount so that the stability enhancing of system so that the growth of device pressure drop can be controlled, and extend the device cycle of operation.
6th, the method for the present invention can utmostly realize that all kinds of catalyst synchronize inactivation, so as to improve the operation of device effect
Rate is increased economic efficiency.
7th, 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 the pressure of each preatreating reactors of adjustment matched by catalyst grade
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 macromolecular in raw material such as gum asphalt
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 instead without reducing.
8th, 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 and mass transfer in system 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 and heavy catalytic cycle oil fraction can be in Residue Hydrotreating Technology processes
Middle imurity-removal, aromatic hydrocarbons saturation become better catalytically cracked material composition, further improve the production of catalytic cracking high added value
Product yield.
9th, it in group technology of the present invention, is not required to set fractionating system in hydrotreating reaction area, hydrotreating generation oil is directly
Into catalyst cracker, it is not required to set feed pump, while reduce a large amount of heat transmission equipments.Equipment investment is made to have very big drop
It is low.
Description of the drawings
Fig. 1 is low grade oils processing method flow chart of the present invention.
Specific embodiment
Method provided by the present invention is further detailed below in conjunction with the accompanying drawings, but does not therefore limit this hair
It is bright.
As shown in Figure 1, low grade oils processing method of the present invention includes the following contents：After residual oil raw material is mixed with hydrogen
Material G enter the weighted BMO spaces reaction zone that is arranged in series through feeding line 1, feeding line 2 and feeding line 3 and add at hydrogen
Reaction zone is managed, the weighted BMO spaces reaction zone includes three weighted BMO spaces reactors being arranged in parallel, and respectively plus hydrogen is pre-
Treatment reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C, the weighted BMO spaces reactor A plus hydrogen are pre-
Treatment reactor B, weighted BMO spaces reactor C feed inlet connect respectively with feeding line 1, feeding line 2 and feeding line 3
It connects, three tunnels of outlet point of the weighted BMO spaces reactor A, feed inlet of the first via through pipeline 6 Yu weighted BMO spaces reactor B
Connection, the second tunnel are connect through pipeline 7 with the feed inlet of weighted BMO spaces reactor C, and third road is anti-through pipeline 10 and hydrotreating
Answer device D connections；Three tunnels of the outlet of the weighted BMO spaces reactor B point, the first via is through pipeline 4 and weighted BMO spaces reactor A
Feed inlet connection, the second tunnel obtains feed inlet with weighted BMO spaces reactor C through pipeline 5 and connect, and third road is through pipeline 11 and adds
The D connections of hydrogen treatment reactor；Three tunnels of the outlet of the weighted BMO spaces reactor C point, the first via is through pipeline 8 and weighted BMO spaces
The feed inlet connection of reactor A, the second tunnel are connect through pipeline 9 with the feed inlet of weighted BMO spaces reactor B, and third road is through pipeline
12 connect with hydrotreating reactor D；Valve 101 is provided on the pipeline 1, valve 102, institute are provided on the pipeline 2
It states and valve 103 is provided on pipeline 3, valve 104 is provided on the pipeline 4, valve 105 is provided on the pipeline 5, it is described
Valve 106 is provided on pipeline 6, valve 107 is provided on the pipeline 7, valve 108, the pipe are provided on the pipeline 8
Valve 109 is provided on line 9, valve 1010 is provided on the pipeline 10, valve 1011 is provided on the pipeline 11, it is described
Valve 1012 is provided on pipeline 12, the generation oil 13 that the hydrotreating reactor obtains obtains after entering separator E separation
Liquefied gas 20 and hydrogenated oil 14 are obtained, the hydrogenated oil 14 enters catalytic cracking reaction zone F, is catalyzed with high temperature regeneration
Cracking catalyst contacts and carries out catalytic cracking reaction, and product is fractionated into obtaining gas 15, catalytically cracked gasoline fraction after reaction
16th, catalytic cracking diesel oil fraction 17, catalytic cracking recycle oil 18 and catalytic cracked oil pulp 19, gas 15 and catalytically cracked gasoline evaporate
Dividing 16 dischargers, catalytic cracking diesel oil fraction 17 and heavy catalytic cycle oil fraction 18 return to weighted BMO spaces reaction zone,
Weighted BMO spaces reaction zone is mixed into residual oil raw material to be reacted, 19 discharger of catalytic cracked oil pulp carries out suitable treatment
After utilize.
In low grade oils processing method 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, altogether including following 6 kinds of processes
1st, 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
Into the handover operation once by being parallel to series connection；
（3）When the pressure drop of weighted BMO spaces reactor B reaches critical value, valve 102, the pipeline 8 of feeding line 2 are closed
Valve 108, open pipeline 9 on valve 109, at this time 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, entire reaction system needs shutdown process.
2nd, 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
Into the handover operation once by being parallel to series connection；
（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 handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor C reaches critical value, entire reaction system needs shutdown process.
3rd, 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
Into the handover operation once by being parallel to series connection；
（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 handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor A reaches critical value, entire reaction system needs shutdown process.
4th, 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
Into the handover operation once by being parallel to series connection；
（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 handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor C reaches critical value, entire reaction system needs shutdown process.
5th, 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
Into the handover operation once by being parallel to series connection；
（3）When the pressure drop of weighted BMO spaces reactor B reaches critical value, valve 102, the pipeline 7 of feeding line 2 are closed
Valve 107, open pipeline 6 on valve 106, at this time 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, entire reaction system needs shutdown process.
6th, 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
Into the handover operation once by being parallel to series connection；
（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 handover operation by being parallel to series connection；
（4）When the pressure drop of weighted BMO spaces reactor B reaches critical value, entire reaction system needs shutdown process.
Illustrate the effect of the present invention with reference to specific embodiment, it is used in embodiment of the present invention and comparative example
Raw material includes three kinds, respectively raw material A, raw material B, raw material C, and specific nature is shown in Table 1, the dress of catalyst in the 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 with 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, weighted BMO spaces reactor C residual oil described in embodiment 1
Charging is all shown in Table 1 using raw material A property, by 50% catalytic cracking diesel oil of catalytic cracking unit and whole catalytic cracking weights
Recycle oil is recycled to weighted BMO spaces reaction zone, and property is shown in Table 2.Wherein heavy catalytic cycle oil is fully allocated to plus hydrogen is located in advance
Reason reactor A, distribute to the catalytic cracking diesel oil ratio of weighted BMO spaces reactor B for 15%, distribute to weighted BMO spaces reaction
The catalytic cracking diesel oil ratio of device C is 35%.The weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces
The catalyst inventory of reactor C, feed properties are identical with inlet amount, and the weighted BMO spaces reactor A plus hydrogen are located in advance
Reason reactor B, weighted BMO spaces reactor C, hydrotreating reactor D catalyst loaded in the way of in table 3, the slag
Oily Hydroprocessing conditions are 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 to be catalyzed
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, in the weighted BMO spaces reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C
All using residual oil raw material B, 30% catalytic cracking diesel oil of catalytic cracking unit and whole heavy catalytic cycle oils are recycled
To weighted BMO spaces reaction zone, wherein heavy catalytic cycle oil is fully allocated to weighted BMO spaces reactor A, distributes to plus hydrogen
The catalytic cracking diesel oil ratio of preatreating reactors B is 15%, distributes to the catalytic cracking diesel oil ratio of weighted BMO spaces reactor C
Example is 15%.Each anti-Feed space velocities are different, and volume space velocity is 0.20h during the weighted BMO spaces reactor A liquid-1, weighted BMO spaces
Volume space velocity is 0.32h during reactor B liquid-1, volume space velocity is 0.44h during weighted BMO spaces reactor C liquid-1.Weighted BMO spaces
Using identical catalyst loading pattern, catalyst in reactor A, weighted BMO spaces reactor B, weighted BMO spaces reactor C
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.Catalytic cracking is grasped
8 are shown in Table as condition, 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 residual oil raw material property used is shown in Table 1, by the 50% of catalytic cracking unit using raw material C in B, weighted BMO spaces reactor C
Catalytic cracking diesel oil and whole heavy catalytic cycle oils are recycled to weighted BMO spaces reaction zone, and wherein catalytic cracking is recirculated
Oil be fully allocated to weighted BMO spaces reactor A, distribute to the catalytic cracking diesel oil ratio of weighted BMO spaces reactor B for 25%,
The catalytic cracking diesel oil ratio for distributing to weighted BMO spaces reactor C is 25%.The weighted BMO spaces reactor A plus hydrogen are located in advance
It is identical to manage reactor B, the inlet amount of weighted BMO spaces reactor C, the weighted BMO spaces reactor A, weighted BMO spaces reaction
3 are shown in Table using identical catalyst loading pattern, catalyst loading pattern in device B, weighted BMO spaces reactor C, the residual oil
Hydroprocessing conditions are 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 catalysis is split
Change catalyst property and be shown in Table 9, 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 feeding, 30% catalytic cracking diesel oil of catalytic cracking unit and whole heavy catalytic cycle oils are followed
Ring to weighted BMO spaces reaction zone, wherein heavy catalytic cycle oil be fully allocated to weighted BMO spaces reactor A, distribute to plus
The catalytic cracking diesel oil ratio of hydrogen pretreatment reactor B is 10%, distributes to the catalytic cracking diesel oil of weighted BMO spaces reactor C
Ratio is 20%.Three weighted BMO spaces reactor feed amounts are identical.The weighted BMO spaces reactor A average response temperature
Spend for 365 DEG C, weighted BMO spaces reactor B average reaction temperature be 375 DEG C, weighted BMO spaces reactor C average reaction temperatures
Average reaction temperature for 385 DEG C, hydrotreating reactor D is 383 DEG C, and 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 is urged
Agent property is shown in Table 9, and catalytic cracking product distribution of products property is shown in Table 10.
Comparative example 1
Also using 4 reactors, respectively reactor A, reactor B, reactor C, reactor D, reactor in comparative example 1
A, reactor B, reactor C are connected with reactor D in the form of being sequentially connected in series.Raw materials used A properties are shown in Table 1 in comparative example 1,
The inlet amount and feed properties of reactor A are identical with the total feed and feed properties of embodiment 1.It is the reactor A, anti-
Answer catalyst inventory weighted BMO spaces reactor A corresponding with embodiment, the weighted BMO spaces of device B, reactor C and reactor D
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, catalytic cracking weight
Recycle oil recycles cracking inside catalytic cracking unit.The residual hydrogenation operating condition is shown in Table 6, and specific reaction result is shown in Table 7.
Hydrocarbon Content by Catalytic Cracking Operation condition is shown in Table 8, and specific catalytic cracking catalyst property is shown in Table 9, and catalytic cracking product distribution of products property is shown in
Table 10.
Comparative example 2
Also using 4 reactors, respectively reactor A, reactor B, reactor C, reactor D, reactor in comparative example 2
A, reactor B, reactor C are connected with reactor D in the form of being sequentially connected in series.It is shown in Table in comparative example 2 using raw material B, property
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 of C and reactor D and 2 corresponding weighted BMO spaces reactor A of embodiment, weighted BMO spaces reactor B plus
Hydrogen pretreatment reactor C, hydrodesulphurisatioreactors reactors D are identical, but the loadings of various species catalyst are different, according to table
Mode in 4 is loaded, and the residual hydrogenation operating condition is shown in Table 6, and specific reaction result is shown in Table 7.Hydrocarbon Content by Catalytic Cracking Operation condition is shown in
Table 8, specific catalytic cracking catalyst property are shown in Table 9, and catalytic cracking product distribution of products property is shown in Table 10.Catalytic cracking unit obtains
To catalytic cracking diesel oil directly go out device, heavy catalytic cycle oil recycles cracking inside catalytic cracking unit.
Comparative example 3
Also using 4 reactors, respectively reactor A, reactor B, reactor C, reactor D, reactor 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 are using the form of series connection, reactor A in comparative example
Entrance is identical with inlet amount and mixed feeding property that embodiment 3 is total.The reactor A, reactor B, reactor C and reactor
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, and heavy catalytic cycle oil recycles cracking inside catalytic cracking unit.
Comparative example 4
Also using 4 reactors, respectively reactor A, reactor B, reactor C, reactor D, reactor in comparative example 4
A, reactor B, reactor C are connected with reactor D in the form of being sequentially connected in series.Comparative example 4 uses raw material C, and property is shown in Table 1,
Using the form of series connection, reactor A entrance and embodiment 4 are total by reactor A, reactor B, reactor C and reactor D in comparative example
Inlet amount it is identical with feed properties.The reactor A, reactor B, reactor C and reactor D catalyst inventory and reality
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, and heavy catalytic cycle oil is filled in catalytic cracking
Put internal cycle cracking.
1 residual oil raw material property of table
2 catalytic cracking diesel oil of table and heavy-cycle oil property
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 generation oil nature
| Embodiment 1 | Comparative example 1 | Embodiment 2 | Comparative example 2 | |
| Fortune Turn Week Phase | 9950 hours, wherein 6600 hours are pre- Treatment reactor C pressure drops reach design Value, 8560 hours preatreating reactors B pressure drops reach design value | 8500 hours two Back-pressure drop reaches Design upper limit dress It puts and is forced to stop work. | 9700 hours, wherein 6400 hours are pre- Treatment reactor C pressure drops reach design Value, 8200 hours preatreating reactors B pressure drops reach design value | 8072 hours two Back-pressure drop reaches Design upper limit dress It puts and is forced to stop work. |
| It is close Degree (20 ℃) , g/ cm3 | 935.0 | 938.8 | 931 | 934 |
| S, wt% | 0.42 | 0.46 | 0.39 | 0.43 |
| N, μ g.g-1 | 1467 | 1580 | 1548 | 1615 |
| CCR , wt% | 5.12 | 5.60 | 5.16 | 5.77 |
| Ni + V, μ g.g-1 | 12.2 | 14.7 | 13 | 16 |
| Embodiment 3 | Comparative example 3 | Embodiment 4 | Comparative example 4 | |
| Fortune Turn Week Phase | 11100 hours, wherein 6900 hours Preatreating reactors A pressure drops, which reach, to be set Evaluation, 8300 hours pretreatment reactions Device B pressure drops reach design value | 8430 hours two Back-pressure drop reaches Design upper limit dress It puts and is forced to stop work. | 9640 hours, wherein 6200 hours are pre- Treatment reactor C pressure drops reach design Value, 8200 hours preatreating reactors B pressure drops reach design value | 8500 hours two Back-pressure drop reaches Design upper limit dress It puts and is forced to stop work. |
| It is close Degree (20 ℃) , g/ cm3 | 932 | 930 | 927 | 929 |
| S, wt% | 0.41 | 0.48 | 0.31 | 0.36 |
| N, μ g.g-1 | 2117 | 2346 | 1830 | 2037 |
| CCR , wt% | 4.60 | 5.26 | 5.12 | 5.86 |
| Ni + V, μ g.g-1 | 13.8 | 15.5 | 12.6 | 15.6 |
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 (31)
1. a kind of low grade oils processing method, including weighted BMO spaces reaction zone, hydrotreating reaction area and catalytic cracking
Reaction zone；The process includes the following contents：Residual oil raw material, at least part catalytic cracking diesel oil fraction and at least part are urged
Change after cracking heavy-cycle oil 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
Cracking reaction effluent isolated dry gas, liquefied gas, catalytically cracked gasoline fraction, catalytic cracking diesel oil in fractionating device evaporate
Point, heavy catalytic cycle oil and catalytic cracked oil pulp, wherein, catalytic cracking diesel oil be partly or entirely recycled back to plus hydrogen is located in advance
It manages reaction zone and carries out hydrogenation reaction, heavy catalytic cycle oil is partly or entirely recycled back to weighted BMO spaces reaction zone and is added
Hydrogen reacts；The weighted BMO spaces reaction zone includes the weighted BMO spaces reactor of two more parallel settings, when described plus hydrogen
When the pressure drop of First weighted BMO spaces reactor reaches the 50%~80% of the reactor design pressure drop upper limit in pretreatment reaction area,
The weighted BMO spaces reactor from weighted BMO spaces reaction zone is cut out, and the weighted BMO spaces reactor is named as and is cut out
Weighted BMO spaces reactor I, and according to material successively by weighted BMO spaces reaction zone, the weighted BMO spaces reactor that cuts out
I, the sequence in hydrotreating reaction area is by the weighted BMO spaces reactor cut out and weighted BMO spaces reaction zone and hydrotreating
Reaction zone is connected in series to, and the charging of weighted BMO spaces reactor cut out at this time is except what this cut out adds hydrogen
The reaction effluent of weighted BMO spaces reactor except preatreating reactors, when the pressure drop of next weighted BMO spaces reactor
When reaching the 50%~80% of the reactor design pressure drop upper limit, which is cut from weighted BMO spaces reaction zone
Go out, and the weighted BMO spaces reactor that this cuts out is named as to the weighted BMO spaces reactor II cut out, and according to material successively
At weighted BMO spaces reaction zone, the weighted BMO spaces reactor II cut out, the weighted BMO spaces reactor I cut out plus hydrogen
The sequence of reaction zone is managed by weighted BMO spaces reactor II that this cuts out and weighted BMO spaces reaction zone and what is cut out add hydrogen to locate in advance
Reason reactor I is connected in series to, and the charging of weighted BMO spaces reactor II cut out at this time is weighted BMO spaces reaction
The reaction effluent of remaining weighted BMO spaces reactor of the area in addition to the weighted BMO spaces reactor cut out, according to above-mentioned side
Formula, until all weighted BMO spaces reactors are all connected in series to.
2. according to the method for claim 1, it is characterised in that：When First 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 by 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 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 of reactor is managed, when the pressure drop of next weighted BMO spaces reactor reaches the reactor design pressure drop upper limit
When 60%~70%, which from weighted BMO spaces reaction zone is cut out, and hydrogen is added 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, the charging of weighted BMO spaces reactor II cut out at this time is weighted BMO spaces reaction zone except the weighted BMO spaces cut out are anti-
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 process conditions setting and the difference of 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 during each weighted BMO spaces reactor difference to realize using one or more of different Catalyst packing density
The 50%~80% of the reactor pressure decrease design 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 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 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 adds hydrogen to locate 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 adds hydrogen to locate 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, operating pressure and immediate two of volume space velocity plus hydrogen is controlled to locate 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 fraction that the catalytic cracking reaction zone obtains or is obtained including other catalytic cracking units
Catalytic cracking diesel oil fraction.
17. according to the method for claim 1, it is characterised in that：Catalytic cracking into weighted BMO spaces reaction zone follows again
Ring oil distillate is the heavy catalytic cycle oil fraction that the catalytic cracking reaction zone obtains or is filled including other catalytic cracking
The heavy catalytic cycle oil fraction put.
18. 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.
19. according to the method for claim 1, it is characterised in that：It is recycled back to the catalytic cracking weight of weighted BMO spaces reaction zone
Cycle oil fraction enters one or several in the weighted BMO spaces reactor being arranged in parallel.
20. according to the method for claim 1, it is characterised in that：The weighted BMO spaces reaction zone includes two or more simultaneously
Join the weighted BMO spaces reactor of setting.
21. according to the method for claim 20, it is characterised in that：The weighted BMO spaces reaction zone includes 3~6 parallel connections
The weighted BMO spaces reactor of setting.
22. according to the method for claim 21, it is characterised in that：The weighted BMO spaces reaction zone includes 3 or 4 simultaneously
Join the weighted BMO spaces reactor of setting.
23. 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.
24. according to the method described in claims 1 or 23, it is characterised in that：The hydrotreating reaction area includes 1~2
The hydrotreating reactor being arranged in series.
25. according to the method for claim 1, it is characterised in that：The operating condition of the weighted BMO spaces reaction zone is：Instead
Temperature is answered as 370 DEG C~420 DEG C, reaction pressure is 10MPa~25MPa, and hydrogen to oil volume ratio is 300~1500, during raw material fluid
Volume space velocity is 0.15h-1~2.00h-1。
26. according to the method for claim 25, 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, during raw material fluid
Volume space velocity is 0.3h-1~1.00h-1。
27. 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 during raw material fluid
Product air speed is 0.15h-1~0.80h-1。
28. according to the method for claim 27, 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, volume during raw material fluid
Air speed is 0.2h-1~0.60h-1。
29. according to the method for claim 1, it is characterised in that：The residual oil raw material is reduced crude or decompression slag
Oil contains straight-run gas oil, decompressed wax oil, one or more of secondary operation wax oil and FCC recycle oil.
30. according to the method for claim 1, it is characterised in that：The operating condition of the catalytic cracking reaction zone is：Reaction
Temperature be 450~600 DEG C, regeneration temperature be 600~800 DEG C, agent weight of oil than 2~30, with catalyst contact time be 0.1~
15 seconds, pressure was 0.1~0.5MPa.
31. according to the method for claim 1, it is characterised in that：The operating condition of the catalytic cracking reaction zone is：Reaction
Temperature be 480~550 DEG C, regeneration temperature be 650~750 DEG C, agent weight of oil than 4~10, with catalyst contact time be 0.5~
5 seconds, pressure was 0.1~0.5MPa.
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| CN102453530A (en) * | 2010-10-26 | 2012-05-16 | 中国石油化工股份有限公司 | Hydrogenation method for processing heavy oil |
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