CN107177373A - A kind of overcritical residual oil and/or catalytic slurry processing system and processing method - Google Patents
A kind of overcritical residual oil and/or catalytic slurry processing system and processing method Download PDFInfo
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- CN107177373A CN107177373A CN201710266851.4A CN201710266851A CN107177373A CN 107177373 A CN107177373 A CN 107177373A CN 201710266851 A CN201710266851 A CN 201710266851A CN 107177373 A CN107177373 A CN 107177373A
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- extractant
- tower
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- oil
- stripper
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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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1077—Vacuum residues
Abstract
The invention discloses a kind of overcritical residual oil and/or catalytic slurry processing system, the system includes blender, extractant feed pipe, separated from bitumen tower, primary heater, deasphalted oil knockout tower and the first stripper；Present invention also offers the method for carrying out residual oil and/or catalytic slurry processing using upper system.The present invention is extracted under undercritical conditions to residual oil and/or catalytic slurry, then solvent recovery is carried out at supercritical conditions, greatly reduce plant energy consumption, simple flow is operated, improve the online rate and reliability of device, reduction investment and plant area, high-quality charging is provided for downstream process device.
Description
Technical field
The invention belongs to supercritical extraction technique field, more particularly to a kind of overcritical residual oil and/or catalytic slurry processing
System and processing method.
Background technology
Solvent separation process is, with a kind of appropriate solvent treatment liquid or liquid-solid mixture, to be existed using mixture each component
The characteristic of different solubility in solvent, and similar compatibility principle, make component to be separated in mixture be dissolved in solvent, so that
Reach the purpose separated with other components.
Solvent separation process is the important process of a class in oil refining, chemical engineering industry, is widely used in petroleum refining industry.Example
The solvent used such as from residual oil when the solvent deasphalting of acquirement residual lubricating oil raw material and catalytically cracked material, production lubricating oil
Refined Aromatics Extractive Project that aromatic hydrocarbons is extracted with solvent dewaxing, from reformed oil or catalytic cracking recycle oil etc. belongs to solvent point
From process.
In petroleum refining industry, solvent deasphalting process is mainly used for producing thick oil base oil from decompression residuum
And catalytically cracked stock, de-oiled asphalt can be used for production road asphalt in the case of raw material is suitable.Wherein, solvent deasphalting
The main function of process is to remove the pitch in residual oil to obtain the deasphalted oil of relatively low carbon residue and improve color and luster.Split in catalysis
Change an important channel for participating in that decompression residuum is raising yield of light oil in raw material gas oil, but much decompression residuum contain
More metal and the easily material of generation coke, are difficult directly to participate in catalytically cracked material, can be with by solvent deasphalting
Most of metal and easy green coke material are removed, so as to significantly improve the quality of RFCC charging.
Traditional solvent deasphalting process is temperature below the critical point of solvent, operated under pressure condition.
This process uses substantial amounts of solvent, and the solvent of use is than generally 3-5 (mass ratio), it is necessary to reclaims and recycles.Solvent is returned
The investment of receiving portions and operating cost have a major impact to the economic benefit of whole device.Need in recovered solvent amount, about 90%
From extract solution (depitching oil phase), remaining then comes from raffinate (de-oiled asphalt phase).Therefore, the emphasis of solvent recovery is to reclaim
Solvent in extract solution.In recent years, it is overcritical molten to what is operated under the temperature more than the critical point of solvent, pressure condition
The research and technological development that agent extracting and supercritical solvent are reclaimed have larger progress.Relative to conventional solvent depitching skill
Art, supercritical extraction technique there occurs qualitative leap in terms of energy consumption and operating reliability.
The content of the invention
In view of this, it is an object of the invention to provide a kind of overcritical residual oil and/or catalytic slurry processing system, to change
The drawbacks of kind conventional solvent deasphalting techniques high energy consumption, operated by overcritical isolation technics simple flow, improve device
Line rate and reliability, reduction investment and plant area, high-quality charging is provided for downstream process device.
For achieving the above object, the present invention is adopted the following technical scheme that：
A kind of overcritical residual oil and/or catalytic slurry processing system, the system include：
Blender, for the oil plant of pending residual oil and/or catalytic slurry to be mixed with Part I extractant, and
Obtained dilution oil plant is sent into separated from bitumen top of tower；
Extractant feed pipe, the bottom for Part II extractant to be sent into separated from bitumen tower；
Separated from bitumen tower, for making the dilution oil plant and Part II extractant counter current contacting carry out subcritical liquid liquid
Extraction, so as to obtain the extraction phase of deasphalted oil and extractant in tower top, raffinate phase is obtained in bottom of towe；
Primary heater, for making the extraction phase be warming up to more than the critical-temperature of extractant；
Deasphalted oil knockout tower, for making the extractant in the extraction phase from the primary heater in supercritical state
Separated under state with deasphalted oil, and the extractant isolated is drawn from tower top；
First stripper, for being stripped using steam to the bottom of towe separation product from the deasphalted oil knockout tower
Processing, to remove the extractant carried secretly in the bottom of towe separation product, deasphalted oil product is obtained in bottom of towe.
The system according to the present invention, it is preferable that the top of the separated from bitumen tower be provided be used for make it is described dilution oil plant to
Under equally distributed top distributor, bottom, which is provided with, to be used to make the Part II extractant equally distributed bottom point upwards
Cloth device；Being provided between the top distributor and bottom distributor is used to make the dilution oil plant and Part II extraction molten
The filler that agent is fully contacted, so as to greatly increase effect of extracting.
The system according to the present invention, it is preferable that the system also includes：
Secondary heater, for carrying out heat temperature raising to the raffinate phase；
Second stripper, for carrying out stripping processing to the raffinate phase from the secondary heater using steam, with de-
Except the extractant carried secretly in the raffinate phase, de-oiled asphalt is obtained in bottom of towe.
The system according to the present invention, it is preferable that the system also includes：
First Heat Exchanger, for making the extraction phase before primary heater is entered with leaving the deasphalted oil knockout tower
The extractant heat exchange heating of tower top；
Preferably, the system also includes the second heat exchanger, and second heat exchanger is used to make to leave first heat exchange
Deasphalted oil of the extraction phase of device with leaving first stripper before primary heater is entered, which exchanges heat, to heat up.
The system according to the present invention, it is preferable that the system also includes：
First cooler, for cooling down the tower top material from the first stripper and the second stripper and condensing；
Solvent surge tank, for receive the condensation material from first cooler and make it is described condensation material reclaimed water with
Extractant stratification；
Solvent recovery pump, for conveying the extractant in the solvent surge tank.
The system according to the present invention, it is preferable that the system also includes：
First Heat Exchanger, for making the extraction phase before primary heater is entered with leaving the deasphalted oil knockout tower
The extractant heat exchange heating of tower top；
Second cooler, for making the extractant from the First Heat Exchanger further cool；
Solvent circulating pump, for receiving the extractant from the solvent recovery pump and the second cooler, and by part
Extractant sends into the blender as Part I extractant, regard partial extraction solvent as Part II extractant
Send into the separated from bitumen tower.
The system according to the present invention, it is preferable that the system also includes：
First flash tank, first flash tank is arranged between the deasphalted oil knockout tower and the first stripper, is used
In carrying out flash distillation process to the bottom of towe separation product from the deasphalted oil knockout tower, and by the extractant flashed off from tank
Top is taken out, and leftover materials feed to first stripper as stripping, so that the tower from the deasphalted oil knockout tower
Bottom separation product can be conducive to improving later separation effect before the first stripper is entered first through flash distillation process；
Second flash tank, second flash tank is arranged between the separated from bitumen tower and the second stripper, for pair
Raffinate phase from the separated from bitumen tower carries out flash distillation process, and the extractant flashed off is taken out from tank deck, residue
Material feeds to second stripper as stripping, so that the raffinate phase from the separated from bitumen tower is entering the second stripping
It can be conducive to improving later separation effect first through flash distillation process before tower.
The system according to the present invention, it is preferable that the system also includes：
Catalytic slurry oxidizing tower, for being carried out before the catalytic slurry enters the blender to the catalytic slurry
Mild oxidation treatments, so that at least part unsaturated hydrocarbons oxidation saturation in the catalytic slurry.
Skilled in the art realises that, the catalytic slurry is usually obtained by catalytic cracking unit, aromatic hydrocarbons contained therein and
Unsaturated hydrocarbons, due to being also easy to produce condensation reaction, is easily caused the adverse consequences such as coking in extraction process, it is therefore preferable that
Mild oxidation is carried out to it using the catalytic slurry oxidizing tower before the catalytic slurry enters the blender, so that institute
State at least part unsaturated hydrocarbons oxidation saturation in catalytic slurry.Above-mentioned oxidation processes are known in the art, such as profit
With air in oxidizing tower, under 220-280 DEG C, condition of normal pressure by with slurry oil carry out countercurrent flow contact, realize aromatic hydrocarbons
The effect aoxidized with unsaturated hydrocarbons.In further preferred embodiment, the system can also set settling tank, for
The catalytic slurry removes at least part catalyst granules in the catalytic slurry before entering the blender.
Present invention also offers the method for carrying out residual oil and/or catalytic slurry processing using said system.
Method in accordance with the invention it is preferred that the extractant is one or more mixing of the C3 into C6 alkane
Thing；It is further preferred that the extractant be the mixed solvent of C3 alkane and iso-butane, the mixed solvent of C4 alkane or
C4 and C5 alkane mixed solvent.
Method in accordance with the invention it is preferred that the consumption volume ratio of the extractant and oil plant is 6:1-8:1, to dress
Put that to resist Feedstock fluctuation extremely advantageous；It is further preferred that when mixing in a mixer, the Part I extractant and oil
The volume ratio of material is 0.8:1-2:1, such as 1:1 or 1.5:1.
Compared with prior art, the present invention is extracted under undercritical conditions to residual oil and/or catalytic slurry, Ran Hou
Solvent recovery is carried out under super critical condition, plant energy consumption is greatly reduced；Meanwhile, feedstock flexibly (charging of the invention
Can be：Normal slag, subtracts slag, normal slag-subtract slag mixing, the mixed catalytic slurry of ginseng), working ability is big.In addition, by setting heat exchanger, this
Invention being thermally integrated (input and output material heat exchange) with height.In addition, using present invention processing residual oil and/or catalytic slurry, can obtain
High-quality deasphalted oil (low metal and CCR, high hydrogen-carbon ratio), and online rate, more than 95%, the time between overhauls(TBO) is molten up to 10 years
Agent loss is extremely low.
The present invention can join mixed catalytic slurry, only need catalytic slurry settling tank, just can be by the catalyst granules in catalytic slurry
Effectively removed before the device of the present invention is entered, it is to avoid device blocks and produces influence to product quality.
Brief description of the drawings
Fig. 1 is a kind of schematic diagram of embodiment of the system of the present invention.
Embodiment
The present invention is described in detail further below, but the present invention is not limited to this.
The present invention carries out subcritical abstraction using extractant to residual oil and/or catalytic slurry, then in super critical condition
Under extraction phase is separated, with recycling design.The each several part of the system shown in Fig. 1 is illustrated individually below.
1st, feed
The charging oil plant of the processing system can be residual oil and/or catalytic slurry, and wherein residual oil is from crude oil separation
Decompression residuum and/or reduced crude.This is illustrated exemplified by sentencing decompression residuum.Decompression residuum is sent to the battery limit (BL) of the system
Place, and the feeding feed surge tank 3 under Liquid level.The pressure of feed surge tank 3 can be on liquid level sealing gland fuel gas (or nitrogen
Gas) maintain, in tank during superpressure fuel gas emissions to refinery's flare system.Feed pump 4 sucks residual oil from feed surge tank, and adds
Pressure is transported in pre-dilution blender 22.In blender 22, decompression residuum presses such as 1 with Part I solvent:1 or 1.5:1
Normal volume ratio mixed in pre-dilution blender 22, to dilute residual oil, obtain dilute oil plant.By pre-dilution,
The viscosity of the top distributor feedstock solution of separated from bitumen tower 6 can be reduced, the distributed effect of charging, reduction distributor is improved and blocks
Risk.
2nd, separated from bitumen tower
The top of separated from bitumen tower 6, which is provided with, to be used to make the downward equally distributed top distributor of dilution oil plant (in figure not show
Go out), bottom, which is provided with, to be used to make Part II extractant equally distributed bottom distributor (not shown) upwards；The top
Being provided between portion's distributor and bottom distributor is used to make the dilution oil plant and filling out that Part II extractant is fully contacted
Expect (not shown).
Enter the top distributor of separated from bitumen tower 6 via blender 22 through prediluted dilution oil plant.Separated from bitumen tower 6
Disposal ability can be controlled by the flow control valve on the outlet line of feed pump 4.Part II solvent enters via extractant
Expects pipe 23 enters the bottom distributor of separated from bitumen tower 6.
Extractant contacts with each other in SEDA extraction stuffings in a counter-current fashion with dilution oil plant charging.Total solvent amount
The volume ratio of (Part I extractant and Part II extractant) and charging residual oil is such as 6:1 or 8:1 (presses standard body
Product).
Separated from bitumen tower 6 is operated under the undercritical conditions of extractant, carries out subcritical liquid-liquid extraction (such as in 4-
5Mpag, 80-110 DEG C of progress subcritical abstractions), this state helps to be easier to realize the overcritical of solvent in later separation tower
Pitch in state, residual oil is insoluble in a solvent.Pitch spins off from solvent, from pitch under the control of level meters
Flow out the bottom of knockout tower 6.Wherein, the outflow pitch of 1 normal volume, which can be carried secretly, is about slightly below 1 normal volume (such as 0.8 standard
Volume) extractant.Pitch-solvent mixture (raffinate phase) of the bottom of separated from bitumen tower 6 discharge can subsequently enter second
Stripper 15 reclaims the solvent in pitch.
In separated from bitumen tower 6, lighter deasphalted oil can be dissolved in extractant.The overwhelming majority is the deasphalted oil of solvent
The solution (extraction phase) constituted with solvent is discharged from the top of separated from bitumen tower 6.
Operation temperature, solvent composition, solvent-residual oil ratio and the less operating pressure of influence degree in separated from bitumen tower 6
Product yield and quality can be influenceed.Due to some technological parameter (i.e. total solvent-residual oil ratio, solvent composition and operation pressures
Power) it is numerical value that is constant or being set in relative constancy, therefore, during operation, the operation temperature of separated from bitumen tower 6 just becomes master
The Properties Control variable wanted.
What the yield of deasphalted oil can be control effectively by the operation temperature of separated from bitumen tower 6.Higher operation
The deasphalted oil yield that temperature can cause separation column to extract declines.Relatively low operation temperature can improve deasphalted oil yield；
But deasphalted oil inferior quality.Solvent air cooler (the second cooler) 21 can control the tower top temperature of separated from bitumen tower 6, so as to control
The yield of deasphalted oil processed.
High pressure low temperature is conducive to liquid-liquid extraction, and control of the separated from bitumen tower 6 to extraction temperature directly influences deasphalted oil
With the product index of pitch, so separated from bitumen tower 6 be the system ensure product quality visual plant.
3rd, separated from bitumen tower is to deasphalted oil knockout tower
The tower top extraction phase of separated from bitumen tower 6 is first in First Heat Exchanger 7 with leaving the extraction of the tower top of deasphalted oil knockout tower 9
Take solvent heat exchange heating, finally before deasphalted oil knockout tower 9 is entered, (be used as heating to be situated between via deep fat in primary heater 8
Matter) finally it is heated to more than the critical-temperature of extractant, extracted to be reclaimed in deasphalted oil knockout tower 9 in supercriticality
Solvent, wherein, alternatively leave before the laggard primary heater 8 of First Heat Exchanger 7 in the second heat exchanger (not shown)
Deasphalted oil with leaving the first stripper 17, which exchanges heat, to be further heated up.
4th, deasphalted oil knockout tower
It is to utilize the low-density of solvent in the supercritical state that solvent temperature is increased into critical-temperature the above object
Matter.More than critical-temperature, solvent temperature raise when, solvent density is substantially reduced, numerical value close to dense phase gases density so that
Good separating effect can be obtained using density contrast.Under final design temperature, deasphalted oil is actually insoluble in molten
Agent, so as to generate phase separation.In raffinate phase, about 90% solvent can pass through (such as 4- under supercriticality
5Mpag, 100-170 DEG C, such as 120-160 DEG C) phase disengagement method reclaim.
Bottom of towe separation product (the solvent and deasphalted oil product of deasphalted oil product entrainment of deasphalted oil knockout tower 9
1) normal volume ratio is less than extracts out under the control of level meters from the bottom of deasphalted oil knockout tower 9, delivers to the first stripper 17 times
Receive the solvent wherein carried secretly.
5th, solvent circuit is circulated
The supercritical solvent that deasphalted oil knockout tower 9 is reclaimed is used as circulating solvent.Most of heat of circulation solvent exists
It is recycled in First Heat Exchanger 7.Circulation solvent solvent air cooler (the second cooler) 21 further cooling after return with
For Part I extractant and/or Part II extractant.Can be bypassed by adjusting solvent air cooler 21 and (or)
Fan speed controls to eventually enter into the temperature needed for the circulation solvent of separated from bitumen tower 6.It will be appreciated by those skilled in the art that herein
Also it can require to replace air cooler by water cooler according to on-site actual situations or owner, circulation solvent is made by bypass and flow control
Reach required temperature.
6th, deasphalted oil product
The bottom of towe separation product of deasphalted oil knockout tower 9 enters the top tray of the first stripper 17, and its flow is by depitching
The interface liquid level gauge control of oily knockout tower 9.Bottom of towe separation product enters after the first stripper 17, pressure reduction, most of solvent
Come out from flash overhead.
Deasphalted oil is descending in the first stripper 17 to be contacted with water vapour (such as superheated steam), is stripped off residual in product
Remaining solvent, so as to reduce the solvent carried secretly in product.Stripped vapor enters the bottom of the first stripper 17 by flow control
Below portion's column plate.Flow control is more effectively stripped to realize.The temperature of stripped vapor is not lower than the first stripper 17
Operation temperature.Vapor (steam) temperature can cool down deasphalted oil when inadequate, weaken Srteam Stripping effect.Non-overheat steam can cause system to foam
The problem of with tower operating aspect, defoamer can be properly filled into eliminate potential foaming problems.
In one embodiment, the part deasphalted oil product of the bottom of towe of the first stripper 17 under flow control by depitching
Oil pump is delivered to the heat heating that the first stripper heater is provided by deep fat, and returns to first under outlet temperature control
The middle column plate of stripper 17, preferably to maintain the desired bottom of towe operation temperature of the first stripper 17.
Deasphalted oil product is extracted out from the bottom of towe of the first stripper 17, and being pumped into the second heat exchanger through deasphalted oil product leads to
Cross heat exchange cooling deasphalted oil product.If demand, deasphalted oil product further can be cooled down in other heat exchangers.
Deasphalted oil product sends into downstream processing units under flow and the effect of stripper liquid level serials control.
7th, asphaltic products
Alternatively, can be first former with charging by the raffinate phase (mixture of pitch and solvent) from the bottom of separated from bitumen tower 6
Material or product are preheated by heat integration (heat exchange).The raffinate phase enter the second stripper 15 before it is finally heated be by
Deep fat in secondary heater 12 is realized under temperature control.Heating can reduce the viscosity of pitch, can be more effectively carried out molten
Agent flash distillation and product stripping.
Raffinate phase from separated from bitumen tower 6 is sent to the top tray of the second stripper 15, and its flow can be by pitch point
Controlled from the interface liquid level gauge of tower 6.Into after the second stripper 15, pressure is reduced, the most of solvent carried secretly in raffinate phase
Come out from flash overhead.
Pitch is descending in the second stripper 15 to be contacted with each other with water vapour (such as superheated steam), is stripped off in product
Residual solvent, so as to reduce the solvent carried secretly in product.Stripped vapor enters stripper bottom tray by flow control
Below.Flow control is more effectively stripped to realize.The temperature of stripped vapor should be not less than the behaviour of the second stripper 15
Make temperature.Vapor (steam) temperature can cool down deasphalted oil when inadequate, weaken Srteam Stripping effect.Non-overheat steam can cause system to foam and tower
The problem of operating aspect, defoamer can be injected to eliminate potential foaming problems.
In one embodiment, the part de-oiled asphalt (asphaltic products) of the bottom of towe of the second stripper 15 under flow control by
Bitumenpump finally sends the middle column plate of the second stripper 15 back to through the second stripper heater.Heater, which provides enough heats, to be come
Preferably maintain the operation temperature of stripper bottom of towe.
Asphaltic products is extracted out under Liquid level from the bottom of the second stripper 15, and is pumped out by asphaltic products.Asphalt Production
Product can deliver to road asphalt attemperation apparatus, power plant's gasification installation or fuel oil device.
8th, solvent recovery
Enter solvent air cooler (first after solvent and the water vapour mixing of first stripper 17 and the tower top of the second stripper 15
Cooler) 18 cooled down.
The solvent and water of condensation, which enter in solvent surge tank 19, carries out solvent-water separation.The acid that solvent surge tank 19 is discharged
Contain H in water2S.Sour water is extracted out under Liquid level from the liquid collecting bag of the bottom of solvent surge tank 19, is then pumped to by sour water
Sour water processing unit outside battery limit (BL).
Solvent surge tank 19 is provided with the floss hole of fixed gas, and on-condensible gas can be discharged into flare system or its elsewhere of refinery
Manage device.
The solvent being stored in solvent surge tank 1,9 is used for carrying out extracting operation and Stress control.In solvent surge tank 19
Recovered solvent is delivered to the entrance of solvent circulating pump 5 by solvent recovery pump 20.
Recycling design is mixed with the circulation solvent from deasphalted oil knockout tower 9 in the entrance of solvent circulating pump 5.Lead to after mixing
Solvent circulating pump 5 is crossed to boost for use as Part I extractant and/or Part II extractant.
In another embodiment, the system also includes the first flash tank 11 and the second flash tank 13, described first
Flash tank 11 is arranged between the stripper 17 of deasphalted oil knockout tower 9 and first, from the deasphalted oil knockout tower 9
Bottom of towe separation product sends into first flash tank 11 and carries out flash distillation process after being heated through the first flash heater 10, and will flash off
Extractant is sent to the first cooler 18 from tank deck taking-up and cooled down, and tank bottom leftover materials are made after being heated through the first strip heater 16
First stripper 17 is fed to for stripping, so that the bottom of towe separation product from the deasphalted oil knockout tower 9 is being entered
Enter the first stripper 17 before first through flash distillation process, be conducive to improving later separation effect；Second flash tank 13 is arranged on
Between the stripper 15 of separated from bitumen tower 6 and second, the raffinate phase from the separated from bitumen tower 6 is through the second flash heater
The second flash tank 13 is sent into after 12 heating and carries out flash distillation process, and the extractant flashed off takes out to be sent to first cold from tank deck
But device 18 is cooled down, and tank bottom leftover materials feed to second stripper after the heating of the second strip heater 14 as stripping
15, thus the raffinate phase from the separated from bitumen tower 6 enter the second stripper 15 before first through flash distillation process, be conducive to carrying
High later separation effect.
In another embodiment, the system is additionally provided with catalytic slurry oxidizing tower 1, wherein charging oil plant is urged as contained
Carburetion starch, catalytic slurry can first in catalytic slurry oxidizing tower 1 with air contact carry out mild oxidation, gained aoxidize slurry oil with
By in the oxidation feeding feed surge of oil-slurry pump 2 tank 3, mixed with residual oil (when charging oil plant includes residual oil).
Present invention improves the drawbacks of existing conventional solvent deasphalting techniques high energy consumption, simplified by overcritical isolation technics
Flow operations, improve the online rate and reliability of device, reduction investment and plant area.High-quality is provided for downstream process device
Charging, extends downstream unit catalyst life, the profit of refinery is increased dramatically.
Further the present invention will be described with reference to embodiments.
Embodiment 1
Charging residual oil and catalytic slurry property are shown in Table 1；
Extractant is iso-butane.
The overcritical residual oil of the present invention-catalytic slurry processing is carried out in system as shown in Figure 1.Wherein, the catalysis
Slurry oil contacts progress gently first in catalytic slurry oxidizing tower before being mixed into feed surge tank 3 with residual oil with air inversion
Degree is aoxidized, and oxidizing condition is：Normal pressure, 220-280 DEG C；
The volume ratio for diluting extractant and residual oil-catalytic slurry in oil plant is 1:1；Into total extraction of separated from bitumen tower
The volume ratio of solvent and residual oil-catalytic slurry is 8:1；
Wherein, the operating condition of separated from bitumen tower is 4-5Mpag, 80-110 DEG C；The operating condition of deasphalted oil knockout tower
For 4-5Mpag, 120-160 DEG C.
After being handled through said system, gained asphaltic products and deasphalted oil product are shown in Table 1.
Table 1
| Product yield | Feed residual oil-slurry oil | Pitch | Deasphalted oil | |
| Operating mode | ||||
| Yield, wt% | Wt% | 100 | 80 | 20 |
| Lv% | 100 | 77.8 | 22.2 | |
| 15.5 DEG C of proportion@ | 1.033 | 1.0629 | 0.929 | |
| API severes | 5.5 | 1.6 | 20.8 | |
| Nitrogen | Wt% | 0.71 | 0.83 | 0.23 |
| Sulphur | Wt% | 1.71 | 2.0 | 0.43 |
| Kang Shi carbon residues | Wt% | 19.9 | 25 | 1.5 |
| Nickel | wppm | 173.2 | 216 | 3.7 |
| Vanadium | wppm | 310.5 | 388 | 0.7 |
| Viscosity： | ||||
| @100℃ | cSt | 51621 | 1747000 | 77 |
| @135℃ | cSt | 1868 | 21540 | 20 |
| @180℃ | cSt | 169 | 899.3 | - |
| @205℃ | cSt | - | - | |
| Ring and ball softening point | ℃ | - | 102 | - |
| Pitch | wppm | - | - | <100 |
The deasphalted oil of the present embodiment is fed as downstream hydrogenation processing unit, and pitch is fed for gasification installation, used
Solvent is iso-butane (iC4).It can be seen that, using the SEDA technologies of the present invention, can significantly reduce Kang Shi carbon residues in deasphalted oil and
The content of metallic nickel, vanadium, greatly increases the quality of deasphalted oil, while also making the ring and ball softening point of asphaltic products and gluing
Degree meets the requirement of downstream unit.
Embodiment 2
Charging residual oil property is shown in Table 2；
Extractant is mixed butanes (50%iC4,50%nC4).
The overcritical residual oil of the present invention is handled to be carried out in system as shown in Figure 1.Wherein, extractant in dilution oil plant
Volume ratio with residual oil is 1.5:1；The volume ratio of total extractant and residual oil into separated from bitumen tower is 6:1；
Wherein, the operating condition of separated from bitumen tower is 4-5Mpag, 80-110 DEG C；The operating condition of deasphalted oil knockout tower
For 4-5Mpag, 120-160 DEG C.
After being handled through said system, gained asphaltic products and deasphalted oil product are shown in Table 2.
Table 2
The deasphalted oil of the present embodiment is fed as downstream lube plant, produces thick oil, and pitch is used for gas
Change stove charging, solvent for use is mixed butanes (50%iC4,50%nC4).It can be seen that, can be notable using the SEDA technologies of the present invention
The Kang Shi carbon residues and metallic nickel, the content of vanadium in deasphalted oil are reduced, the quality of deasphalted oil is greatly increased, it is high-quality
Charging can be improved the life-span of downstream unit catalyst, improve the online rate of downstream unit.
Claims (10)
1. a kind of overcritical residual oil and/or catalytic slurry processing system, the system include：
Blender, for the oil plant of pending residual oil and/or catalytic slurry to be mixed with Part I extractant, and will
The dilution oil plant feeding separated from bitumen top of tower arrived；
Extractant feed pipe, the bottom for Part II extractant to be sent into separated from bitumen tower；
Separated from bitumen tower, extracts for making the dilution oil plant and Part II extractant counter current contacting carry out subcritical liquid liquid
Take, so as to obtain the extraction phase of deasphalted oil and extractant in tower top, raffinate phase is obtained in bottom of towe；
Primary heater, for making the extraction phase be warming up to more than the critical-temperature of extractant；
Deasphalted oil knockout tower, for making the extractant in the extraction phase from the primary heater in the supercritical state
Separated with deasphalted oil, and the extractant isolated is drawn from tower top；
First stripper, for using steam to from the bottom of towe separation product of the deasphalted oil knockout tower carry out stripping at
Reason, to remove the extractant carried secretly in the bottom of towe separation product, deasphalted oil product is obtained in bottom of towe.
2. system according to claim 1, it is characterised in that the system also includes：
Secondary heater, for carrying out heat temperature raising to the raffinate phase；
Second stripper, for carrying out stripping processing to the raffinate phase from the secondary heater using steam, to remove
The extractant carried secretly in raffinate phase is stated, de-oiled asphalt is obtained in bottom of towe.
3. system according to claim 1, it is characterised in that the top of the separated from bitumen tower is provided with described dilute for making
Oil plant equally distributed top distributor downwards is released, bottom, which is provided with, to be used to make the Part II extractant be uniformly distributed upwards
Bottom distributor；Being provided between the top distributor and bottom distributor is used to make the dilution oil plant and described second
The filler for dividing extractant fully to contact.
4. the system according to any one of claim 1-3, it is characterised in that the system also includes：
First Heat Exchanger, for making the extraction phase separate column overhead with leaving the deasphalted oil before entrance primary heater
Extractant heat exchange heating；
Preferably, the system also includes the second heat exchanger, and second heat exchanger is used to make to leave the First Heat Exchanger
Deasphalted oil of the extraction phase with leaving first stripper before primary heater is entered, which exchanges heat, to heat up.
5. the system according to any one of claim 1-3, it is characterised in that the system also includes：
First cooler, for cooling down the tower top material from the first stripper and the second stripper and condensing；
Solvent surge tank, for receiving the condensation material from first cooler and making the condensation material reclaimed water and extraction
Solvent stratification；
Solvent recovery pump, for conveying the extractant in the solvent surge tank.
6. system according to claim 5, it is characterised in that the system also includes：
First Heat Exchanger, for making the extraction phase separate column overhead with leaving the deasphalted oil before entrance primary heater
Extractant heat exchange heating；
Second cooler, for making the extractant from the First Heat Exchanger further cool；
Solvent circulating pump, for receiving the extractant from the solvent recovery pump and the second cooler, and by partial extraction
Solvent is sent into the blender as Part I extractant, sent into partial extraction solvent as Part II extractant
The separated from bitumen tower.
7. system according to claim 2, it is characterised in that the system also includes：
First flash tank, first flash tank is arranged between the deasphalted oil knockout tower and the first stripper, for pair
Bottom of towe separation product from the deasphalted oil knockout tower carries out flash distillation process, and the extractant flashed off is taken from tank deck
Go out, leftover materials feed to first stripper as stripping；
Second flash tank, second flash tank is arranged between the separated from bitumen tower and the second stripper, for from
The raffinate phase of the separated from bitumen tower carries out flash distillation process, and the extractant flashed off is taken out from tank deck, and leftover materials are made
Second stripper is fed to for stripping.
8. the system according to any one of claim 1-7, it is characterised in that the system also includes：
Catalytic slurry oxidizing tower, it is slight for being carried out before the catalytic slurry enters the blender to the catalytic slurry
Oxidation processes, so that at least part unsaturated hydrocarbons oxidation saturation in the catalytic slurry.
9. a kind of system using according to any one of claim 1-8 carries out the side of residual oil and/or catalytic slurry processing
Method.
10. method according to claim 9, it is characterised in that the extractant be one kind into C6 alkane of C3 or
A variety of mixtures；Preferably, the extractant be the mixed solvent of C3 alkane and iso-butane, the mixed solvent of C4 alkane,
Or C4 and C5 alkane mixed solvent；
It is further preferred that the consumption volume ratio of the extractant and oil plant is 6:1-8:1.
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