CN107653005A - Decompression distillation system and vacuum distillation deep drawing technique - Google Patents
Decompression distillation system and vacuum distillation deep drawing technique Download PDFInfo
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- CN107653005A CN107653005A CN201610594753.9A CN201610594753A CN107653005A CN 107653005 A CN107653005 A CN 107653005A CN 201610594753 A CN201610594753 A CN 201610594753A CN 107653005 A CN107653005 A CN 107653005A
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/10—Vacuum distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
-
- 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
- C10G2300/1033—Oil well production fluids
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/06—Gasoil
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention provides a kind of decompression distillation system and it is evaporated under reduced pressure deep drawing technique.The decompression distillation system includes：Vacuum distillation apparatus and stirred reactor, vacuum distillation apparatus include tower reactor section, condensation segment and the decompressor set gradually along gas flow direction, and condensation segment exports including fixed gas；Stirred reactor is connected with tower reactor section, for being stirred to the material in tower reactor section and material being returned into tower reactor section；Wherein, condensation segment passes sequentially through fixed gas outlet and decompressor is connected with stirred reactor.The airflow balance of the system operation, vacustat, both discharged without waste gas, and eliminated the device of processing waste gas, and reduced cost of investment；Liquid-phase product is added again, improves extracting rate.
Description
Technical field
The present invention relates to petroleum refining field, in particular to a kind of decompression distillation system and is evaporated under reduced pressure deep drawing work
Skill.
Background technology
Atmospheric vacuum rectifying column is the core apparatus of oil plant, is the key equipment of leading oil plant economic benefit.With original
Oily heaviness, in poor quality and shale oil, tar sand oil, (thick) oil, extra heavy oil, deep petroleum and pitch, coal tar etc. are non-again
The conventional bad oily a large amount of productions of heavy, the product yield of atmospheric distillation tower will be forced to be gradually reduced, thus, refine improving or keeping
For oily Business Economic Benefit, vacuum rectification tower will play more importantly role.
All the output with Improvement vacuum rectification tower is being paid close attention to about the research institution and refinery that refine oil in countries in the world
Benefit.The index of evaluation vacuum rectification tower quantum of output is referred to as the extracting rate of vacuum rectification tower,
Vacuum rectification tower extracting rate=1-(the decompression residuum total amount of bottom of towe discharge/enter the normal pressure base oil of vacuum rectification tower
Total amount).
In general, the extracting rate of vacuum rectification tower depends on property, the structure of vacuum rectification tower of crude oil and normal base oil
And its technological parameter etc..On the premise of the first two factor is constant, the extracting rate of vacuum rectification tower is dependent on to its own
The improvement of structure and technique.Chinese invention patent CN1194070C, a kind of oil Atmospheric vacuum technique is disclosed, subtracted with increase is a set of
The mode of stove and vacuum rectification tower is pressed to improve dial-out rate, effect is preferable, and equipment investment is high, conjunction economically although extracting
Rationality needs to be proved.Chinese patent application CN101376068A, it is proposed that by Atmospheric vacuum system " the two-furnace three-tower " (flash distillation of routine
Tower → atmospheric pressure kiln → atmospheric tower → vacuum furnace → vacuum rectification tower) change into " tower of two stove four ", i.e., atmospheric tower and vacuum furnace it
Between set up a flash column, so as to mitigate the load of vacuum rectification tower, light oil extracting rate increases.The patent is for decompression
Existing refinery's technological transformation of rectifying column overload, there is certain reference value, but nonsensical for grassroot refinery.It is moreover, new
Increase a flash column, into follow-up vacuum furnace material temperature will step-down, so as to add the burden of vacuum furnace, and newly-increased
Equipment reduces the benefit for causing system.
Chinese patent application CN103242885A, it is proposed that increase by three flash vaporization kettles between vacuum furnace and vacuum rectification tower
With two pot arches, furnace temperature causes flash temperature to reach 420 DEG C and using superheated steam, high temperature nitrogen or high-temperature hydrogen to normal pressure
Residual oil is stripped.Increase of this method to vacuum tower extracting rate is effective certainly.The problem of patent is present is to increase
There is the component that rotating speed is up to 600 revs/min in three each kettles of flash vaporization kettle, to the flash vaporization kettle of 550T/ hours, its diameter should be
More than 2m, the power of motor of rotary evaporation can be up to more than 200kw, so the investment of flash vaporization kettle can be at a relatively high, three flash vaporization kettles
Between also have two pot arches, along with for steam stripped high-temperature gas, investment can increase a lot.
Chinese patent application CN1884441A discloses the method for improving light oil yield of atmospheric and vacuum distillation of petroleum oil, will contain rosin
Additive be added in the crude oil of atmospheric and vacuum distillation of petroleum tower, by change the intermolecular active force of crude oil improve Atmospheric vacuum steam
The light oil yield evaporated.But this method adds oil refining process using biomass, has suitable novelty, but not basic in technique
Upper change distillation technique.
The technology for improving vacuum rectification tower extracting rate is referred to as deep drawing technology.The main path of existing deep drawing technology has three, one
It is to improve vacuum rectification tower feeding temperature, second, the oil gas partial pressure of product in tower is reduced, third, improving the vacuum of vacuum rectification tower
Degree.In general, under deep drawing technique, vacuum rectification tower feeding temperature needs raising 5%~8%, and feeding temperature is higher, extracts
Rate is also higher, but too high feeding temperature can cause material coking and the more cracking fixed gases of generation in tower, have a strong impact on
The normal operation of vacuum rectification tower.For reducing oil gas partial pressure, the method for current trend is to be passed through vapor to reduce decompression
Oil gas partial pressure in rectifying column, vapor is more, and oil gas partial pressure is also lower.But the wet type rectification under vacuum of a large amount of steam is used at present
Tower is gradually eliminated, because in wet type vacuum rectification tower, the large quantity of moisture steam more light than wax oil quality is crowded
In tower, about 90% space is occupied, considerably increases the load of vacuum rectification tower, reduces and extracts efficiency, and is produced many
Waste water to be processed is needed, thus injects tower bottom steam amount and is also limited by efficiency and environmental protection.
Because preceding two measures are by suitable constraint, what deep drawing technology was paid close attention to the most is exactly improve vacuum rectification tower true
Reciprocal of duty cycle.Real process conditions of the boiling cut point (TBP) higher than 565.60 DEG C are referred to as deep drawing technique, state by the oil company of foreign well-known
It is interior due to the limitation of equipment and technology, the real boiling cutting of deep drawing technique is typically at 540 DEG C or so.
In summary, under the conditions of existing process, the most important constraint of rectification under vacuum is to make material in vacuum rectification tower
Only undergo the physical process of a distillation phase inversion and there can not be any chemical process.It is entitled《Vacuum rectifying apparatus and its
Rectificating method》Chinese patent application CN201510498467.8, it is proposed that a kind of improvement of tower structure, by condenser, again boil
Device is integrated in tower bottom, reduces investment and energy-conservation, and the conception of the patent is worth recommending, but be not related to distillation general principle and
Constraint.For current process conditions, this constraint is necessary, because under conditions of without external hydrogen source, residual oil splits
Solution will cause further to be condensed, and material is become heavier, be unfavorable for follow-up coking process.Therefore, existing vacuum rectification tower
In operation, there is strict limitation residence time of the material in rectification under vacuum tower reactor, and decompression residuum once leaves decompression essence
Tower is evaporated, is required for adding quench oil and reducing subtracting slag temperature, avoids cracking.Therefore, existing rectification under vacuum deep drawing technique stills need
Improve.
The content of the invention
It is a primary object of the present invention to provide a kind of decompression distillation system and rectification under vacuum deep drawing technique, further to carry
The extracting rate of high rectification under vacuum in the prior art.
To achieve these goals, according to an aspect of the invention, there is provided a kind of decompression distillation system, the decompression are steamed
The system of evaporating includes：Vacuum distillation apparatus and stirred reactor, vacuum distillation apparatus include what is set gradually along gas flow direction
Tower reactor section, condensation segment and decompressor, condensation segment export including fixed gas；Stirred reactor is connected with tower reactor section, is used for
Material in tower reactor section is stirred and material is returned into tower reactor section；Wherein, condensation segment passes sequentially through fixed gas outlet and subtracted
Pressure device is connected with stirred reactor.
Further, tower reactor section includes flash vaporization kettle, and flash vaporization kettle includes gaseous phase outlet, recycle stock entrance and recycle stock
Outlet, gaseous phase outlet are connected with condensation segment, and stirred reactor is respectively by recycle stock outlet and recycle stock entrance with dodging
Kettle is steamed to connect to form material circulation loop.
Further, flash vaporization kettle is provided with gas phase entrainment block piece at gaseous phase outlet.
Further, gas phase entrainment block piece include along flash vaporization kettle inwall it is circumferentially disposed annular boiling liquid baffle plate with
And the annular stop umbrella boiled above liquid baffle plate is arranged on along the axial direction of flash vaporization kettle, annular boiling liquid baffle plate has centre bore, hindered
Gear umbrella is connected and positioned at the top of centre bore with annular boiling liquid baffle plate.
Further, condensation segment includes rectifying column, and rectifying column includes packed tower, structured packing is filled with packed tower.
Further, decompressor is vavuum pump.
Further, stirred reactor includes：Stirred reactor body, conduit is sucked, suck in conduit and be provided with extraction
Portion, the one end for sucking conduit are stretched into inside flash vaporization kettle by recycle stock outlet, suck the other end and stirred reactor of conduit
Body is connected, and sucking conduit extracts the material in flash vaporization kettle and material is delivered in stirred reactor body and is stirred instead
Should, flash vaporization kettle is returned to by recycle stock entrance after material is agitated.
Further, stirred reactor also includes driving agitating element, drives one end of agitating element to sequentially pass through stirring
Reactor body and sucking conduit are simultaneously stretched into inside flash vaporization kettle, drive the other end of agitating element to be connected with drive device.
Further, driving agitating element includes stirring shaft and the first agitating paddle, and one end of stirring shaft is successively
Through stirred reactor body and sucking conduit and stretch into inside flash vaporization kettle, the other end of stirring shaft is connected with drive device
It is logical；First agitating paddle is arranged on one end that stirring shaft is stretched into inside flash vaporization kettle, the length of the first agitating paddle and flash vaporization kettle
The ratio between internal diameter is 0.1~0.3:1.
Further, extracting part includes promoting blade, promotes blade to be arranged on stirring shaft and positioned at sucking conduit
It is interior.
Further, the second agitating paddle is provided with stirred reactor body, the second agitating paddle drives with stirring shaft
Connection.
Further, there are one or more groups of blades on the second agitating paddle, blade be arranged in parallel with stirring shaft.
Further, the ratio between internal diameter of the blade length of the second agitating paddle and flash vaporization kettle is 0.6~1.2:1.
Further, the speed of agitator of the second agitating paddle is 0~1500r/min continuously adjustabes.
Further, stirred reactor also includes stirring material outlet, and the one end and recycle stock for stirring material outlet enter
Mouth is connected, and the other end passes through the kettle wall of flash vaporization kettle and the intracavity inter-connection of flash vaporization kettle.
Further, decompression distillation system also includes fixed gas surge tank, and along gas flow direction, decompressor passes through not
Solidifying gas surge tank is connected with stirred reactor.
Further, catalyst inlet is additionally provided with stirred reactor.
To achieve these goals, according to an aspect of the invention, there is provided a kind of be evaporated under reduced pressure deep drawing technique, the depth
Technique is pulled out to carry out being evaporated under reduced pressure processing including the normal pressure base oil from vacuum furnace is inputted into any of the above-described kind of decompression distillation system
Step, wherein, being evaporated under reduced pressure the step of handling includes：The tower reactor section of normal pressure base oil input vacuum distillation apparatus is subjected to decompression steaming
Send out to obtain gaseous phase materials and liquid phase material；Condensation segment of the gaseous phase materials through vacuum distillation apparatus carries out distillation processing, is steamed
Evaporate product and fixed gas；Fixed gas is passed through stirred reactor and with the liquid phase material from tower reactor section mix instead
Should, obtain mixed material；Mixed material return tower reactor section is evaporated under reduced pressure；Wherein, the step with distillation processing is evaporated under reduced pressure
Suddenly carried out under the depressurization of decompressor.
Further, the temperature of normal pressure base oil is 320 DEG C~380 DEG C.
Further, be evaporated under reduced pressure with distillation handle the step of in decompressor outlet pressure for 10kPa~
40kPa。
Further, be evaporated under reduced pressure the step of in, residence time of the normal pressure base oil in tower reactor section be 30min~
90min。
Further, stirred reactor is 1min~5min to the stirring reaction time of fixed gas and liquid phase material.
Apply the technical scheme of the present invention, by the way that stirred reactor is connected with vacuum distillation apparatus, make caused by not
Solidifying gas is fully incorporated stirred reactor, and the material with being sucked out of tower reactor section is sufficiently mixed stirring, in stirring and the work of catalyst
Under, by the chemical reaction of complexity and the oil gas partial pressure of change evaporation process, not only it is broken the macromolecule hydro carbons in material
Turn into stable saturated hydrocarbons for small molecule hydro carbons and in the presence of hydrogen is mended, and make part fixed gas condensation be liquid form product group
Dividing and return in tower reactor section, the fixed gas of the oil product of lighting and non-liquefied is discharged from the tower reactor section of vacuum distillation apparatus, and then
Change the oil gas partial pressure of still-process, finally make the airflow balance of system operation, vacustat, both discharged without waste gas, saved
The device of processing waste gas has been removed, has reduced cost of investment；Liquid-phase product is added again, improves extracting rate.
Brief description of the drawings
The Figure of description for forming the part of the application is used for providing a further understanding of the present invention, and of the invention shows
Meaning property embodiment and its illustrate be used for explain the present invention, do not form inappropriate limitation of the present invention.In the accompanying drawings：
Fig. 1 shows the process flow diagram of the decompression distillation system in a kind of preferred embodiment of the present invention；
Fig. 2 shows the structural representation of the flash vaporization kettle in a kind of preferred embodiment of the present invention；
Fig. 3 shows the schematic top plan view in the A-A faces of annular boiling liquid baffle plate in Fig. 2；And
Fig. 4 shows the structural representation of the stirred reactor in a kind of preferred embodiment of the present invention.
Wherein, above-mentioned accompanying drawing marks including the following drawings：
10th, vacuum distillation apparatus；11st, tower reactor section；12nd, condensation segment；13rd, decompressor；121st, fixed gas exports；
110th, flash vaporization kettle；111st, gaseous phase outlet；112nd, recycle stock entrance；113rd, recycle stock exports；114th, gas phase mist
Foam carries block piece secretly；1141st, annular boiling liquid baffle plate；1142nd, umbrella is stopped；
20th, stirred reactor；21st, conduit is sucked；22nd, stirred reactor body；23rd, stirring shaft；24th, the first stirring
Oar；211st, blade is promoted；221st, the second agitating paddle；222nd, blade；25th, material outlet is stirred；26th, catalyst inlet；
30th, fixed gas surge tank.
Embodiment
It should be noted that in the case where not conflicting, the feature in embodiment and embodiment in the application can phase
Mutually combination.The present invention is described in detail below in conjunction with embodiment.
It should be noted that the length of the first agitating paddle and the second agitating paddle is referred to respectively to drive agitating shaft in the application
Center line be boundary, the length sum of the blade at its both ends.In the application, with the tower reactor section or flash vaporization kettle of vacuum distillation apparatus
A diameter of D calculate, then the length of the first agitating paddle is 0.1D~0.3D；The length of second agitating paddle is 0.6D~1.2D.
As background section is previously mentioned, otherwise transformation presence equipment investment of the prior art to decompression distillation system
It is high, less economical, otherwise deep drawing rate improves the defects of limited.In order to improve this situation, in a kind of typical implementation of the application
In mode, there is provided a kind of decompression distillation system, as shown in figure 1, the decompression distillation system includes：Vacuum distillation apparatus 10, bag
The tower reactor section 11 set gradually along gas current method, condensation segment 12 and decompressor 13 are included, wherein, condensation segment 12 is included not
Solidifying gas outlet 121；Stirred reactor 20, stirred reactor 20 are connected with tower reactor section 11, for the material in tower reactor section 11
It is stirred and material is returned into tower reactor section 11；Wherein, condensation segment 12 pass sequentially through fixed gas outlet 121 and decompressor 13 with
Stirred reactor 20 is connected.
Above-mentioned decompression distillation system, by the way that stirred reactor is connected with vacuum distillation apparatus, make vacuum distillation apparatus
In caused fixed gas (product such as hydrogen, carbon monoxide, carbon dioxide, methane, ethane, ethene and water vapour during main component)
Stirred reactor is fully incorporated, the material with being sucked out of tower reactor section is sufficiently mixed stirring, in the presence of stirring reaction, changes
The oil gas partial pressure of evaporation process causes part fixed gas condensation to be returned for liquid form product component in tower reactor section, and part fixed gas is still
So discharged from the tower reactor section of vacuum distillation apparatus, and then change the oil gas partial pressure of still-process, finally make the tolerance of system operation
Balance, vacustat, no waste gas is discharged from system and liquid-phase product increased, so as to improve extracting rate.
In above-mentioned decompression distillation system, tower reactor section 11 can select the tower reactor of proper volume according to material handling capacity, such as,
Existing tower reactor can be used if the tower reactor volume of existing vacuum tower disclosure satisfy that treating capacity.It is a kind of preferable real in the application
Apply in example, as depicted in figs. 1 and 2, above-mentioned tower reactor section 11 includes flash vaporization kettle 110, and flash vaporization kettle 110 includes gaseous phase outlet 111, circulation
Material inlet 112 and recycle stock outlet 113, gaseous phase outlet 111 is connected with condensation segment 12, and stirred reactor 20 leads to respectively
Cross recycle stock outlet 113 and recycle stock entrance 112 connects to form material circulation loop with flash vaporization kettle 110.
Above-mentioned tower reactor section 11 is provided with flash vaporization kettle 110 so that normal pressure base oil or agitated reaction into flash vaporization kettle
The material that device 20 is returned from recycle stock entrance 112 carries out gas-liquid separator, so as to by light-end products from the row of gaseous phase outlet 111
Go out, condensation separation is carried out into condensation segment 12.Not only mitigate the load of condensation segment, and can make normal pressure base oil enters material temperature
In the case that the feeding temperature spent than existing deep drawing rectifying column reduces by 30~50 DEG C, extracting rate is improved.
Condensation segment in above-mentioned vacuum distillation apparatus according to according to actual conditions selection rectifying column or with condenser,
Cut need not be such as precisely separated in petroleum refining industry, or petrol and diesel oil ratio is less in cut, it is when rectifying has little significance, then general to use
Condenser substitutes.Following judgement can be done from the pilot scale stage of the present invention：If from initial boiling point to 205 DEG C of gasoline section institute accounting
The 15% of Li≤steamed food material, petrol and diesel oil Suo accounting Li≤40%, petrol and diesel oil is directly distillated using rectifying column, rest materials enter
FCC crackings, it is reasonably to select；If being unsatisfactory for above-mentioned condition, distillation condensation gained light oil and refinery's vacuum distillation apparatus
The line that subtracts 2 or subtract 3 line distillate oil be identical, then need not build rectifying column, condensable product is directly entered FCC or is hydrocracked, from skill
Art economic angle com-parison and analysis is reasonable.
In a kind of preferred embodiment of the application, as shown in Fig. 2 above-mentioned flash vaporization kettle 110 is set at gaseous phase outlet 111
There is gas phase entrainment block piece 114, be advantageous to remove mist, reduce inclusion rates of the gas phase oil product to heavy oil product.For mist
Filtering off except can have a variety of implementations, such as using screen pack for foam, it is any in the prior art to realize the function
Part is suitable for the application.
In the application another kind preferred embodiment, as shown in Figures 2 and 3, the gas phase entrainment block piece 114 wraps
Include along the circumferentially disposed annular boiling liquid baffle plate 1141 of the inwall of flash vaporization kettle 110 and be arranged on along the axial direction of flash vaporization kettle 110
The stop umbrella 1142 of the top of annular boiling liquid baffle plate 1141, annular boiling liquid baffle plate 1141 have centre bore, stop umbrella 1142 and annular
Liquid baffle plate 1141 is boiled to be connected and positioned at the top of centre bore.
In above-mentioned preferred embodiment, annular boiling liquid baffle plate 1141 is annular hollow baffle plate, can be blocked along wall flowing
Liquid, and gas therefrom overflow by vacancy.Stop that the area of umbrella 1142 is slightly larger than the area of ring baffle hollow space, liquid and bubble
Foam is blocked umbrella 1142 and blocked, and gas can rise from side around the edge of umbrella.The ring baffle of annular boiling liquid baffle plate 1141
Part can prevent from turning on most of liquid phase oil product and by gas phase being mingled with into rectifying column, and when a small amount of liquid phase oil product is in gas phase
Under the entrainment of oil product after the centre bore of annular boiling liquid baffle plate 1141 passes through, run into during continuing to rise centrally disposed
Stop umbrella 1142 above hole and be blocked, it is achieved thereby that being carried out to mist caused by heavy oil product or gas phase oil product
Filter and stop.
In above-mentioned decompression distillation system, condensation segment 12 carries out rectifying using existing rectifying tower tray, passes through evaporation point
The gas separated out enters in the rectifying column of condensation segment, different liquid-phase products by rectifying column side take-off, in tower reactor section 11 not
The liquid phase decompression residuum that can be evaporated is discharged from the bottom of tower reactor section 11, into subsequent technique.In order to further improve rectifying effect
Fruit, in a kind of preferred embodiment of the application, above-mentioned condensation segment 12 includes packed tower, and structured packing is filled with packed tower,
Structured packing has the advantages that specific surface area is big, pressure drop is small, fluid point is uniform, mass-and heat-transfer efficiency high, and rectification effect is good.Herein
Particular/special requirement is had no to the specific species of structured packing, using known conventional structured packing.Conventional structured packing
Include but are not limited to corrugated plate regular packing, folding peak formula structured packing or MELLAPAK fillers etc..
Decompressor 13 in above-mentioned decompression distillation system uses conventional vavuum pump, it is possible to use others are improved
Device, as long as the decompressor that can be depressured to tower reactor section and condensation segment is suitable for the application, preferred liquid in the application
Ring vacuum pump, waste liquid is not produced, be more conducive to environmental protection.
In actual extensive heavy oil hydroprocessing process production, according to the size of the specific kettle volume of tower reactor section 11, such as
When tower reactor is flash vaporization kettle, volume reaches tens cubes of even cubic inches up to a hundred, and mixing plant is installed additional hardly in flash vaporization kettle
May.Thus, in this application, preferably set up around tower reactor section 11 one or the less stirred reactor 20 of several capacity with
Meet the requirement of mass transfer and chemical reaction.
In above-mentioned decompression distillation system, as long as stirred reactor 20 can be realized to the material and condensation segment in tower reactor section 11
Caused fixed gas is partially converted into light-end products in the presence of stirring and catalyst in 12 or fluid oil loops back,
The airflow balance of system operation and the liquid-phase product of increase system discharge are easy to implement, improves extracting rate.In the prior art,
The petroleum pipeline that the normal temperature base oil being heated is conveyed between vacuum furnace to vacuum distillation apparatus is often referred to as oil transfer line.In oil transfer line
Material liquid phase is simultaneously deposited and is in high temperature, to make oil transfer line have minimum resistance loss and its making of thermal losses quite tired
Difficulty, thus, oil transfer line turns into the vacuum distillation apparatus component with high cost and high technology content, also has many patents to surround and turns
Oily line is improved.In this application, the connection between stirred reactor 20 and flash vaporization kettle 110 can both use existing turn of oil
Line is attached, and the oil transfer line after improving can also be used to be attached.The number of lines specifically needed is according to stirred reactor
20 number is determined.
In a kind of preferred embodiment of the application, as shown in figure 4, above-mentioned stirred reactor 20 includes：Stirred reactor
Body 22, conduit 21 is sucked, suck and extracting part is provided with conduit 21, the one end for sucking conduit 21 is exported by recycle stock
113 stretch into inside flash vaporization kettle 110, and the other end for sucking conduit 21 is connected with stirred reactor body 22, suck conduit 21 and take out
Take the material in flash vaporization kettle 110 and material is delivered in stirred reactor body 22 and be stirred reaction, after material is agitated
Flash vaporization kettle 110 is returned to by recycle stock entrance 112.
In above-mentioned preferred embodiment, sucking inside flash vaporization kettle 110 is stretched into by the way that stirred reactor 20 to be arranged to include
The form that conduit 21 is connected with the stirred reactor 20 being arranged on outside flash vaporization kettle is inhaled, the extracting part sucked in conduit 21 can be right
Material in flash vaporization kettle 110 is extracted, and is then entered by recycle stock outlet 113 by stirred reactor 20, and pass through
Recycle stock entrance 112 returns to flash vaporization kettle 110, and this set form is easy to tightly adsorb stirred reactor 20 in flash vaporization kettle
In 110 tower reactor, a kind of outer circulation type sucking response device is formed, the stirring and reaction of convention stir reactor can not only be realized
Effect, and the setting of oil transfer line is also reduced, reduce cost of investment.
Inside above-mentioned stirred reactor 20 set component according to suck sucking of the conduit 21 to material in flash vaporization kettle 110 and
Conveying function is configured, and specific setting form can have a variety of patterns, can rationally be set according to being actually needed.At this
Apply in a kind of preferred embodiment, in addition to driving agitating element, one end of the driving agitating element sequentially pass through stirring instead
Answer device body 22 and suck conduit 21 and stretch into inside flash vaporization kettle 110, drive the other end of agitating element to be connected with drive device
It is logical.
In the application another kind preferred embodiment, as shown in figure 4, above-mentioned driving agitating element includes stirring shaft
23 and first agitating paddle 24, one end of stirring shaft 23 sequentially pass through stirred reactor body 22 and suck conduit 21 and stretch into
Inside flash vaporization kettle 110, the other end of stirring shaft 23 is connected with drive device, and the first agitating paddle 24 is arranged on stirring driving
One end that axle 23 is stretched into inside flash vaporization kettle 110.Preferably, the ratio between the length of the first agitating paddle 24 and internal diameter of flash vaporization kettle 110 are
0.1~0.3:1.For a 2M3Flash vaporization kettle for the blade length of the first agitating paddle 24 be 100~150mm.Pass through setting
The first agitating paddle 24 stretched into inside flash vaporization kettle 110 so that the material in flash vaporization kettle 110 is constantly in the state being stirred, more
Beneficial to efficiently separating for gas-liquid phase materials.For above-mentioned flash vaporization kettle, if the blade length of the first agitating paddle 24 be arranged to
30~50mm so that the agitating paddle belongs to miniature agitating paddle relative to flash vaporization kettle 110, and the stirring to material in tower reactor belongs to slight
Mixing, avoid the decomposition and condensation reaction for causing material.
The extracting part in sucking conduit 21 in above preferred embodiment is in order to which the material suction in flash vaporization kettle 110 is stirred
Mix in reactor body 22, thus, any specific constructive form that can realize the function is suitable for the application.In the application
In a kind of preferred embodiment, the mode that above-mentioned sucking conduit 21 sucks material is the process that simulated hexapod is sucked blood, and sucking is led
Pipe 21 is inserted in flash vaporization kettle 110, sucking the extracting part in conduit 21 to promote blade 211, promotes the action principle of blade 211
The principle of centrifugal pump or electric fan is the same, the certain angle of blade twist, has impetus to liquid (or gas) during rotation.It will push away
Movable vane piece 211 is provided through on the stirring shaft 23 for sucking conduit 21, the material in tower reactor can be sucked into stirring reaction
In device body 22.
Stirred reactor body 22 in above preferred embodiment is a sucking response kettle with strong stirring function,
The second agitating paddle 221 is provided with stirred reactor body 22, the second agitating paddle 221 is connected with stirring shaft 23, and second stirs
Mix oar 221 and the drive connection of stirring shaft 23.It is highly preferred that have on the second agitating paddle 221 one or more groups of with stirring driving
The blade 222 that axle 23 be arranged in parallel.
Above-mentioned stirred reactor body 22 is easy to the thing that will be sucked conduit 21 and input by setting the agitating paddle of said structure
Material is sheared, stirred, and chemical reaction is produced in the presence of catalyst, and it is small molecule hydrocarbon to make macromolecule hydrocarbon substance decomposition
Class, and then beneficial to the lighting for realizing mink cell focus.Meanwhile the stirred reactor body 22 is compactly adhered to by sucking conduit 21
On the outer wall of flash vaporization kettle 110, the investment goods of oil transfer line has not only been saved, and has reduced the loss of material.
Judge that whether strongly a kind of stirring of stirred reactor, can be judged by the watt level of stirring motor.Most
Main judge index has two：First, mixing speed, if mixing speed doubles, power of motor increases by 8 times (23)；Second,
The length of stirrer paddle, length double, and power of motor increases by 32 times (25).In a kind of preferred embodiment of the application,
The rotating speed of above-mentioned second agitating paddle 221 is 0 turn/min~1500 turn/min continuously adjustabes.It is in addition, another preferably in the application
Embodiment in, the ratio between the blade length of above-mentioned second agitating paddle 221 and the internal diameter of flash vaporization kettle be 0.6~1.2:1.It is above-mentioned preferred
In embodiment, stirring intensity is improved by improving speed of agitator and/or the increase blade length of the second agitating paddle 221, and then
Material is decomposed in the presence of catalyst and react generation small molecule, and small molecule is sent into keep away by condensation segment by flash distillation
Exempt from that condensation reaction occurs, so as to improve deep drawing rate.
It is highly preferred that above-mentioned second agitating paddle 221 is coaxially disposed with the first agitating paddle 24, mixing direction is identical.But both
The design of blade is different, and the first agitating paddle 24 promotes axis direction of the material along stirring shaft 23 (with centrifugal pump or electric fan
It is identical), and the second agitating paddle 221 releases the tangential direction of circumference of the material along the second agitating paddle 221 stirring track formation, two
The launch direction of individual agitating paddle material is in 90 degree.
Because the decomposition of material is carried out with condensation simultaneously, and condensation course is irreversible, therefore, can only be in the second stirring
When the paddle of oar is stirred vigorously, material is run through Venturi tube and flashed, so that the small molecule decomposed is in flash distillation
Escape condensation.And the first agitating paddle 24 primarily serves miniature stirring and material is pushed into the work in stirred reactor body 22
With, in the case that both are coaxially disposed, the rotating speed of two agitating paddles is defined by the speed demand of the second agitating paddle 221, i.e., and second
The rotating speed of agitating paddle 221 determines the rotating speed of the first agitating paddle 24.In order to reduce material when the first agitating paddle 24 stirs as far as possible
Decomposition or condensation, the width and length of the blade of the first agitating paddle 24 can be according to the sliminesses and catalyst grain size of material
Suitable control is carried out with quality, as long as the stirring meets the requirement of catalyst mixing.
Above-mentioned stirred reactor 20 with recycle stock entrance 112 due to being connected, when stirred reactor body 22 is to material
After stirring reaction, directly it can be returned by the recycle stock entrance 112 in flash vaporization kettle 110, can also be by other with following
The entrance that ring material inlet 112 is connected is returned in flash vaporization kettle 110.In a kind of preferred embodiment of the application, such as Fig. 4 institutes
Show, above-mentioned stirred reactor 20 also includes stirring material outlet 25, stirs one end and the recycle stock entrance 112 of material outlet 25
It is connected, the other end passes through the kettle wall of flash vaporization kettle 110 and the intracavity inter-connection of flash vaporization kettle 110.Specifically, material outlet 25 is stirred
The Venturi nozzle that can be provided on the kettle wall of flash vaporization kettle 110, as shown in figure 3, with common with recycle stock entrance 112
Material inlet end, but there is the passage that penetrates kettle wall different from recycle stock entrance 112.Second in stirred reactor body 22
Reacted material is pushed into this section of Venturi tube by centrifugal force caused by the strong stirring of agitating paddle 221, then sprays into tower at a high speed
Reach the purpose of flash distillation in kettle.
Above-mentioned decompression distillation system also includes fixed gas surge tank 30, and along gas flow direction, decompressor 13 is not by
Solidifying gas surge tank 30 is connected with stirred reactor 20, and it is unstable to not coagulated in follow-up stirred reactor 20 to reduce fixed gas discharge
The reaction efficiency of gas, cause the unstable of oil gas partial pressure in follow-up tower reactor section 11 and condensation segment 12.Fixed gas surge tank is set
Put so that airflow balance in whole decompression distillation system running, vacustat, and discharged without waste gas.
In above-mentioned decompression distillation system, stirred reactor 20 is a stirred reactor, can carry out physical agitation, may be used also
Chemically reacted using in the presence of catalyst again as a reactor.Wherein, the chemical reaction one that catalyst occurs
It is cracking, that is, promotes the carbochain of macromolecular hydrocarbon to be broken into small molecule hydrocarbon, existing metal oxide
Type catalyst for cracking or natural and artificial zeolite molecules sieve-type catalyst for cracking are applied to the application.Second, mend
Hydrogen, it is therefore an objective to which the small molecule hydrocarbon for generating fracture obtains hydrogen atom, turns into stable saturated hydrocarbons, reaches heavy oil lightweight
The purpose of change, existing metal oxide catalyst, such as, the hydrogenation catalyst of group VIII transition metal element is applicable
In the application.That is, the catalyst of the application has cracking and the appropriate function of mending hydrogen, make the small molecule hydrocarbon after cracking into
It is unlikely to be combined into the aromatic ring for being difficult to crack for alkane.
And particular/special requirement is had no to the addition manner of catalyst, as long as stirred reactor 20 can be enable in the same of stirring
The above-mentioned chemical reactions of Shi Jinhang.For example can be added from fixed gas entrance, or the recycle stock in tower reactor section 11
Outlet 113, which is delivered on the conveyance conduit between stirred reactor 20, adds catalyst, makes the thing of catalyst and reaction to be mixed
Material is delivered to stirred reactor 20 together, so as to be catalyzed above-mentioned chemical reaction.In a kind of preferred embodiment of the application, preferably
Catalyst inlet 26 is additionally provided with stirred reactor 20, it is convenient to add catalyst in real time as needed.
In another typical embodiment of the application, a kind of vacuum distillation deep drawing technique, the deep drawing work are additionally provided
Skill includes the normal pressure base oil from vacuum furnace inputting the step of any of the above-described kind of decompression distillation system carries out being evaporated under reduced pressure processing,
The step of being wherein evaporated under reduced pressure processing includes：The tower reactor section 11 of normal pressure base oil input vacuum distillation apparatus 10 is evaporated under reduced pressure
Obtain gaseous phase materials and liquid phase material；Condensation segment 12 of the gaseous phase materials through vacuum distillation apparatus 10 carries out distillation processing, is steamed
Evaporate product and fixed gas；Fixed gas is passed through stirred reactor 20, and mixed with source with the liquid phase material of tower reactor section 11
Stirring reaction, obtain mixed material；Mixed material after stirring reaction is sent into tower reactor section 11 to be evaporated under reduced pressure；Wherein, subtract
Pressure evaporation is carried out with distillation processing step under the depressurization of decompressor 13.
The above-mentioned vacuum distillation deep drawing technique of the application, by the way that the normal pressure base oil from vacuum furnace is inputted into above-mentioned be connected with
In the decompression distillation system of stirred reactor 20, by the way that stirred reactor 20 is connected with vacuum distillation apparatus 10, make distillation
Caused fixed gas is fully incorporated stirred reactor 20 in tower, and stirring is sufficiently mixed with the material of the suction out of tower reactor section 11,
In the presence of stirring reaction, the oil gas partial pressure for changing evaporation process causes part fixed gas condensation to return to tower for liquid form product component
In kettle section 11, and part fixed gas is still discharged from the tower reactor section 11 of vacuum distillation apparatus, and then changes the oil gas of still-process
Partial pressure, finally make the airflow balance of system operation, vacustat, not only discharged without waste gas from system, save at waste gas
Cost is managed, and adds liquid-phase product, improves extracting rate.
In above-mentioned deep drawing technique, the temperature of normal pressure base oil uses the feeding temperature of existing vacuum tower.In order to enter
One step reduces energy consumption, and the temperature of normal pressure base oil is preferably 320 DEG C~380 DEG C in the application.The feeding temperature ratio of the normal pressure base oil
In general deep drawing rectifying column material temperature reduce by 30~50 DEG C, can not only by stirring reaction improve extracting rate, and reduce
Heating energy consumption, energy-saving effect are obvious.
In above-mentioned deep drawing technique, depressurized using the decompressor of vavuum pump etc, specific decompressor goes out
Mouthful pressure size can need to carry out reasonable adjusting according to evaporation effect, specific regulating measure can by the rotating speed of vavuum pump come
Realize.In above-mentioned deep drawing technique, the outlet pressure with controlling decompressor 13 in distillation processing step preferably is being evaporated under reduced pressure
For 10kPa~40kPa, under the pressure limit, flash evaporation effect is good.
Residence time length of the normal pressure base oil in tower reactor section 11 can be with the reduction vaporization step of above-mentioned deep drawing technique
Depending on the requirement such as based on crude quality, feeding temperature and light oil extracting rate, equally, the extracting rate of light oil can pass through charging
Temperature and residence time control.In a kind of preferred embodiment of the application, normal pressure base oil is controlled in step is evaporated under reduced pressure
Residence time in tower reactor section 11 is 30min~90min.Material can fully be evaporated in the period, relatively more
Gas-liquid separation is thoroughly realized, so as to improve extracting rate.
In above-mentioned deep drawing technique, stirred reactor 20 can basis to the stirring reaction time of fixed gas and liquid phase material
Crude oil species and the different of quality carry out Reasonable adjustment, and in a kind of preferred embodiment of the application, the stirring reaction time is
(the stirring reaction time refers to residence time of the material in stirred reactor 20 to 1min~5min, i.e., is stirred by the second agitating paddle 221
Time).Due in the stirring reaction of the application in addition to the mixing of physics, the also chemical reaction of Hydrocracking, because
And by reacting while stirring, mixing time can not only be shortened, and the lighting of heavy oil product can also be promoted, improve light oil
The extracting rate of product.
In addition, tower reactor section 11 also exports decompression residuum after light oil is extracted from bottom.Due to crude oil heaviness trend
Constantly extension, the extracting rate of existing general vacuum distillation apparatus are at best able to arrival 70%~75%.It was proved that this
The deep drawing technique of application can further extract 30% to having extracted the decompression residuum after 70%~75% light oil~
80% light oil.That is, the deep drawing technique of the application can be obtained extracting rate as 83%~95%.From the angle of economic benefit
Consider, it is proposed that the operation selection of destilling tower is run in two extreme situations, i.e., extracting rate is 83% or 95%.When selection extracting rate
For 83% (establishing standard curve by experiment to determine the concrete operations parameter under specific extracting rate), 8 are higher by than general deep drawing
Percentage point, its economic benefit is quite notable, and that discharges subtracts slag, to after common deep drawing to subtract slag amount similar, without changing
Any process conditions can be used to follow-up delayed coking；When select extracting rate for 95% when, then the vacuum distillation of the application
Process reduces follow-up coking process, is expelled directly out about 5% bed material (substantially pitch), and the quality of liquid-phase product is far high
In the liquid-phase product of coking, (coking is thermal cracking, and its product is mainly cyclic hydrocarbon；Catalytic pyrolysis can be with output alkane, thus quality
More preferably).
Further illustrate the beneficial effect of the application below in conjunction with specific embodiments.
It should be noted that example 1 below and 2 is single pot of experiment, it is not continuous experiment.Wherein, embodiment 1 is plus taken
Discontinuous one of experimental record (based on hectogram), the embodiment 2 of expanding of big UNB universities is the discontinuous pilot experiment in Beijing Yanshan Mountain
One of record (based on hundred kilograms).
Embodiment 1
The decompression for using existing vacuum distillation apparatus (extracting rate is 70%~75%) to obtain the post processing of light oil extraction
Residual oil is handled using vacuum distillation deep drawing technique of the invention as shown in Figure 1 on this basis as raw material.Specific step
It is rapid as follows：
Decompression residuum 207g normal temperature is added in the vacuum distillation apparatus of the present invention, when temperature of charge reaches 350 DEG C,
Under 40ml/min nitrogen atmosphere protection, material is sent into stirred reactor under the promotion of the first agitating paddle shown in Fig. 4 (to be added
Add hydrocracking catalyst) continuously stir 30min under 650r/min speed of agitator.
Under 200ml/min nitrogen atmosphere protection, at a temperature of 350 DEG C, continued with 650r/min speed of agitator
60min is continuously stirred, obtains liquid oil 172.7g.The liquid yield of the embodiment subtracts slag base deep drawing 70~75%
On plinth, and more than 80% (172.7/207=83.1%) of deep drawing.
In whole course of reaction, the pressure of Top of Vacuum Tower vavuum pump is maintained between 40~50Kpa.
Embodiment 2
The mixing slurry oil that two catalysis and three catalysis are thrown away in the swallowization FCC apparatus of Beijing is used to be adopted on this basis for raw material
Handled with vacuum distillation deep drawing technique of the invention as shown in Figure 1.Comprise the following steps that：
Heating process：Catalytic slurry 320kg is inputted in vacuum distillation apparatus, the design temperature of vacuum distillation apparatus is
380 DEG C, the wall temperature of heating 4h vacuum distillation apparatus reaches 380 DEG C, and temperature of charge reaches 320 DEG C, and stirred reactor (with the addition of and add
Hydrogen catalyst for cracking) continuously stirred under 0.6HZ stirring frequency.Now, vavuum pump is also without vacuumizing.
Course of reaction：Material sustained response 1h at 320 DEG C, is vacuumized by vavuum pump, and the fixed gas of extraction is passed through
In fixed gas surge tank, then fixed gas is passed through to the stirring being connected with vacuum distillation apparatus as the protective gas of course of reaction
In reactor.Under the conditions of being somebody's turn to do, stirred reactor continuously stirs 1h under 7.5HZ stirring frequency, passes through the strong of stirred reactor
Power stirs, and in the presence of catalyst, cracking reaction occurs for slurry oil, produces small molecule hydro carbons, enters shell and tube by flash vaporization kettle
Condenser condenses.
Reaction effect：Reaction temperature is arranged to 150 DEG C, temperature of charge from 320 DEG C it is rapid decline, waste gas protection do not stop,
Shut down after continuing 0.2h under 0.6HZ stirring frequency, residual gas is evacuated in condenser, obtains liquid 95kg.The embodiment
Liquid yield subtracts after slag enters back into FCC crackings, thrown away from cracked fuel oil on the basis of deep drawing 70~75% subtracts slag
Nearly 30% (95/320=29.7%) light oil has been extracted in catalytic slurry again.
Embodiment 3
The method of the present invention is used for the design of certain newly-built 1,000,000 tons/year of crude oil atmospheric vacuum distillation device, wherein, decompression is steamed
The technological process for evaporating system is same as shown in Figure 1.
Reference examples 1
According to flash process is strengthened disclosed in CN103242885A, three sets of decompressions have been disposed between atmospheric tower and vacuum tower
Stove and flash vaporization kettle, by flashing one after another, normal base oil is pulled out as far as possible.
Under same feedstock, process conditions, for embodiment 3 and reference examples 1 in decompression extracting rate, plant energy consumption, investment
Etc. carry out data comparison, comparison result is shown in Table 1.
Table 1：
The data of upper table 1 are carried out with analysis it can be seen that：
1) temperature of embodiment 3 is less than reference examples 1, and by taking flash vaporization kettle feeding temperature as an example, the two temperature difference is 395-350=45
DEG C, 2.1MJ/T* DEG C of the calorific value average out to of heavy oil heating, then comparative example 1 need the increased heat to be：2.1MJ/T*℃×45℃
× 550T/h=51975MJ/h.Equivalent to the caloric value of 1.32 tons of mink cell focuses, if 1 year calculated by 8000 hours, compare
Example 1 needs the caloric value of 10560 tons of heavy oil of consumption more；If pressing inner accounting valency, decompression residuum valency=ten thousand/tons of $0.18, then
The consumption=ten thousand/years of $1900 of 1 year.
2) the raw material maximum heating temperature of reference examples 1 reaches 420 DEG C, will cause the decomposition and condensation of reduced crude, this
The Quality Down of decompression residuum will be caused.
3) for relative degree of vacuum, relative degree of vacuum=absolute pressure-local atmospheric pressure, if it is assumed that local atmospheric pressure
For 0.1MPa=100KPa (atmospheric pressure), the relative degree of vacuum of the vacuum distillation apparatus tower top of that the application for 30~
40KPa-100KPa=- (60~70) KPa (is slightly below half of atmospheric pressure -50KPa), true using the more cheap pendular ring of price
Empty pump can be achieved；And relative degree of vacuum=1.315KPa-100KPa=-98.685KPa of the Top of Vacuum Tower of reference examples 1 (-
100KPa is absolute vacuum, can only be reached in theory), close to absolute vacuum.So high vacuum needs many energy
It can reach and it is necessary to which, using vapor jet vacuum pump, not only capital intensive, operating cost are also very high.
4) due to deep drawing, true boiling-point (TBP) deep drawing cutting temperature=612 DEG C of reference examples 1, and embodiments herein 3 is without such as
This high deep drawing vacuum, therefore true boiling-point (TBP) deep drawing cutting temperature=526 DEG C, due in the deep drawing technique of the application except physics
Reaction is outer, additionally uses chemical reaction, therefore the height of extracting rate can not be evaluated with the height of the true boiling-point (TBP) cutting temperature.
5) due to being using vapor jet vacuum pump or using superheated steam extraction oil gas, the steam consumption of reference examples 1
6783kg/h, the price Mu Qian great Yue Shi $160/T of vapor, then reference examples 1 be used for steam expense=6.783 × 160=
Ten thousand/years of $407/h=$325.6.
6) top vacuum pump load=1.32MW that reference examples 1 propose, this is a quite huge energy consumption, and the application adopts
Liquid-ring vacuum pump is only 120kw=0.012MW.The scheme of reference examples 1 is calculated and (calculated than steam cheap) by the electricity charge will
The vavuum pump expense in Fu Chu ten thousand/years of $633.6.
7) the application, which stirs two reactors, needs agitating paddle to stir, and the volume of reactor is only the 1/5 of flash vaporization kettle, and
It is elongated cylindrical shape, the diameter of reactor is only 1~1.2m, its stirrer paddle length<(1~1.2) m/2 rice, mixing speed
For 0~300 rev/min, average speed=150 rev/min；Three flash vaporization kettles of reference examples 1 have mixing component (not draw stirring
Motor, have certainly) though the length of stirrer paddle is not provided, by taking the first flash vaporization kettle as an example, its blade length will be 1.5
~2.0m even more than, its mixing speed be 0~600 rev/min, average speed=300 rev/min；According to the Tian Jinzhi forever of classics
Agitating paddle rating formula, agitating paddle power and rotating speed are in 3 power relations, and blade length is in 5 power relations, and the application is set
The agitating paddle power of motor of meter is 90~120kw, and the power of agitator only rotating speed one that can extrapolate reference examples 1 is exactly this patent
8 times, if considering further that the factor of stirrer paddle, its power is very big, be often only consumption stirring motor on consumption
In electric $400~6,000,000/year, this is also a considerable numeral.
8) the highest extracting rate of the application reaches the 85~95% of normal base oil, remaining decompression residuum (by vacuum tower
After 60% extracting rate, 70~80% light oil is extracted again to 40% decompression residuum to calculate) about=8.0~12%, can
To be directly entered asphalt industry, delayed coking process is eliminated, it is invested and operating cost ratio is established delayed coking and saved perhaps
It is more；Reference examples 1 and the application be not in an order of magnitude, nor identical theory and principle.
Embodiment 4
Certain oil refining enterprise's technological transformation：
Certain oil refining enterprise, reduced crude 1.2MT/a, light oil extracting rate is 60% in the vacuum rectification tower of routine,
About 480,000 tons/year of 40% decompression residuum, subsequently into delay coking process.
Problem：Delay coking process scale is smaller, the decompression residuum amount that can't stand 480,000 tons/year=60 ton hours is held, wished
The charging of about 20 ton hours can be reduced by hoping, keep the normal operation of coking workshop section.
Plan uses scheme：
Scheme one, application scheme (embodiment 4)：In the flash distillation for carrying stirred autoclave of newly-built one of vacuum tower rear portion
Kettle, flash vaporization kettle top products connect condenser and vacuumized, and top products are lightweight wax oil, and bottoms decompression residuum, which enters, to be prolonged
Slow coking process.
Scheme two, prior art (reference examples 2)：Newly-built one flash vaporization kettle with decompression tower body (claims after atmospheric tower
Flash column), it is vacuum furnace after flash column, normal base oil is heated up to 392~420 DEG C and enters vacuum tower by vacuum furnace, and VACUUM TOWER BOTTOM subtracts
Wt (20~70) % of pressure residual oil returns to newly-built flash column and flashed again, this external application high-temperature gas (nitrogen, hydrogen -80~
400 DEG C) enter flash column assistance air lift.
The comparative result of two schemes is shown in Table 2：
Table 2：
* the numerical value for representing 158.6~180.0 is calculated according to equation below：150+ [42.9 × (20%~
70%)].
Seen in slave unit, scheme one and scheme two have flash vaporization kettle, but the difference of the two is, the flash vaporization kettle dress of scheme one
It is located at after vacuum distillation apparatus, the material passed through is only to be depressurized that column distillation is remaining to subtract slag, and flow is about 60T/h, and side
Case one only has flash vaporization kettle without tower body.The flash column of scheme two is installed in before vacuum distillation apparatus, except normal base oil will pass through
Outside, vacuum tower base oil will also return to 20%~70%.From table 2 it was found from flash evaporation feed amount, the inlet amount of scheme two almost compares
About 3 times of scheme one, therefore the flash distillation tower diameter of scheme two should be more than the decompression tower diameter Φ 5200 in existing scheme.
From investment, the two is more or less the same, and the flash vaporization kettle of scheme one is smaller and does not have tower body, but adds a stirring
Reactor；The flash vaporization kettle of scheme two is larger and has tower body, and the investment of its vacuum system is higher than the former.Both sides balance, and investment is more or less the same.
From the point of view of heater outlet temperature is depressurized, scheme two is higher by 30 DEG C than scheme one.In general, heavy oil feed temperature is higher than
360~370 DEG C, material is easily condensed change weight, it is therefore necessary to add quench oil cooling, prevent from being condensed, this same increase operation into
This.
From operating cost, scheme two is all higher than scheme one, therefore its from steam, power consumption, gas consumption (stripping gas) is consumed
Annual earnings are less than scheme one.
As can be seen from the above description, the application the above embodiments realize following technique effect：A, operation section
Energy：Using the process of the invention, the feeding temperature of normal base oil than in general deep drawing rectifying column material temperature lower 30~50 DEG C；
B, energy saving in running：Using the process of the invention, the vacuum level requirements of rectifying column are only the ten of general deep drawing rectifying column requirement
/ mono-, it can reach requirement with liquid-ring vacuum pump.C, environmental protection：Fixed gas is incorporated to refinery off gas system compared in traditional method
System, burning take hot processing method different, and fixed gas is recycled in the application；And liquid-ring vacuum pump does not produce waste liquid,
System is more conducive to environmental protection also without waste residue.D, deep drawing technology and benefit：Using the process of the application, extracting rate is adjustable,
Flexible operation；Extracting rate is much higher than in general deep drawing technology.By taking the normal base oil for handling 1Mt/a as an example, due to the heavy of crude oil
Change trend is serious, the extracting rate of vacuum distillation apparatus typically 60%~70%, if using the application, can from decompression residuum
30% light oil is extracted again, then total extracting rate can improve 8 percentage points, and the benefit is far above equipment investment (as general
When vacuum tower tower reactor is changed into flash vaporization kettle, residence time of material is elongated, and the increase of tower reactor volume, structure is also required to change, and surrounds
Tower reactor also has one or several stirred reactors, and this increases the additional investment of equipment to a certain extent).If pulled out from subtracting in slag
Go out 80%, then rectification under vacuum process directly instead of coking process, and bed material is substantially pitch, and liquid-phase product quality is far above Jiao
The liquid-phase product of change.
Seen from the above description, for a newly-built refinery, steamed using the decompression with deep drawing technology of the application
Evaporating system undoubtedly has higher economy and environmental benefit.For existing refinery, if existing process structure can not be changed,
A set of above-mentioned provided decompression distillation system can also be provided after existing vacuum distillation apparatus.The decompression newly established is steamed
Evaporate system with it is above-mentioned it is newly-built under the conditions of decompression distillation system have following difference in process conditions：A, inlet feed is not normal pressure
Base oil but decompression residuum, the amount of decompression residuum is fewer than normal base oil, so device can also appropriate contracting scale smaller；B, condensation segment
Top can connect rectifying column and can also simply install condenser, the liquid product being condensed is equivalent to the vacuum tower line that subtracts 2
Or the line product that subtracts 3, FCC apparatus can be sent directly into.Which kind of device is specifically used, is considered as the quality, quantity and dress of light oil
The economic indicators such as investment, running cost are put, depending on comparison；C, the extracting rate of the system still suggests taking two outliers
According to when that is, extracting rate is 30%, delay coking process can be sent into by extracting the base oil after light oil；When extracting rate is 80%, bottom
Oil is mainly pitch, can be used directly as road asphalt or solid fuel.
The preferred embodiments of the present invention are the foregoing is only, are not intended to limit the invention, for the skill of this area
For art personnel, the present invention can have various modifications and variations.Within the spirit and principles of the invention, that is made any repaiies
Change, equivalent substitution, improvement etc., should be included in the scope of the protection.
Claims (22)
1. a kind of decompression distillation system, it is characterised in that the decompression distillation system includes：
Vacuum distillation apparatus (10), including set gradually along gas flow direction tower reactor section (11), condensation segment (12) and subtract
Pressure device (13), wherein, the condensation segment (12) includes fixed gas outlet (121)；
Stirred reactor (20), the stirred reactor (20) is connected with the tower reactor section (11), for the tower reactor section
(11) material in is stirred and the material is returned into the tower reactor section (11)；
Wherein, the condensation segment (12) passes sequentially through the fixed gas outlet (121) and the decompressor (13) stirs with described
Reactor (20) is mixed to be connected.
2. decompression distillation system according to claim 1, it is characterised in that the tower reactor section (11) includes flash vaporization kettle
(110), the flash vaporization kettle (110) includes gaseous phase outlet (111), recycle stock entrance (112) and recycle stock outlet
(113), the gaseous phase outlet (111) is connected with the condensation segment (12), and the stirred reactor (20) is respectively by described
Recycle stock exports (113) and the recycle stock entrance (112) and connects to form material and be recycled back to the flash vaporization kettle (110)
Road.
3. decompression distillation system according to claim 2, it is characterised in that the flash vaporization kettle (110) goes out in the gas phase
Mouth (111) place is provided with gas phase entrainment block piece (114).
4. decompression distillation system according to claim 3, it is characterised in that the gas phase entrainment block piece (114)
Including the circumferentially disposed annular boiling liquid baffle plate (1141) of the inwall along the flash vaporization kettle (110) and along the flash vaporization kettle (110)
Axial direction be arranged on stop umbrella (1142) above annular boiling liquid baffle plate (1141), the annular boiling liquid baffle plate
(1141) there is centre bore, the stop umbrella (1142) and the annular boil liquid baffle plate (1141) and be connected and be located at the centre bore
Top.
5. decompression distillation system according to claim 2, it is characterised in that the condensation segment (12) is rectifying column, described
Rectifying column includes packed tower, and structured packing is filled with the packed tower.
6. decompression distillation system according to claim 2, it is characterised in that the decompressor (13) is vavuum pump.
7. the decompression distillation system according to any one of claim 2 to 6, it is characterised in that the stirred reactor
(20) include：
Stirred reactor body (22),
Conduit (21) is sucked, extracting part is provided with the sucking conduit (21), described one end for sucking conduit (21) passes through institute
State recycle stock outlet (113) and stretch into the flash vaporization kettle (110) inside, the other end for sucking conduit (21) and the stirring
Reactor body (22) is connected, and the conduit (21) of sucking extracts material in the flash vaporization kettle (110) and by the material
It is delivered in stirred reactor body (22) and is stirred reaction, passes through the recycle stock entrance after the material is agitated
(112) flash vaporization kettle (110) is returned.
8. decompression distillation system according to claim 7, it is characterised in that the stirred reactor (20) also includes driving
Agitating element, one end of the driving agitating element sequentially pass through the stirred reactor body (22) and the sucking conduit
(21) and the flash vaporization kettle (110) inside is stretched into, the other end of the driving agitating element is connected with drive device.
9. decompression distillation system according to claim 8, it is characterised in that the driving agitating element includes stirring and driven
Axle (23) and the first agitating paddle (24), one end of the stirring shaft (23) sequentially pass through the stirred reactor body (22)
With the sucking conduit (21) and to stretch into the flash vaporization kettle (110) internal, the other end of the stirring shaft (23) with it is described
Drive device is connected；First agitating paddle (24) is arranged on the stirring shaft (23) and stretches into the flash vaporization kettle (110)
Internal one end, the ratio between the length of first agitating paddle (24) and the internal diameter of the flash vaporization kettle (110) are 0.1~0.3:1.
10. decompression distillation system according to claim 9, it is characterised in that the extracting part includes promoting blade
(211), the promotion blade (211) is arranged on the stirring shaft (23) and in the sucking conduit (21).
11. decompression distillation system according to claim 9, it is characterised in that set in the stirred reactor body (22)
It is equipped with the second agitating paddle (221), second agitating paddle (221) and the stirring shaft (23) drive connection.
12. decompression distillation system according to claim 11, it is characterised in that have one on second agitating paddle (221)
Group or multigroup blade (222), the blade (222) be arranged in parallel with the stirring shaft (23).
13. decompression distillation system according to claim 12, it is characterised in that the blade of second agitating paddle (221)
The ratio between internal diameter of length and the flash vaporization kettle (110) is 0.6~1.2:1.
14. decompression distillation system according to claim 12, it is characterised in that the stirring of second agitating paddle (221)
Rotating speed is 0~1500r/min continuously adjustabes.
15. decompression distillation system according to claim 7, it is characterised in that the stirred reactor (20) also includes stirring
Material outlet (25) is mixed, one end of the stirring material outlet (25) is connected with the recycle stock entrance (112), the other end
Through the intracavity inter-connection of the kettle wall and the flash vaporization kettle (110) of the flash vaporization kettle (110).
16. decompression distillation system according to claim 1, it is characterised in that the decompression distillation system also includes not coagulating
Gas surge tank (30), along gas flow direction, the decompressor (13) is stirred by the fixed gas surge tank (30) with described
Reactor (20) is mixed to be connected.
17. the decompression distillation system according to claim 1 or 16, it is characterised in that on the stirred reactor (20) also
It is provided with catalyst inlet (26).
18. one kind is evaporated under reduced pressure deep drawing technique, it is characterised in that the deep drawing technique is included the normal pressure base oil from vacuum furnace
The step of decompression distillation system any one of input claim 1 to 17 carries out being evaporated under reduced pressure processing, the decompression are steamed
The step of evaporating processing includes：
The tower reactor section (11) of normal pressure base oil input vacuum distillation apparatus (10) is evaporated under reduced pressure to obtain gaseous phase materials
And liquid phase material；
Condensation segment (12) of the gaseous phase materials through the vacuum distillation apparatus (10) carries out distillation processing, obtain product of distillation and
Fixed gas；
The fixed gas is passed through stirred reactor (20) and mixed with the liquid phase material from the tower reactor section (11)
Stirring reaction is closed, obtains mixed material；
The mixed material is returned into the tower reactor section (11) to be evaporated under reduced pressure；
Wherein, the step of reduction vaporization is handled with the distillation is carried out under the depressurization of decompressor (13).
19. deep drawing technique according to claim 18, it is characterised in that the temperature of the normal pressure base oil is 320 DEG C~380
℃。
20. deep drawing technique according to claim 18, it is characterised in that in the reduction vaporization and the distillation processing
The outlet pressure of decompressor described in step (13) is 10kPa~40kPa.
21. deep drawing technique according to claim 18, it is characterised in that described normal in the step of reduction vaporization
It is 30min~90min to press residence time of the base oil in the tower reactor section (11).
22. deep drawing technique according to claim 18, it is characterised in that the stirred reactor (20) is to the fixed gas
The stirring reaction time with the liquid phase material is 1min~5min.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112843764A (en) * | 2021-03-24 | 2021-05-28 | 捷创(东营)能源技术有限责任公司 | Vacuum rectification tower with satellite type tower kettle and vacuum rectification method of atmospheric residue |
| CN113617052A (en) * | 2021-07-19 | 2021-11-09 | 茂名海和石油化工有限公司 | Stripping oil refining process using nitrogen as gas source |
| TWI842989B (en) * | 2021-04-20 | 2024-05-21 | 張正穎 | Solar energy heat collection and decompression evaporation seawater desalination device |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1287872A (en) * | 1999-09-15 | 2001-03-21 | 上海石油化工股份有限公司 | Crude oil atmospheric vacuum distillation method with deep stripping process |
-
2016
- 2016-07-25 CN CN201610594753.9A patent/CN107653005B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1287872A (en) * | 1999-09-15 | 2001-03-21 | 上海石油化工股份有限公司 | Crude oil atmospheric vacuum distillation method with deep stripping process |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112843764A (en) * | 2021-03-24 | 2021-05-28 | 捷创(东营)能源技术有限责任公司 | Vacuum rectification tower with satellite type tower kettle and vacuum rectification method of atmospheric residue |
| TWI842989B (en) * | 2021-04-20 | 2024-05-21 | 張正穎 | Solar energy heat collection and decompression evaporation seawater desalination device |
| CN113617052A (en) * | 2021-07-19 | 2021-11-09 | 茂名海和石油化工有限公司 | Stripping oil refining process using nitrogen as gas source |
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