CN107653005B - 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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- CN107653005B CN107653005B CN201610594753.9A CN201610594753A CN107653005B CN 107653005 B CN107653005 B CN 107653005B CN 201610594753 A CN201610594753 A CN 201610594753A CN 107653005 B CN107653005 B CN 107653005B
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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 present invention provides a kind of decompression distillation system and vacuum distillation deep drawing techniques.The decompression distillation system includes: vacuum distillation apparatus and stirred reactor, and vacuum distillation apparatus includes tower reactor section, condensation segment and the decompressor set gradually along gas flow direction, and condensation segment includes fixed gas outlet；Stirred reactor is connected with tower reactor section, for being stirred to the material in tower reactor section and material being returned to tower reactor section；Wherein, condensation segment passes sequentially through fixed gas outlet and decompressor is connected with stirred reactor.The airflow balance of system operation, vacustat were both discharged without exhaust gas, eliminated the device of processing exhaust gas, reduced cost of investment；Liquid-phase product is increased again, improves extracting rate.
Description
Technical field
The present invention relates to petroleum refining fields, in particular to a kind of decompression distillation system and vacuum distillation deep drawing work
Skill.
Background technique
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 mass production of the conventional bad oil of heavy, the product yield of atmospheric distillation tower will be forced to be gradually reduced, thus, to raising or keep refining
For oily Business Economic Benefit, vacuum rectification tower will play more importantly role.
Countries in the world are in relation to the research institution and refinery that refine oil, all output in concern and Improvement vacuum rectification tower
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-(tower bottom discharge decompression residuum total amount/enter vacuum rectification tower normal pressure base oil
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..Under the premise of the first two factor is constant, the extracting rate of vacuum rectification tower is dependent on to own
The improvement of structure and technique.Chinese invention patent CN1194070C discloses a kind of petroleum Atmospheric vacuum technique, is subtracted with increase is a set of
The mode of furnace 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 is proposed conventional Atmospheric vacuum system " two-furnace three-tower " (flash distillation
Tower → atmospheric pressure kiln → atmospheric tower → vacuum furnace → vacuum rectification tower) change into " two furnaces, four tower ", i.e., atmospheric tower and vacuum furnace it
Between add a flash column, 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, has certain reference value, but nonsensical for grassroot refinery.Moreover, new
Increase a flash column, the material temperature into subsequent vacuum furnace will be lower, to increase the burden of vacuum furnace, and newly-increased
The benefit that equipment will lead to system reduces.
Chinese patent application CN103242885A proposes three flash vaporization kettles of increase 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.This method is effective certainly to the increase of vacuum tower extracting rate.The patent the problem is that, increase
There are also the component that revolving speed is up to 600 revs/min in three each kettles of flash vaporization kettle, to 550T/ hours flash vaporization kettles, diameter should be
The power of motor of 2m or more, rotary evaporation can be up to 200kw or more, so the investment of flash vaporization kettle can be quite high, three flash vaporization kettles
Between there are two pot arch, along with steam stripped high-temperature gas is used for, investment can be increased very much.
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 oil refining process is added using biomass in this method, has comparable novelty, but not basic in technique
Upper change distillation technique.
The technology for improving vacuum rectification tower extracting rate is known 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 is that the oil gas partial pressure of product in tower is reduced, third is that improving the vacuum of vacuum rectification tower
Degree.In general, vacuum rectification tower feeding temperature needs to improve 5%~8%, and feeding temperature is higher under deep drawing technique, extract
Rate is also higher, but excessively high feeding temperature will lead to material coking and the more cracking fixed gases of generation in tower, seriously affect
The normal operation of vacuum rectification tower.For reducing oil gas partial pressure, currently popular method 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 a large number of water molecules steam more light than wax oil quality is crowded in wet type vacuum rectification tower
In tower, about 90% space is occupied, considerably increases the load of vacuum rectification tower, reduces and extracts efficiency, and is generated many
Waste water to be treated, thus inject tower bottom steam amount and also limited by efficiency and environmental protection.
Since preceding two measures are by comparable 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 boiling cut point (TBP) higher than 565.60 DEG C are known as deep drawing technique, state by the oil company of foreign well-known
The interior limitation due to equipment and technology, the real boiling cutting of deep drawing technique is generally at 540 DEG C or so.
In conclusion the most important constraint of rectification under vacuum is to make material in vacuum rectification tower under the conditions of prior art
It only undergoes the physical process of a distillation phase inversion and cannot have any chemical process.It is entitled " vacuum rectifying apparatus and its
Rectificating method " Chinese patent application CN201510498467.8, propose 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 basic principle and
Constraint.For current process conditions, this constraint is necessary, because residual oil is split under conditions of without external hydrogen source
Solution will lead to further condensation, and material is made to become heavier, be unfavorable for subsequent coking process.Therefore, existing vacuum rectification tower
In operation, there is stringent limitation in residence time of the material in rectification under vacuum tower reactor, and decompression residuum once leaves decompression essence
Tower is evaporated, requires that quench oil is added and reduces to subtract slag temperature, avoids cracking.Therefore, existing rectification under vacuum deep drawing technique there is still a need for
It improves.
Summary of the invention
The main purpose of the present invention is to provide a kind of decompression distillation system and rectification under vacuum deep drawing techniques, further to mention
The extracting rate of high rectification under vacuum in the prior art.
To achieve the goals above, 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, and vacuum distillation apparatus includes setting gradually along gas flow direction
Tower reactor section, condensation segment and decompressor, condensation segment include fixed gas outlet；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 subtracts
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 by recycle stock outlet and recycle stock entrance and dodges respectively
Kettle is steamed to be connected 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 inner wall be circumferentially arranged annular boiling liquid baffle with
And the blocking umbrella above annular boiling liquid baffle is set along the axial direction of flash vaporization kettle, annular boiling liquid baffle has centre bore, resistance
Gear umbrella is connected with annular boiling liquid baffle and is located at the top of centre bore.
Further, condensation segment includes rectifying column, and rectifying column includes packed tower, is filled with structured packing in packed tower.
Further, decompressor is vacuum pump.
Further, stirred reactor includes: stirred reactor ontology, sucks conduit, sucks in conduit and is provided with extraction
Portion, the one end for sucking conduit are protruded into inside flash vaporization kettle by recycle stock outlet, suck the other end and stirred reactor of conduit
Ontology is connected, and sucking conduit extracts the material in flash vaporization kettle and material is delivered in stirred reactor ontology and is stirred instead
It answers, flash vaporization kettle is returned to by recycle stock entrance after material is agitated.
Further, stirred reactor further includes driving agitating element, and one end of agitating element is driven to sequentially pass through stirring
Reactor body and sucking conduit simultaneously protrude into inside flash vaporization kettle, and the other end of agitating element is driven to be connected with driving device.
Further, driving agitating element includes stirring shaft and the first agitating paddle, and one end of stirring shaft is successively
It across stirred reactor ontology and sucks conduit and protrudes into inside flash vaporization kettle, the other end of stirring shaft is connected with driving device
It is logical；First agitating paddle is arranged in stirring shaft and protrudes into one end 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 pushing blade, pushes blade to be arranged on stirring shaft and be located at and sucks conduit
It is interior.
Further, the second agitating paddle is provided in stirred reactor ontology, the second agitating paddle and stirring shaft drive
Connection.
Further, there are one or more groups of blades on the second agitating paddle, blade is 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 continuously adjustable for 0~1500r/min.
Further, stirred reactor further includes stirring material outlet, and the one end and recycle stock for stirring material outlet enter
Mouth is connected, and the kettle wall that the other end passes through flash vaporization kettle is connected with the inner cavity of flash vaporization kettle.
Further, decompression distillation system further includes fixed gas surge tank, and along gas flow direction, decompressor is not by
Solidifying gas surge tank is connected with stirred reactor.
Further, catalyst inlet is additionally provided on stirred reactor.
To achieve the goals above, according to an aspect of the invention, there is provided a kind of vacuum distillation deep drawing technique, the depth
Pulling out technique includes that the normal pressure base oil from vacuum furnace is inputted to any of the above-described kind of decompression distillation system to carry out vacuum distillation processing
Step, wherein the step of vacuum distillation is handled includes: that the tower reactor section of normal pressure base oil input vacuum distillation apparatus is carried out decompression steaming
Hair is to obtain gaseous phase materials and liquid phase material；Gaseous phase materials carry out distillation processing through the condensation segment of vacuum distillation apparatus, are steamed
Evaporate product and fixed gas；Fixed gas is passed through stirred reactor and be mixed with the liquid phase material from tower reactor section anti-
It answers, obtains 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 it is 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 be 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 time that is stirred to react of fixed gas and liquid phase material.
It applies the technical scheme of the present invention, by the way that stirred reactor is connected with vacuum distillation apparatus, makes to generate not
Solidifying gas is fully incorporated stirred reactor, stirring is sufficiently mixed with the material sucked out of tower reactor section, in stirring and the work of catalyst
Under, is divided by complicated chemical reaction and the oil gas for changing evaporation process, be not only broken the macromolecule hydro carbons in material
Become stable saturated hydrocarbons for small molecule hydro carbons and under the action of mending hydrogen, and fixed gas condensation in part is made to be liquid form product group
Divide 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, in turn
Change the oil gas partial pressure of distillation process, the airflow balance for finally running system, vacustat was both discharged without exhaust gas, and saved
The device of processing exhaust gas has been removed, cost of investment is reduced；Liquid-phase product is increased again, improves extracting rate.
Detailed description of the invention
The accompanying drawings constituting a part of this application is used to provide further understanding of the present invention, and of the invention shows
Examples and descriptions thereof are used to explain the present invention for meaning property, does not constitute improper limitations 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 invention；
Fig. 2 shows the structural schematic diagrams of the flash vaporization kettle in a kind of preferred embodiment of the invention；
Fig. 3 shows the schematic top plan view in the face A-A of annular boiling liquid baffle in Fig. 2；And
Fig. 4 shows the structural schematic diagram of the stirred reactor in a kind of preferred embodiment of the invention.
Wherein, the above drawings include the following reference numerals:
10, vacuum distillation apparatus；11, tower reactor section；12, condensation segment；13, decompressor；121, fixed gas exports；
110, flash vaporization kettle；111, gaseous phase outlet；112, recycle stock entrance；113, recycle stock exports；114, gas phase mist
Foam carries block piece secretly；1141, annular boiling liquid baffle；1142, stop umbrella；
20, stirred reactor；21, conduit is sucked；22, stirred reactor ontology；23, stirring shaft；24, the first stirring
Paddle；211, blade is pushed；221, the second agitating paddle；222, blade；25, material outlet is stirred；26, catalyst inlet；
30, fixed gas surge tank.
Specific embodiment
It should be noted that in the absence of conflict, the features in the embodiments and the embodiments of the present application can phase
Mutually combination.Below in conjunction with embodiment, the present invention will be described in detail.
It should be noted that the length of the first agitating paddle and the second agitating paddle is respectively referred to drive agitating shaft in the application
Center line be boundary, the sum of the length of blade at both ends.In the application, with the tower reactor section or flash vaporization kettle of vacuum distillation apparatus
Diameter be D calculate, then the length of the first agitating paddle be 0.1D~0.3D；The length of second agitating paddle is 0.6D~1.2D.
As background technology part is previously mentioned, transformation presence or equipment investment of the prior art to decompression distillation system
High, less economical or deep drawing rate improves limited defect.In order to improve this situation, in a kind of typical implementation of the application
In mode, a kind of decompression distillation system is provided, as shown in Figure 1, the decompression distillation system includes: vacuum distillation apparatus 10, packet
Include tower reactor section 11, condensation segment 12 and the decompressor 13 set gradually along gas current method, wherein condensation segment 12 includes 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 makes vacuum distillation apparatus by the way that stirred reactor is connected with vacuum distillation apparatus
The fixed gas (products such as hydrogen, carbon monoxide, carbon dioxide, methane, ethane, ethylene and water vapour when main component) of middle generation
It is fully incorporated stirred reactor, is sufficiently mixed stirring with the material sucked out of tower reactor section, under the action of being stirred to react, is changed
The oil gas of evaporation process divides so that fixed gas condensation in part is that liquid form product component returns in tower reactor section, and part fixed gas is still
It is so discharged from the tower reactor section of vacuum distillation apparatus, and then changes the oil gas partial pressure of distillation process, the tolerance for finally running system
Balance, vacustat, no exhaust gas is discharged from system and liquid-phase product increased, 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, for example,
Existing tower reactor can be used if the tower reactor volume of existing vacuum tower can satisfy treating capacity.In a kind of preferred reality of the application
It applies 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
It crosses recycle stock outlet 113 and recycle stock entrance 112 is connected 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 into the normal pressure base oil or agitated reaction of flash vaporization kettle
Material that device 20 is returned from recycle stock entrance 112 carries out gas-liquid separator, thus by light-end products from 111 row of gaseous phase outlet
Out, into being condensed and separated in condensation segment 12.Not only mitigate the load of condensation segment, but also the charging temperature of normal pressure base oil can be made
In the case where spending 30~50 DEG C of the feeding temperature reduction than existing deep drawing rectifying column, extracting rate is improved.
Condensation segment in above-mentioned vacuum distillation apparatus according to selection rectifying column according to the actual situation or with condenser,
In petroleum refining industry as without to fraction be precisely separated or fraction in petrol and diesel oil ratio it is less, it is when rectifying has little significance, then general to use
Condenser substitution.Following judgement can be done from the pilot scale stage of the invention: if from initial boiling point to 205 DEG C of gasoline section institute accounting
Li≤steamed food material 15%, petrol and diesel oil Suo accounting Li≤40% directly distillate petrol and diesel oil using rectifying column, and rest materials enter
FCC cracking 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 do not need to build rectifying column, condensable product is directly entered FCC or is hydrocracked, from skill
The analysis of art economic angle is more reasonable.
In a preferred embodiment of the present application, as shown in Fig. 2, above-mentioned flash vaporization kettle 110 is arranged at gaseous phase outlet 111
There is gas phase entrainment block piece 114, be conducive to remove mist, reduces gas phase oil product to the inclusion rates of heavy oil product.For mist
The filtering removal of foam can be there are many implementation, for example use filter screen, in the prior art any function that can be realized
Component 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 packet
It includes and boils liquid baffle 1141 along the annular that the inner wall of flash vaporization kettle 110 is circumferentially arranged and exist along the axial direction setting of flash vaporization kettle 110
The blocking umbrella 1142 of 1141 top of annular boiling liquid baffle, annular boiling liquid baffle 1141 have centre bore, stop umbrella 1142 and annular
Boil the top that liquid baffle 1141 is connected and is located at centre bore.
In above-mentioned preferred embodiment, annular boiling liquid baffle 1141 is annular hollow baffle, can be blocked along wall flowing
Liquid, and gas therefrom overflow by vacancy.The area of umbrella 1142 is stopped to be slightly larger than the area of ring baffle hollow space, liquid and bubble
Foam is blocked umbrella 1142 and blocks, and gas can rise from side around the edge of umbrella.The ring baffle of annular boiling liquid baffle 1141
Part can prevent most of liquid phase oil product from turning over and being mingled with by gas phase 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 transmission of annular boiling liquid baffle 1141, encountered during continuing and rising centrally disposed
Blocking umbrella 1142 above hole and be blocked, the mist of heavy oil product or the generation of gas phase oil product was carried out to realize
Filter and blocking.
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 increase rectifying effect
Fruit, in a preferred embodiment of the present application, above-mentioned condensation segment 12 include packed tower, are filled with structured packing in packed tower,
Structured packing has many advantages, such as that large specific surface area, pressure drop are small, fluid point is uniform, mass-and heat-transfer is high-efficient, and rectification effect is good.Herein
Particular/special requirement is had no to the specific type of structured packing, using known conventional structured packing.Common structured packing
Include but are not limited to corrugated plate regular packing, the folding structured packing of peak formula or MELLAPAK filler etc..
Decompressor 13 in above-mentioned decompression distillation system uses common vacuum 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 does not generate waste liquid, more conducively environmentally friendly.
In practical 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, installs mixing plant additional hardly in flash vaporization kettle
It may.Thus, in this application, preferably set up around tower reactor section 11 the lesser stirred reactor 20 of one or 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
The fixed gas generated in 12 is partially converted into light-end products under the action of stirring and catalyst or fluid oil loops back,
It is easy to implement the airflow balance of system operation and increases the liquid-phase product of system discharge, improve extracting rate.In the prior art,
The petroleum pipeline that the room 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
High temperature is deposited and be in material liquid phase simultaneously, and oil transfer line to be made to have the smallest resistance loss and its production of thermal losses quite tired
Difficulty, thus, oil transfer line becomes the vacuum distillation apparatus component with high cost and high technology content, also surrounds and turns there are many patent
Oily line improves.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 can also be attached using improved oil transfer line.The number of lines specifically needed is according to stirred reactor
20 number is determined.
In a preferred embodiment of the present application, as shown in figure 4, above-mentioned stirred reactor 20 includes: stirred reactor
Ontology 22 sucks conduit 21, sucks and is provided with extracting part in conduit 21, and the one end for sucking conduit 21 is exported by recycle stock
113 protrude into inside flash vaporization kettle 110, and the other end for sucking conduit 21 is connected with stirred reactor ontology 22, suck conduit 21 and take out
It takes the material in flash vaporization kettle 110 and material is delivered in stirred reactor ontology 22 and be stirred to react, after material is agitated
Flash vaporization kettle 110 is returned by recycle stock entrance 112.
In above-mentioned preferred embodiment, by setting stirred reactor 20 to comprising protruding into sucking inside flash vaporization kettle 110
The form that conduit 21 is connected with the stirred reactor 20 being arranged in 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 convenient for stirred reactor 20 being tightly adsorbed on flash vaporization kettle
In 110 tower reactor, a kind of outer circulation type sucking response device is formed, can not only realize the stirring and reaction of convention stir reactor
Effect, and the setting of oil transfer line is also reduced, reduce cost of investment.
Setting component inside above-mentioned stirred reactor 20 according to suck conduit 21 to the sucking of material in flash vaporization kettle 110 and
Conveying function is configured, and the specific form that is arranged can rationally can be arranged according to actual needs there are many pattern.At this
Apply in a kind of preferred embodiment, further includes driving agitating element, it is anti-that one end of the driving agitating element sequentially passes through stirring
It answers device ontology 22 and sucks conduit 21 and protrude into inside flash vaporization kettle 110, the other end of agitating element is driven to be connected with driving 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 ontology 22 and suck conduit 21 and protrude into
Inside flash vaporization kettle 110, the other end of stirring shaft 23 is connected with driving device, and the setting of the first agitating paddle 24 drives in stirring
Axis 23 protrudes into one end inside flash vaporization kettle 110.Preferably, the ratio between the length of the first agitating paddle 24 and the internal diameter of flash vaporization kettle 110 are
0.1~0.3:1.For a 2M3Flash vaporization kettle for the first agitating paddle 24 blade length be 100~150mm.Pass through setting
The first agitating paddle 24 inside flash vaporization kettle 110 is protruded into, so that the material in flash vaporization kettle 110 is constantly in the state being stirred, more
Conducive to efficiently separating for gas-liquid phase materials.For above-mentioned flash vaporization kettle, if set the blade length of the first agitating paddle 24 to
30~50mm belongs to slightly the stirring of material in tower reactor so that the agitating paddle belongs to miniature agitating paddle relative to flash vaporization kettle 110
Mixing, avoid the decomposition for causing material and condensation reaction.
The extracting part in sucking conduit 21 in above preferred embodiment is to stir the material sucking in flash vaporization kettle 110
It mixes in reactor body 22, thus, any specific constructive form that can be realized 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 process that simulated hexapod is sucked blood, and sucking is led
Pipe 21 is inserted into flash vaporization kettle 110, is to push blade 211 sucking the extracting part in conduit 21, is pushed the action principle of blade 211
The principle of centrifugal pump or electric fan is the same, the certain angle of blade twist, and there is impetus in when rotation to liquid (or gas).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 and is stirred to react
In device ontology 22.
Stirred reactor ontology 22 in above preferred embodiment is the sucking response kettle with strong stirring function,
The second agitating paddle 221 is provided in stirred reactor ontology 22, the second agitating paddle 221 is connected with stirring shaft 23, and second stirs
It mixes paddle 221 and stirring shaft 23 is drivingly connected.It is highly preferred that there is one or more groups of and stirring to drive on the second agitating paddle 221
The blade 222 disposed in parallel of axis 23.
Above-mentioned stirred reactor ontology 22 passes through the agitating paddle of setting above structure, convenient for that will suck the object that conduit 21 inputs
Material is sheared, is stirred, and generates chemical reaction under the effect of the catalyst, makes macromolecule hydrocarbon substance decomposition small molecule hydrocarbon
Class, and then be conducive to realize the lighting of mink cell focus.Meanwhile the stirred reactor ontology 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 have not only been saved, but also have reduced the loss of material.
Strongly whether the stirring for judging a kind of stirred reactor, can be judged by the watt level of stirring motor.Most
Main judge index has two: first is that mixing speed, if mixing speed doubles, power of motor increases by 8 times (23)；Second is that
The length of stirrer paddle, length double, and power of motor increases by 32 times (25).In a preferred embodiment of the present application,
The revolving speed of above-mentioned second agitating paddle 221 is continuously adjustable for 0 turn/min~1500 turn/min.In addition, another preferably in the application
Embodiment in, the ratio between internal diameter of blade length of above-mentioned second agitating paddle 221 and flash vaporization kettle is 0.6~1.2:1.It is above-mentioned preferred
In embodiment, stirring intensity is improved by improving the speed of agitator of the second agitating paddle 221 and/or increasing blade length, in turn
So that material is decomposed under the effect of the catalyst and react generation small molecule, and is kept away small molecule feeding condensation segment by flash distillation
Exempt from that condensation reaction occurs, to improve deep drawing rate.
It is highly preferred that above-mentioned second agitating paddle 221 and the first agitating paddle 24 are coaxially disposed, mixing direction is identical.But the two
The design of blade is different, and axis direction of first agitating paddle 24 by material along stirring shaft 23 promotes (with centrifugal pump or electric fan
It is identical), and the tangential direction release for the circumference that the second agitating paddle 221 forms material along the second agitating paddle 221 stirring track, two
The launch direction of a agitating paddle material is in 90 degree.
Since the decomposition and condensation of material carry out simultaneously, and condensation course is irreversible, therefore, can only be in the second stirring
When the paddle of paddle is vigorously stirred, so that material is run through Venturi tube and flashed, to make the small molecule decomposed in flash distillation
Escape condensation.And the first agitating paddle 24 primarily serves miniature stirring and material is pushed the work in stirred reactor ontology 22
In the case where being coaxially disposed with, the two, the revolving speed of two agitating paddles is subject to the speed demand of the second agitating paddle 221, i.e., and second
The revolving speed of agitating paddle 221 determines the revolving speed of the first agitating paddle 24.In order to reduce material to the greatest extent when the first agitating paddle 24 stirs
Decomposition or condensation, the width and length of 24 blade of the first agitating paddle can be according to the sliminess 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 ontology 22 is to material
After being stirred to react, can directly by the recycle stock entrance 112 return flash vaporization kettle 110 in, can also by other with follow
The entrance that ring material inlet 112 is connected returns in flash vaporization kettle 110.In a preferred embodiment of the present application, such as Fig. 4 institute
Show, above-mentioned stirred reactor 20 further includes stirring material outlet 25, stirs one end and the recycle stock entrance 112 of material outlet 25
It is connected, the kettle wall that the other end passes through flash vaporization kettle 110 is connected with the inner cavity of flash vaporization kettle 110.Specifically, material outlet 25 is stirred
It can be the Venturi nozzle being arranged on 110 kettle wall of flash vaporization kettle, as shown in figure 3, having common with recycle stock entrance 112
Material inlet end, but there is the channel that penetrates kettle wall different from recycle stock entrance 112.Second in stirred reactor ontology 22
Material after reaction is pushed into this section of Venturi tube by the centrifugal force that 221 strong stirring of agitating paddle generates, then high speed sprays into tower
Achieve the purpose that flash distillation in kettle.
Above-mentioned decompression distillation system further 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, reduce fixed gas discharge it is unstable to not coagulated in subsequent stirred reactor 20
The reaction efficiency of gas causes the oil gas in subsequent tower reactor section 11 and condensation segment 12 to divide unstable.Fixed gas surge tank is set
It sets so that airflow balance, vacustat in entire decompression distillation system operational process, and is discharged without exhaust gas.
In above-mentioned decompression distillation system, stirred reactor 20 is a stirred reactor, both can be carried out physical agitation, may be used also
It is chemically reacted using under the action of catalyst again as a reactor.Wherein, the chemical reaction one that catalyst occurs
It is cracking, i.e. the carbochain of promotion macromolecular hydrocarbon is broken into small molecule hydrocarbon, existing metal oxide
Type catalyst for cracking or natural and artificial zeolite molecules sieve-type catalyst for cracking are suitable for the application.Second is that mending
Hydrogen, it is therefore an objective to which the small molecule hydrocarbon for generating fracture obtains hydrogen atom, becomes stable saturated hydrocarbons, reaches heavy oil lightweight
The purpose of change, existing metal oxide catalyst, for example, the hydrogenation catalyst of group VIII transition metal element, that is, applicable
In the application.That is, the catalyst of the application have the function of cracking and it is appropriate mend hydrogen, the small molecule hydrocarbon after making cracking at
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 reaction of Shi Jinhang.For example, can be added from fixed gas entrance, or in the recycle stock of tower reactor section 11
Outlet 113, which is delivered on the conveyance conduit between stirred reactor 20, adds catalyst, makes catalyst and the object to be mixed reacted
Material is delivered to stirred reactor 20 together, to be catalyzed above-mentioned chemical reaction.In a preferred embodiment of the present application, preferably
Catalyst inlet 26 is additionally provided on 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 steps that the normal pressure base oil from vacuum furnace is inputted to any of the above-described kind of decompression distillation system carries out vacuum distillation processing,
Wherein the step of vacuum distillation processing includes: that 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；Gaseous phase materials carry out distillation processing through the condensation segment 12 of vacuum distillation apparatus 10, are steamed
Evaporate product and fixed gas；Fixed gas is passed through stirred reactor 20, and is mixed with source with the liquid phase material of tower reactor section 11
It is stirred to react, obtains mixed material；Mixed material after being stirred to react is sent into tower reactor section 11 and is evaporated under reduced pressure；Wherein, subtract
Pressure evaporation carries out under the depressurization of decompressor 13 with distillation processing step.
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 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 to distill
The fixed gas generated in tower is fully incorporated stirred reactor 20, is sufficiently mixed stirring with the material sucked out of tower reactor section 11,
Under the action of being stirred to react, the oil gas for changing evaporation process is divided so that fixed gas condensation in part is that liquid form product component returns to tower
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 distillation process
Partial pressure, the airflow balance for finally running system, vacustat are not only discharged from system without exhaust gas, save at exhaust gas
Cost is managed, and increases 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 into
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
The material temperature of general deep drawing rectifying column reduce by 30~50 DEG C, can not only be by being stirred to react raising extracting rate, and reduce
Heating energy consumption, energy-saving effect are obvious.
It in above-mentioned deep drawing technique, is depressurized using the decompressor of vacuum pump etc, specific decompressor goes out
Mouthful pressure size can need rationally be adjusted according to evaporation effect, specific regulating measure can by the revolving speed of vacuum pump come
It realizes.In above-mentioned deep drawing technique, preferably in the outlet pressure for being evaporated under reduced pressure with controlling decompressor 13 in distillation processing step
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 in the reduction vaporization step of above-mentioned deep drawing technique
Depending on based on crude quality, feeding temperature and light oil extracting rate etc. require, equally, the extracting rate of light oil can pass through charging
Temperature and residence time control.In a preferred embodiment of the present 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 sufficiently be evaporated in the period, relatively more
Gas-liquid separation is thoroughly realized, to improve extracting rate.
In above-mentioned deep drawing technique, stirred reactor 20 can basis to the time that is stirred to react of fixed gas and liquid phase material
The difference of crude oil type and quality is reasonably adjusted, and in a preferred embodiment of the present application, this is stirred to react the time and is
(be stirred to react the 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 being stirred to react of the application other than the mixing of physics, there are also the chemical reaction of Hydrocracking, because
And by reacting while stirring, it not only can be shortened mixing time, but also 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 from bottom after extracting light oil.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 to the decompression residuum after 70%~75% light oil has been extracted can further extract 30%~
80% light oil.That is, it is 83%~95% that the deep drawing technique of the application, which can be obtained extracting rate,.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
(standard curve is established by experiment to determine the concrete operations parameter under specific extracting rate) for 83%, is higher by 8 than general deep drawing
Percentage point, economic benefit is quite significant, and what is be discharged subtracts slag, to after common deep drawing to subtract slag amount similar, do not have to change
Any process conditions can be used to subsequent delayed coking；When selecting extracting rate is 95%, then the vacuum distillation of the application
Process reduces subsequent coking process, is expelled directly out about 5% bottom 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 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 following example 1 and 2 is single pot of experiment, it is not continuous experiment.Wherein, embodiment 1 is plus takes
One of the discontinuous expansion experimental record of big UNB university (based on hectogram), embodiment 2 are the discontinuous pilot experiments in Beijing Yanshan Mountain
One of record (based on hundred kilograms).
Embodiment 1
The decompression for using existing vacuum distillation apparatus (extracting rate for 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 room temperature is added in vacuum distillation apparatus of the invention, when temperature of charge reaches 350 DEG C,
Under the nitrogen atmosphere protection of 40ml/min, it is sent into stirred reactor and (adds under the promotion of material the first agitating paddle shown in Fig. 4
Add hydrocracking catalyst) 30min is continuously stirred under the speed of agitator of 650r/min.
Under the nitrogen atmosphere protection of 200ml/min, 350 DEG C at a temperature of, continued with the speed of agitator of 650r/min
60min is continuously stirred, liquid oil 172.7g is obtained.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 entire reaction process, the pressure of Top of Vacuum Tower vacuum pump is maintained between 40~50Kpa.
Embodiment 2
It uses the mixing slurry oil that two catalysis and three catalysis are thrown away in the swallowization FCC apparatus of Beijing for raw material, adopts on this basis
It is handled with vacuum distillation deep drawing technique of the invention as shown in Figure 1.Specific step is as follows:
Heating process: catalytic slurry 320kg is inputted in vacuum distillation apparatus, the set 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 (is added to and adds
Hydrogen catalyst for cracking) it is continuously stirred under the stirring frequency of 0.6HZ.At this point, vacuum pump is also without vacuumizing.
Reaction process: material sustained response 1h at 320 DEG C is vacuumized by vacuum pump, and the fixed gas of extraction is passed through
In fixed gas surge tank, then using fixed gas as the protective gas of reaction process it is passed through the stirring being connected with vacuum distillation apparatus
In reactor.Under this condition, stirred reactor continuously stirs 1h under the stirring frequency of 7.5HZ, pass through the strong of stirred reactor
Power stirring, under the effect of the catalyst, cracking reaction occurs for slurry oil, generates small molecule hydro carbons, enters shell and tube by flash vaporization kettle
Condenser condensation.
Reaction effect: setting 150 DEG C for reaction temperature, temperature of charge from 320 DEG C of declines rapidly, exhaust gas protection do not stop,
It is shut down after continuing 0.2h under the stirring frequency of 0.6HZ, residual gas is evacuated in condenser, obtains liquid 95kg.The embodiment
Liquid yield subtracts after slag enters back into FCC cracking, throws away from cracked fuel oil on the basis of deep drawing 70~75% subtracts slag
The light oil of nearly 30% (95/320=29.7%) has been extracted in catalytic slurry again.
Embodiment 3
Method of the invention creates the design of 1,000,000 tons/year of crude oil atmospheric vacuum distillation devices with Mr. Yu, wherein decompression is steamed
The process flow 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
Furnace and flash vaporization kettle are pulled out normal base oil by flashing one after another 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 analyzed it can be seen that
1) temperature of embodiment 3 is lower 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 needs increased heat are as follows: 2.1MJ/T* DEG C × 45 DEG C
× 550T/h=51975MJ/h.It is equivalent to the calorific value of 1.32 tons of mink cell focuses, if 1 year calculated by 8000 hours, is compareed
Example 1 needs to consume the calorific value of 10560 tons of heavy oil more；If pressing inner accounting valence, decompression residuum valence=ten thousand/ton of $0.18, then
1 year consumption=ten thousand/year of $1900.
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
It will lead to the quality decline of decompression residuum.
3) for relative degree of vacuum, relative degree of vacuum=absolute pressure-locality 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 is 30~
40KPa-100KPa=- (60~70) KPa (is slightly below half of atmospheric pressure -50KPa), true using the more cheap pendular ring of price
Sky pump can be realized；And relative degree of vacuum=1.315KPa-100KPa=-98.685KPa of 1 Top of Vacuum Tower of reference examples (-
100KPa is absolute vacuum, can only theoretically be reached), close to absolute vacuum.So high vacuum degree needs many energy
It can reach and it is necessary to be pumped using vapor jet vacuum, not only capital intensive, operating cost is 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 degree, therefore true boiling-point (TBP) deep drawing cutting temperature=526 DEG C, due in the deep drawing technique of the application in addition to physics
Reaction is outer, additionally uses chemical reaction, therefore the height of extracting rate cannot be evaluated with the height of the true boiling-point (TBP) cutting temperature.
5) due to being pumped using vapor jet vacuum or extracting oil gas using superheated steam, 1 steam consumption of reference examples is
6783kg/h, the price Mu Qian great Yue Shi $160/T of vapor, then reference examples 1 are used for expense=6.783 × 160=of steam
Ten thousand/year of $407/h=$325.6.
6) top vacuum that reference examples 1 propose pumps load=1.32MW, 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 vacuum pump expense in Fu Chu ten thousand/year of $633.6.
7) two reactors of the application stirring need to stir paddle stirring, 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, stirrer paddle length < m/2 meters of (1~1.2), mixing speed
It is 0~300 rev/min, average speed=150 rev/min；Three flash vaporization kettles of reference examples 1 have mixing component (not draw stirring
Motor has certainly) though the length of stirrer paddle is not provided, by taking the first flash vaporization kettle as an example, blade length will be 1.5
~2.0m even more than, mixing speed be 0~600 rev/min, average speed=300 rev/min；According to classical Tian Jinzhi forever
Agitating paddle rating formula, agitating paddle power and revolving speed are in 5 power relationships in 3 power relationships and blade length, and the application is set
The agitating paddle power of motor of meter is 90~120kw, can extrapolate the powers of agitator of reference examples 1 only revolving speed one be exactly this patent
8 times, if considering further that the factor of stirrer paddle, power be it is very big, be often only consumption stirring motor on consumption
Electricity $400~6,000,000/year, this is also a considerable number.
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%, it can
To be directly entered asphalt industry, delayed coking process is eliminated, investment and operating cost are saved perhaps than establishing delayed coking
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 conventional vacuum rectification tower,
It is about 480,000 tons/year of 40% decompression residuum, subsequent to enter delay coking process.
Problem: delay coking process scale is smaller, cannot withstand 480,000 tons/year=60 ton/hours of decompression residuum amount, wishes
Prestige can reduce by about 20 ton/hours of charging, keep the normal operation of coking workshop section.
Proposed adoption scheme:
Scheme one, application scheme (embodiment 4): in the newly-built flash distillation with stirred autoclave in vacuum tower rear portion
Kettle, flash vaporization kettle top products connect condenser and vacuumize, and top products are lightweight wax oil, and bottoms decompression residuum, which enters, to be prolonged
Slow coking process.
Prior art (reference examples 2): scheme two creates the flash vaporization kettle with decompression tower body after atmospheric tower and (claims
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 flashes again, this external application high-temperature gas (nitrogen, hydrogen -80~
400 DEG C) enter flash column assistance air lift.
The comparison result of two schemes is shown in Table 2:
Table 2:
* the numerical value for indicating 158.6~180.0 is calculated according to following formula: 150+ [42.9 × (20%~
70%)].
From equipment, scheme one and scheme two have flash vaporization kettle, but the difference of the two is, the flash vaporization kettle dress of scheme one
Be located at after vacuum distillation apparatus, by material be only to be depressurized that column distillation is remaining to subtract slag, flow is about 60T/h, and side
Case one only has flash vaporization kettle without tower body.Two flash column of scheme is installed in front of vacuum distillation apparatus, in addition to normal base oil will pass through
Except, vacuum tower base oil will also return to 20%~70%.The flash evaporation feed amount from table 2 is it is found that 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 greater than the decompression tower diameter Φ 5200 in existing scheme.
From investment, the two is not much different, and the flash vaporization kettle of scheme one is smaller and does not have tower body, but increases a stirring
Reactor；Two flash vaporization kettle of scheme is larger and has tower body, and vacuum system investment is higher than the former.Both sides balance, investment are not much different.
From the point of view of depressurizing heater outlet temperature, 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 easy condensation and becomes weight, it is therefore necessary to quench oil cooling is added, prevents from being condensed, this is same increase operation at
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 lower than scheme one.
It can be seen from the above description that the application the above embodiments realize following technical effect: a, operation section
Can: using the process of the invention, the general deep drawing rectifying column material temperature of the feeding temperature ratio of normal base oil lowers 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, fixed gas environmental protection: is incorporated to refinery off gas system compared in traditional method
System, burning take the processing method of heat different, and fixed gas is recycled in the application；And liquid-ring vacuum pump does not generate 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 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 generally 60%~70%, if using the application, can from decompression residuum
30% light oil is extracted again, then total extracting rate can be improved 8 percentage points, the benefit is much higher than equipment investment (as general
When vacuum tower tower reactor becomes flash vaporization kettle, residence time of material is elongated, and tower reactor volume increases, and structure is also required to change, and surrounds
There are one tower reactors or several stirred reactors, this increases the additional investment of equipment to a certain extent).If pulled out from subtracting in slag
Out 80%, then for rectification under vacuum process directly instead of coking process, bottom material is substantially pitch, and liquid-phase product quality is much higher than coke
The liquid-phase product of change.
Seen from the above description, it for a newly-built refinery, is steamed using the decompression with deep drawing technology of the application
Evaporate system undoubtedly economy and environmental benefit with higher.For existing refinery, if prior art structure can not be changed,
A set of above-mentioned provided decompression distillation system can also be newly established after existing vacuum distillation apparatus.The decompression newly established is steamed
Evaporate system and the decompression distillation system under the conditions of above-mentioned create has following difference in process conditions: a, inlet feed are not normal pressures
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, the quality, quantity and dress of light oil are considered as
The economic indicators such as investment, running cost are set, depending on comparison；C, the extracting rate of the system still suggests taking two outliers
According to when that is, extracting rate is 30%, the base oil after extracting light oil can be sent into delay coking process；When extracting rate is 80%, bottom
Oil is mainly pitch, can be used directly as road asphalt or solid fuel.
The foregoing is only a preferred embodiment of the present invention, is not intended to restrict the invention, for the skill of this field
For art personnel, the invention may be variously modified and varied.All within the spirits and principles of the present invention, made any to repair
Change, equivalent replacement, improvement etc., should all be included in the protection scope of the present invention.
Claims (21)
1. a kind of decompression distillation system, which is characterized 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) are connected with the tower reactor section (11), for the tower reactor section
(11) material in is stirred and the material is returned to the tower reactor section (11)；
Wherein, the condensation segment (12) passes sequentially through the fixed gas outlet (121) and the decompressor (13) is stirred with described
Reactor (20) is mixed to be connected；
Catalyst inlet (26) are additionally provided on the stirred reactor (20).
2. decompression distillation system according to claim 1, which is characterized 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 outlet (113) and the recycle stock entrance (112) are connected to the flash vaporization kettle (110) to be formed material and is recycled back to
Road.
3. decompression distillation system according to claim 2, which is characterized in that the flash vaporization kettle (110) goes out in the gas phase
Gas phase entrainment block piece (114) is provided at mouth (111).
4. decompression distillation system according to claim 3, which is characterized in that the gas phase entrainment block piece (114)
Including annular boiling liquid baffle (1141) being circumferentially arranged along the inner wall of the flash vaporization kettle (110) and along the flash vaporization kettle (110)
Axial direction setting it is described annular boiling liquid baffle (1141) above blocking umbrella (1142), it is described annular boiling liquid baffle
(1141) there is centre bore, the blocking umbrella (1142) is connected with annular boiling liquid baffle (1141) and is located at the centre bore
Top.
5. decompression distillation system according to claim 2, which is characterized in that the condensation segment (12) is rectifying column, described
Rectifying column includes packed tower, and structured packing is filled in the packed tower.
6. decompression distillation system according to claim 2, which is characterized in that the decompressor (13) is vacuum pump.
7. the decompression distillation system according to any one of claim 2 to 6, which is characterized in that the stirred reactor
(20) include:
Stirred reactor ontology (22),
It sucks conduit (21), extracting part is provided in the sucking conduit (21), described one end for sucking conduit (21) passes through institute
It states recycle stock outlet (113) and protrudes into the flash vaporization kettle (110) inside, the other end for sucking conduit (21) and the stirring
Reactor body (22) is connected, and material in the flash vaporization kettle (110) is extracted and by the material in described suck conduit (21)
It is delivered in stirred reactor ontology (22) and is stirred to react, pass 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, which is characterized in that the stirred reactor (20) further includes driving
One end of agitating element, the driving agitating element sequentially passes through the stirred reactor ontology (22) and the sucking conduit
(21) and the flash vaporization kettle (110) inside is protruded into, the other end of the driving agitating element is connected with driving device.
9. decompression distillation system according to claim 8, which is characterized in that the driving agitating element includes stirring driving
Axis (23) and the first agitating paddle (24), one end of the stirring shaft (23) sequentially pass through the stirred reactor ontology (22)
With the sucking conduit (21) and to protrude into the flash vaporization kettle (110) internal, the other end of the stirring shaft (23) with it is described
Driving device is connected；First agitating paddle (24), which is arranged, protrudes into the flash vaporization kettle (110) in the stirring shaft (23)
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, which is characterized in that the extracting part includes pushing blade
(211), the promotion blade (211) is arranged on the stirring shaft (23) and is located in the sucking conduit (21).
11. decompression distillation system according to claim 9, which is characterized in that set in the stirred reactor ontology (22)
It is equipped with the second agitating paddle (221), second agitating paddle (221) and the stirring shaft (23) are drivingly connected.
12. decompression distillation system according to claim 11, which is characterized in that have one on second agitating paddle (221)
Group or multiple groups blade (222), the blade (222) are arranged in parallel with the stirring shaft (23).
13. decompression distillation system according to claim 12, which is characterized 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, which is characterized in that the stirring of second agitating paddle (221)
Revolving speed is continuously adjustable for 0~1500r/min.
15. decompression distillation system according to claim 7, which is characterized in that the stirred reactor (20) further includes stirring
It mixes material outlet (25), one end of stirring material outlet (25) is connected with the recycle stock entrance (112), the other end
Kettle wall across the flash vaporization kettle (110) is connected with the inner cavity of the flash vaporization kettle (110).
16. decompression distillation system according to claim 1, which is characterized in that the decompression distillation system further includes not solidifying
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. a kind of vacuum distillation deep drawing technique, which is characterized in that the deep drawing technique includes will be from the normal pressure base oil of vacuum furnace
Decompression distillation system described in input any one of claims 1 to 16 carries out the step of vacuum distillation processing, and the decompression is steamed
The step of evaporating processing include:
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 is mixed with the liquid phase material from the tower reactor section (11)
Conjunction is stirred to react, and obtains mixed material；
The mixed material is returned to the tower reactor section (11) to be evaporated under reduced pressure；
Wherein, the step of reduction vaporization is handled with the distillation carries out under the depressurization of decompressor (13).
18. deep drawing technique according to claim 17, which is characterized in that the temperature of the normal pressure base oil is 320 DEG C~380
℃。
19. deep drawing technique according to claim 17, which is characterized in that in the reduction vaporization and the distillation processing
The outlet pressure of decompressor described in step (13) is 10kPa~40kPa.
20. deep drawing technique according to claim 17, which is characterized in that in the reduction vaporization the step of, it is described often
Pressing residence time of the base oil in the tower reactor section (11) is 30min~90min.
21. deep drawing technique according to claim 17, which is characterized in that the stirred reactor (20) is to the fixed gas
The time that is stirred to react with the liquid phase material is 1min~5min.
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| 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 |
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