CN103242886B - Deep reduced pressure flash tank and reduced pressure deep distillation method - Google Patents

Deep reduced pressure flash tank and reduced pressure deep distillation method Download PDF

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CN103242886B
CN103242886B CN201210024897.2A CN201210024897A CN103242886B CN 103242886 B CN103242886 B CN 103242886B CN 201210024897 A CN201210024897 A CN 201210024897A CN 103242886 B CN103242886 B CN 103242886B
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tank
vacuum
reduced pressure
reduced
distillation
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CN201210024897.2A
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CN103242886A (en
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张龙
李经伟
齐慧敏
王海波
王岩
李欣
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中国石油化工股份有限公司
中国石油化工股份有限公司抚顺石油化工研究院
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Abstract

The invention discloses a deep reduced pressure flash tank and a reduced pressure deep distillation method. The reduced pressure flash tank comprises a tank body and internal members of the tank. The internal members comprises a feeding inlet distributor arranged in a gas phase zone at the upper part of the reduced flash tank and a rotary disk arranged above a liquid surface of the lower part liquid phase zone, wherein the rotary disk is fixed on a rotary shaft arranged in an axis direction of the tank body. In the reduced pressure deep distillation method, the reduced pressure flash tank is arranged behind the reduced pressure tower; the atmospheric pressure bottom oil is heated by a reduced pressure furnace and introduced to the reduced pressure tower through a reduced pressure transfer line; reduced pressure light fraction oil is pumped out from the lateral line of the reduced pressure tower; reduced pressure heavy oil is pumped out from the bottom of the tower and introduced to the reduced pressure flash tank; the obtained gas phase is introduced to a gas-liquid separation tank; the reduced pressure light fraction oil is discharged from the bottom of the gas-liquid separation tank; and the flashed reduced pressure residual oil is discharged from the bottom of the reduced pressure flash tank. The deep reduced pressure flash tank and the reduced pressure deep distillation method can obviously increase distillation yield during a distillation process of crude oil, reduce energy consumption during the process and increase economic benefits of the apparatus.

Description

A kind of further depressurized flash tank and deep vacuum distillation method
Technical field
The invention belongs to refining of petroleum field, relate to a kind of further depressurized flash tank and deep vacuum distillation method and apparatus, relate in particular to a kind of crude oil processing method and the device that improve crude oil vacuum distillation process intermediate distillates yield.
Technical background
Refinery crude oil atmospheric vacuum distillation technique is the first operation of refining of petroleum, is the component by the method for distillation crude oil being divided into different boiling range scope, to adapt to product and downstream unit to the processing requirement of raw material.The height of its light oil yield and the size of energy consumption directly affect the economic benefit of refining of petroleum.Usually using < 500 DEG C of cuts in the energy consumption of total extracting rate of device benzoline, device and vacuum residuum or < 538 DEG C of ends content as the index of measurement plant running.The flow process of the conventional many employings of crude oil atmospheric vacuum distillation technique " two stove three towers ": enter primary tower (or flashing tower) after crude oil upgrading, then atmospheric tower is entered through atmospheric pressure kiln heating, oil at the bottom of atmospheric tower delivers to vacuum distillation tower through vacuum furnace heating by pressure-reducing line for oil-transferring, complete the air distillation to crude oil and underpressure distillation, obtain and meet the product of specification of quality and the raw material of downstream unit.
Along with the continuous growth that scientific and technical develop rapidly and social life are consumed, world petroleum demand amount increases year by year along with expanding economy, in crude resources supply, heavy oil and overweight oil supplying ratio progressively increase, and lightweight oil, middle matter oil supplying constant decline.Improve the extracting rate in crude oil atmospheric vacuum distillation, obtain more light oil distillate oil, reduce atmospheric and vacuum distillation unit energy consumption, raising device economic benefit becomes the problem that global Refining Chemical Industry is paid close attention to jointly.And along with the fast development of Chinese national economy, China's oil total quantity consumed is estimated breakthrough 6.5 hundred million tons at the year two thousand twenty, and the external dependence degree of crude oil will reach 50% ~ 60%.Appropriate application crude resources, optimization processing technology has been the imperative act of China's oil chemical industry.In larger-scale unit and Integrated Refinery And Petrochemical novel refinery design, as " tap " crude oil atmospheric vacuum distillation device maximum resource utilization, energy utilization economized, running cost rationalize, size investment optimizing, realize, in the Sustainable development of China's oil chemical industry, there is very important status.Therefore, newly-built crude unit requires higher depth of cut, and in vacuum residuum, less than 500 DEG C ends content are less than 5%(quality), even lower; Many old atmospheric and vacuum distillation unit, while requiring higher cut point, face process scale and can not meet the situation that treatment capacity requires and oil variety constantly changes, need to carry out capacity expansion revamping to device, eliminate " bottleneck ", improve crude distillation ability.
For this reason, Chinese scholars compares deep research to deep vacuum distillation technology, for improving the extracting rate of vacuum fractionation tower, having drawn a series of experience, can be summed up as: (1) adopts advanced vacuum system, improved the vacuum tightness of vacuum fractionation tower top; (2) adopt novel, high efficiency packing, reduce tower internal drop, make flash zone at the bottom of tower keep higher vacuum; (3) improve transfer line design, reduction transfer line Pressure Drop and temperature are fallen; (4) washing section design and operation is optimized, the fractionation concept of strengthening washing section; (5) new and effective gas and liquid distributor etc. are adopted.
Patent US7172686 has delivered a kind of method improving crude distillation distillate yield, and method one extracts gaseous stream out from tower inside cord, and carry out separation and obtain product, a part of gas phase returns in tower; Method two is incoming mixture by boiling point height heating and separating is lighting end, middle runnings, last running, then enters in tower at different feed entrance points respectively and carries out fractionation, extract out successively gently from side line, last running.Method one is equivalent to side line and has added a stripping tower, improves distillate quality.But to a certain degree add plant investment and energy consumption; Method two achieves gently, last running sectional feeding, improve the operation of crude distillation separation column, be conducive to improving distillate yield, but the lighting end of having separated from parallel feeding is sent in tower again carry out fractionation, repetitive operation increases plant energy consumption and does not reduce the load of tower.
Patent CN2242892Y discloses a kind of composite crude oil distillation vacuum distillation tower, is provided with a liquid seal device and top separates, and has a vacuum system interface to be connected with top vacuum system at the bottom of tower.This utility model is separated by the deep drawing section of liquid seal device by the rectifying section of vacuum distillation tower and bottom, oil quality and extracting rate can be paid attention to respectively, can relatively improve decompression extracting rate, but the oil quality of deep drawing is difficult to meet the processing requirement of downstream unit to raw material, the tower structure of this utility model is complicated simultaneously, top vacuum system loading is high, and plant energy consumption relatively can be high.
Patent CN1287872A has delivered a kind of crude oil atmospheric vacuum distillation method with degree of depth stripping process, it is a washing tank in parallel in vacuum distillation tower side, the feed zone of vacuum distillation tower and stripping stage are isolated sparger by fluid-tight and are separated, the oil gas of stripping stage is by entering the bottom of washing tank communicating pipe, take from the absorption oil that vacuum distillation tower subtracts three line dischargings and enter downwards spray and the reverse mass-and heat-transfer of oil gas upwards by washing tank top after cooling, the tank deck oil gas discharging of washing tank returns to the top of vacuum distillation tower, and discharging at the bottom of tank returns vacuum distillation tower as washing oil.This technique makes vacuum distillation tower stripping stage experienced by a steam stripped process of the degree of depth by setting up washing tank, is conducive to improving decompression extracting rate.But the method is just optimized improvement to vacuum distillation tower stripping stage, subtracts third fractional oil preferably as washing oil by quality, economic benefit waits research.
Patent CN1884441A discloses the method improving light oil yield of atmospheric and vacuum distillation of petroleum oil, is added in the crude oil of atmospheric and vacuum distillation of petroleum tower by the additive containing rosin, improves the light oil yield of atmospheric and vacuum distillation by changing the intermolecular reactive force of crude oil.But the method fundamentally changes distillation technique in Technology, and will consume a large amount of additives, add the operation easier of plant running cost and interpolation chemical reagent.
Patent CN101376068A discloses a kind of atmospheric vacuum distillation method with vacuum flasher and equipment, is before long residuum enters vacuum furnace, arrange a vacuum flasher.Oil at the bottom of flashing tower enters heating under reduced pressure stove, and flashing tower top gas enters above or below certain sideline product outlet port close with flashing tower top gas cut.The method improves the flow process of atmospheric and vacuum distillation unit by increasing vacuum flasher, reach raising treatment capacity, improves extracting rate, reduces the object of energy consumption.But oil enters flashing tower at the bottom of atmospheric tower, because at the bottom of atmospheric tower, the temperature of oil is relatively low, the vacuum tightness of adding stokehold flashing tower is relatively not high, the limited use that flashing tower is flash vaporized, and flash distillation top gaseous phase enters vacuum distillation tower, be equivalent to vacuum distillation tower sectional feeding after flash distillation, not in the fractionation fundamentally changing vacuum distillation tower.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of further depressurized flash tank and deep vacuum distillation method and apparatus.Use the present invention can significantly improve the extracting rate in crude oil vacuum distillation process, reduces plant energy consumption, increases device economic benefit.
Reduced-pressure flash tank of the present invention comprises tank body and tank inner member, and tank body is horizontal type structure, and tank length is 2 ~ 5 with the ratio of tank diameter, comprises gas phase zone and the lower liquid phase district on top in tank; Arrange air collector in tank top, air collector is communicated with upper gaseous phase section, inside establishes foam removal net, and connect gas phase discharge port, air collector internal diameter is 20% ~ 70% of tank diameter; Tank inner member is included in the feed distributor that upper gaseous phase section is arranged, the rotating disk thin-film evaporator arranged at liquid level place of lower liquid phase district, rotating disk thin-film evaporator comprises rotating disk and rotating shaft, rotating shaft is horizontally set on the tank body axial direction due in tank body, rotating shaft is 40% ~ 60% of tank diameter apart from the go to the bottom distance of tangent line of tank, and rotating disk is fixed in rotating shaft.20% ~ 70% of rotating disk, preferably 30% ~ 50% is immersed in below the liquid level in Guan Nei lower liquid phase district.Rotating shaft adopts motor to drive or magnetic force driving.
The tank body of reduced-pressure flash tank of the present invention is arranged opening for feed, flash distillation gas phase discharge port and flash distillation liquid phase relief outlet, opening for feed is arranged on tank body upper gaseous phase section, enters along tank body axial direction due, connects feed distributor; Flash distillation gas phase discharge port is arranged on the air collector at tank body top, and flash distillation liquid phase relief outlet is arranged on the bottom of tank body, and there is Liquid level flash tank liquid phase region.
The feed distributor of reduced-pressure flash tank of the present invention is tubulose cellular type sparger, also can adopt the pipe distributor of excellent property.
In reduced-pressure flash tank of the present invention, rotating disk can be screw type rotary dish, also can be the circular plate type rotating disk of multi-disc perpendicular to rotating shaft, the card of rotating disk can arrange some fins, to increase the surface-area forming film.The quantity of rotating disk is determined according to the scale of reduced-pressure flash tank.The pitch of screw type rotary dish or the spacing often between the board-like rotating disk of two panels parallel cylindrical are generally 30 ~ 300mm.
The rotating disk of the rotating disk thin-film evaporator of reduced-pressure flash tank of the present invention is arranged along tank body vertical section radial symmetry, rotating disk equal diameters or successively decrease successively along tank axial direction due to both sides from Guan Nei center, the dish footpath of the rotating disk that tank central position is maximum is 20% ~ 40% of tank diameter.The rotating speed of rotating disk can be determined according to the scale of the character of charging, device and operational requirement, generally can be 5 ~ 500 revs/min.
A kind of deep vacuum distillation method of the present invention comprises following content: oil at the bottom of the atmospheric tower of crude oil after air distillation (hereinafter referred to as oil of the normal end) is heated by vacuum furnace, enters vacuum still carry out underpressure distillation through pressure-reducing line for oil-transferring; From vacuum still lateral line withdrawal function decompression benzoline, at the bottom of vacuum still tower, extract depressed heavy oil out enter a reduced-pressure flash tank; Reduced-pressure flash tank top gas phase (hereinafter referred to as sudden strain of a muscle top gas) connects pumped vacuum systems by knockout drum, maintains the vacuum tightness that reduced-pressure flash tank is higher.Gas-liquid separation pot bottom discharges vacuum distillate, discharges the vacuum residuum after degree of depth flash distillation at the bottom of reduced-pressure flash tank.
In deep vacuum distillation method of the present invention, described reduced-pressure flash tank is the above-mentioned reduced-pressure flash tank arranging rotating disk thin-film evaporator of the present invention.
In deep vacuum distillation method of the present invention, depressed heavy oil enters reduced-pressure flash tank, carries out gas-liquid separation distribution by a feed distributor, and gas phase rises in tank deck air collector and discharged by gas phase discharge port through foam removal net, and liquid phase freely falls to tank liquid phase region.When rotating disk below liquid level forwards ullage to, rotate the gas-phase space that the liquid phase that card is adhered to takes ullage to, the card of rotating disk is formed liquid film district, the liquid film that continuous formation is new, evaporate in a short period of time under the condition of liquid film high vacuum, high temperature in tank, thus more light constituent in residual oil is evaporated, improve the extracting rate of underpressure distillation.
In deep vacuum distillation method of the present invention, the depressed heavy oil of discharging at the bottom of vacuum still tower introduces reduced-pressure flash tank by expanding pipeline step by step, makes the lighting end in vacuum residuum divide pressure to be evaporated at the oil gas reduced step by step, finally in the complete flash distillation of reduced-pressure flash tank.
In deep vacuum distillation method of the present invention, pressure comparatively low 2kPa ~ 5 kPa of vacuum still tower bottom pressure of reduced-pressure flash tank, the depressed heavy oil that vacuum distillation tower is discharged flows into reduced-pressure flash tank by self-pressure.
In deep vacuum distillation method of the present invention, the position of reduced-pressure flash tank height is in vacuum still, and reduced-pressure flash tank opening for feed is positioned at 30% ~ 70% place of liquid level at the bottom of vacuum still tower, and preferably 45% ~ 55%.Ensure that vacuum still can not be evacuated, and prevents liquid phase residual overlong time at the bottom of vacuum still tower from causing coking on the other hand on the one hand.
In deep vacuum distillation method of the present invention, described reduced-pressure flash tank is horizontal tank, to realize the larger flash distillation face of reduced-pressure flash tank.
In deep vacuum distillation method of the present invention, vacuum flashing head space gas phase and the normal end oil or device in need heat logistics heat exchange, reduce plant energy consumption.
In deep vacuum distillation method of the present invention, extracted out the vacuum residuum of degree of depth flash distillation at the bottom of reduced-pressure flash tank tank by pump, liquid automatic control pump discharge flow at the bottom of tank.
In deep vacuum distillation method of the present invention, can arrange a set of pumped vacuum systems, vacuum still and reduced-pressure flash tank share a set of pumped vacuum systems vacuum pumping, can arrange control device, control the vacuum tightness of vacuum still and flash tank respectively; Two cover pumped vacuum systems also can be set, vacuum still and reduced-pressure flash tank vacuum pumping respectively.The vacuum degree control of reduced-pressure flash tank is arranged on the knockout drum after sudden strain of a muscle top gas condenser.The vacuum pumping of reduced-pressure flash tank and vacuum still can adopt the method and apparatus of this area routine.
In deep vacuum distillation method of the present invention, other technology contents, if the design of vacuum furnace, vacuum still, transfer line and operation are technology contents well known to those skilled in the art.
Another technical problem that the present invention solves is to provide a kind of crude oil deep vacuum distillation device improving extracting rate.Technical scheme is: a kind of deep vacuum distillation device, comprise vacuum furnace, transfer line, vacuum still, reduced-pressure flash tank, transfer line connects vacuum furnace and vacuum still, underpressure distillation tower bottom is communicated with reduced-pressure flash tank by pipeline expanding step by step, and vacuum flashing tank top is communicated with pumped vacuum systems by knockout drum.
Wherein said reduced-pressure flash tank is the reduced-pressure flash tank arranging rotating disk thin-film evaporator recited above.
Compared with prior art, the present invention has the following advantages:
1) by arranging reduced-pressure flash tank after vacuum still, making cut relatively light in vacuum residuum obtain flash distillation further, improving the decompression yield of this device on the one hand; Reduce the load of the process such as downstream coking or visbreaking vacuum residuum device on the other hand, reduce the cracking loss of benzoline.
2) working pressure of reduced-pressure flash tank is lower, realizes the complete flash distillation of decompression lighting end, and the cut of < 500 DEG C and < 538 DEG C in vacuum residuum is reduced greatly.
3) adopt the reduced-pressure flash tank of architecture, the light constituent in vacuum residuum is evaporated as much as possible, be conducive to the yield reducing vacuum residuum.
4) reduced-pressure flash tank can be used as the surge tank of discharging pump at the bottom of tower, prevents discharging pump at the bottom of tower from finding time.
5) sudden strain of a muscle top gas and oil of the normal end carry out heat exchange, reduce vacuum furnace load, reduce plant energy consumption.
6) present invention process advanced technology is reasonable, and energy consumption level is low, and vacuum residuum yield is low, for the transformation of old device, have scrap build amount few, invest low, the transformation duration is short, and device income is the advantage such as quick obviously; For the design and construction of new device, have rational technology advanced person, energy consumption level is low, vacuum distillate yield high.
Accompanying drawing explanation
Fig. 1 is a kind of deep vacuum distillation method process flow diagram.
Fig. 2 is reduced-pressure flash tank structural representation of the present invention.
Wherein 1 is oil of the normal end (i.e. oil at the bottom of atmospheric tower); 2 is vacuum furnace; 3 is vacuum still; 4 is transfer line; 5 is depressed heavy oil; 6 is vacuum residuum; 7 is stripped vapor; 8 is pumped vacuum systems; 9 is sideline product discharging; 10 is vacuum distillate; 11 is reduced-pressure flash tank; 12 is flash tank top knockout drum; 13 is reduced-pressure flash tank opening for feed; 14 is rotary evaporation dish; 15 is rotating shaft; 16 is foam removal net; 17 is gaseous phase outlet; 18 is liquid-phase outlet; 19 is air collector; 20 is feed distributor.
Embodiment
The inventive method adopts with the reduced-pressure flash tank of rotating disk thin-film evaporator, oil of the normal end is heated by vacuum furnace, introduces vacuum still carry out the depressed heavy oil after underpressure distillation carry out vacuum flashing under the condition of reduced-pressure flash tank condition of high vacuum degree, high temperature through transfer line.Dodge top gas by tank deck through heat exchange oily with the normal end, then enter knockout drum after water cooler cooling.Gas-liquid separation tank top connects pumped vacuum systems, maintains the vacuum tightness that reduced-pressure flash tank is relatively high; Bottom extracts vacuum distillate out as product.Vacuum residuum is extracted out at the bottom of reduced-pressure flash tank tank.By the outlet connection of depressed heavy oil at the bottom of vacuum still tower reduced-pressure flash tank, reduce the content of < 500 DEG C of cuts and < 538 DEG C of cuts in vacuum residuum as much as possible, reach the requirement of underpressure distillation degree of depth cutting.Present method, to the capacity expansion revamping of old device, when main equipment reuses, can reduce the yield of vacuum residuum, reduces plant energy consumption, increases device economic benefit; To new device, optimize reduced pressure distillation process design, reduce vacuum residuum yield, increase the ton oil profit of device.
As shown in Figure 1, oil of the normal end 1 first enters vacuum furnace 2 after heat exchange raised temperature, after heating temperatures in vacuum furnace is to 400 DEG C ~ 420 DEG C after transfer line 4 three grades of expanding decompressions, oil gas rate of the normal end reaches 45% ~ 55%(mass percent, lower same), then enter the flash zone of vacuum still 3, under the effect of stripped vapor 7 and underpressure distillation tower top pumped vacuum systems 8, carry out underpressure distillation, obtain sideline product discharging 9 in tower.Depressed heavy oil 5 is by discharging at the bottom of vacuum still tower, and introduce reduced-pressure flash tank 11 through expanding pipeline step by step, under the condition of reduced-pressure flash tank high vacuum, the depressed heavy oil of high temperature obtains further flash distillation.Dodge top gas and enter knockout drum 12 after heat exchange cooling, separating tank top connects pumped vacuum systems, maintains the vacuum tightness that reduced-pressure flash tank 11 is higher, extracts vacuum distillate 10 out as product discharge bottom separating tank.Reduced-pressure flash tank liquid phase is extracted out by the bottom of tank, as vacuum residuum 6 discharging.
Reduced-pressure flash tank 11, vacuum still 3 and knockout drum 12 have Level Detection to show respectively.
Vacuum still described in the present invention can be fuel type vacuum still, also can be Lube Type vacuum still; Can be wet distiller, also can decline wet distiller; Sideline product discharging number is specifically arranged as required.
The present invention, when device goes into operation, can open large vacuum furnace load, and heating is fed to 390 DEG C ~ 400 DEG C, ensures underpressure distillation operation.Go into operation after stablizing, the sensible heat and the latent heat that make full use of high temperature sudden strain of a muscle top gas heat to oil of the normal end, and can reduce the load of vacuum furnace, implement device is energy-conservation.
By reference to the accompanying drawings 2, temperature is that the depressed heavy oil 5 of 380 DEG C ~ 400 DEG C enters reduced-pressure flash tank 11 by reduced-pressure flash tank opening for feed 13, preliminary gas-liquid separation is carried out through feed distributor 20, gas phase rises to air collector 19 and discharges from flash tank sudden strain of a muscle top gaseous phase outlet 17 through foam removal net 16, liquid phase drops to flash tank liquid phase region, under the drive of rotating shaft 15, helical disk 14 is carried to ullage the liquid below liquid level, in helical disk card or helical disk superjacent air space formed liquid film district, liquid film is high vacuum in tank, evaporate in a short period of time under the condition of high temperature, the lighting end in residual oil is made fully to be evaporated to gas phase, through carrying out mass transfer with the residual oil liquid phase declined, after heat transfer, discharge from flash tank gaseous phase outlet 17 with sudden strain of a muscle top gas.Be not deposited at the bottom of flash tank by the material evaporated, send from reduced-pressure flash tank liquid-phase outlet 18.
With the deep vacuum distillation method of reduced-pressure flash tank after vacuum still of the present invention, improve crude oil reduced pressure distillation process, vacuum furnace heating and gasifying, the parallel feeding of the expanding decompression of transfer line afterwards containing 45% ~ 55% gas phase carries out underpressure distillation in vacuum still, obtains vacuum distillation tower sideline product.The reduced-pressure flash tank that depressed heavy oil at the bottom of tower enters condition of high vacuum degree carries out further flash distillation, cut relatively light in depressed heavy oil is flashed off completely, ensure that the ends content of < 500 DEG C in vacuum residuum is reduced to minimum, thus improve the extracting rate of underpressure distillation, increase the economic benefit of device.Confirm through the analog calculation of Aspen process simulation software, process the vacuum residuum yield few 1% ~ 2% of the identical more existing operational path of raw material present invention process method.
Below by specific embodiment, method of the present invention is described in detail.In embodiment and comparative example, data are that the analog calculation of Aspen process simulation software obtains.
Embodiment 1
Method of the present invention is used for the design of certain newly-built crude oil atmospheric vacuum distillation device, and relief portion division technique flow process is identical with shown in accompanying drawing 1.
The treatment capacity of reliever is 5,500,000 tons/year, and decompression flow process comprises vacuum furnace, vacuum still, reduced-pressure flash tank.Vacuum still is regular packed tower, and adopt wet process operation, tower bottom blowing vapour amount is 1% of tower charging, and tower top working pressure is 2 kPa, and full tower pressure drop is 685kPa.Vacuum flashing pressure tank is 1.2 kPa.Described reduced-pressure flash tank is a kind of reduced-pressure flash tank (as shown in Figure 2) with spiral isometrical rotating disk thin-film evaporator.The long L of tank is 3 times of tank diameter D1, and air collector internal diameter D2 is 50% of tank diameter D1.Rotating disk dish footpath d is 30% of tank diameter D1, and 40% of rotating disk is immersed in the liquid level in Guan Nei lower liquid phase district, and rotating shaft is 50% of tank diameter apart from the go to the bottom distance h of tangent line of tank.
Oil of the normal end 1 is fed into vacuum distillation apparatus with 655 tons/hour, after vacuum furnace 2 is heated to 420 DEG C, enter into vacuum still 3 by pressure-reducing line for oil-transferring transition section 4.Reduced-pressure flash tank is directly connected with discharging at the bottom of vacuum distillation tower tower, and flash tank pressure is 1.2 kPa.Dodge after adiabatic flash that top gas accounts for discharging at the bottom of vacuum still tower 1.41%, at the bottom of reduced-pressure flash tank, oil is as vacuum residuum discharging.From vacuum distillation tower lateral line withdrawal function product 9.Vacuum residuum is 36.13%(quality to the yield of combined feed total feed), the cut point of decompressed wax oil reaches 593 DEG C.
Comparative example 1
Relate to the design of the newly-built 1,000 ten thousand tons/year of crude oil atmospheric vacuum distillation devices of embodiment 1 equally.The treatment capacity of reliever is 5,000,000 tons/year.Adopt the atmospheric vacuum distillation method with vacuum flasher disclosed in CN101376068A.Under same feedstock, processing condition, vacuum residuum is 37.64% to the yield of combined feed total feed, and decompressed wax oil cut point is 565 DEG C, and deep drawing degree is not as good as the present invention.
Embodiment 2
Method of the present invention is used for the capacity expansion revamping of certain Atmospheric Vacuum Unit, normal pressure part is identical with conventional atmospheric and vacuum distillation unit, decompression part adopts the crude oil processing method process flow diagram shown in accompanying drawing 1, mainly comprises vacuum furnace, vacuum distillation tower distillation, reduced-pressure flash tank.Vacuum still is regular packed tower, and adopt wet process operation, tower bottom blowing vapour amount is 1% of tower charging, and tower top working pressure is 2 kPa, and full tower pressure drop is 685Pa.Vacuum flashing pressure tank is 1.2 kPa.Further depressurized flash tank is a kind of reduced-pressure flash tank (as shown in Figure 2) with spiral isometrical rotating disk thin-film evaporator.The long L of tank is 3 times of tank diameter D1, and the internal diameter D2 of air collector is 50% of tank diameter D1.Rotating disk dish footpath d is 30% of tank diameter D1, and 40% of rotating disk is immersed in the liquid level in Guan Nei lower liquid phase district, and rotating shaft is 50% of tank diameter apart from the go to the bottom distance h of tangent line of tank.
Oil of the normal end 1 is fed into vacuum distillation apparatus with 655 tons/hour, after vacuum furnace 2 is heated to 420 DEG C, enter into vacuum still 3 by pressure-reducing line for oil-transferring transition section 4.Reduced-pressure flash tank is directly connected with discharging at the bottom of vacuum distillation tower tower, and flash tank pressure is 1.2 kPa.Dodge after adiabatic flash that top gas accounts for discharging at the bottom of vacuum still tower 1.38%, at the bottom of reduced-pressure flash tank, oil is as vacuum residuum discharging.From vacuum distillation tower lateral line withdrawal function product 9.Vacuum residuum is 36.13%(quality to the yield of combined feed total feed), the cut point of decompressed wax oil reaches 593 DEG C.
This device capacity expansion revamping relief portion is divided and is retained original vacuum furnace and vacuum distillation tower, transforms vacuum distillation tower internals and filler.Newly-increased main equipment is reduced-pressure flash tank, oil charging/sudden strain of a muscle top gas interchanger of the normal end.After transformation, vacuum residuum yield reduces by 1% ~ 1.5%.
Comparative example 2
Relate to the capacity expansion revamping of certain crude oil atmospheric vacuum distillation device in embodiment 2 equally.The atmospheric vacuum distillation method with vacuum flasher disclosed in CN101376068A is adopted to carry out capacity expansion revamping.
Under same feedstock, processing condition, vacuum residuum is 37.64% to the yield of combined feed total feed, and decompressed wax oil cut point is 565 DEG C, and deep drawing degree is not as good as the present invention.
Calculate by 1,000 ten thousand tons/year of atmospheric and vacuum distillation unit, relief portion divides charging to be about 655 tons/hour, embodiment 2 reduces yield of residual oil 1.5%, and come in residual oil and mixed gatch price difference 300 yuan/ton, year amounts to Renminbi: 655 × 1.5% × 300 × 8400=2475.9 ten thousand yuan.Add the part that device reduces energy consumption, the device economic benefit highly significant obtained.

Claims (13)

1. a deep vacuum distillation method, comprises following content: at the bottom of the atmospheric tower of crude oil after air distillation, oil is heated by vacuum furnace, enters vacuum still carry out underpressure distillation through pressure-reducing line for oil-transferring; From vacuum still lateral line withdrawal function decompression benzoline, the depressed heavy oil of discharging at the bottom of vacuum still tower introduces a reduced-pressure flash tank by expanding pipeline step by step; Reduced-pressure flash tank top gas phase connects pumped vacuum systems by knockout drum, maintains the vacuum tightness that reduced-pressure flash tank is higher; Gas-liquid separation pot bottom discharges vacuum distillate, discharges the vacuum residuum after flash distillation at the bottom of reduced-pressure flash tank;
Wherein said reduced-pressure flash tank comprises tank body and tank inner member, tank body is horizontal type structure, the gas phase zone on top and the liquid phase region of bottom is comprised in tank, it is characterized in that, tank inner member is included in the feed distributor that upper gaseous phase section is arranged, the rotating disk thin-film evaporator arranged at liquid level place of lower liquid phase district, and rotating disk thin-film evaporator comprises rotating disk and rotating shaft, rotating shaft is horizontally set on the tank body axial direction due in tank body, and rotating disk is fixed in rotating shaft;
The position height of described reduced-pressure flash tank is in vacuum still, and reduced-pressure flash tank opening for feed is positioned at 30% ~ 70% place of liquid level at the bottom of vacuum still tower.
2. in accordance with the method for claim 1, it is characterized in that, described depressed heavy oil enters reduced-pressure flash tank, carries out gas-liquid separation distribution by feed distributor, gas phase rises in tank deck air collector and is discharged by gas phase discharge port through foam removal net, and liquid phase freely falls to tank liquid phase region.
3. in accordance with the method for claim 1, it is characterized in that, pressure comparatively low 2 kPa ~ 5 kPa of vacuum still tower bottom pressure of described reduced-pressure flash tank.
4. in accordance with the method for claim 1, it is characterized in that, in oil at the bottom of vacuum flashing head space gas phase and atmospheric tower or device, need the logistics heated to carry out heat exchange.
5. in accordance with the method for claim 1, it is characterized in that, arrange a set of pumped vacuum systems, vacuum still and reduced-pressure flash tank share a set of pumped vacuum systems vacuum pumping, control device is set, controls the vacuum tightness of vacuum still and reduced-pressure flash tank respectively.
6. in accordance with the method for claim 1, it is characterized in that, arrange two cover pumped vacuum systems, vacuum still and reduced-pressure flash tank vacuum pumping respectively, the vacuum degree control of reduced-pressure flash tank is arranged on the knockout drum after vacuum flashing head space gas condenser.
7. in accordance with the method for claim 1, it is characterized in that, arrange air collector in tank top, air collector is communicated with upper gaseous phase section, inside establishes foam removal net, connects gas phase discharge port.
8. in accordance with the method for claim 1, it is characterized in that, 20% ~ 70% of described rotating disk is immersed in below the liquid level in Guan Nei lower liquid phase district.
9. in accordance with the method for claim 1, it is characterized in that, described rotating disk is screw type rotary dish or the multi-disc circular plate type rotating disk perpendicular to rotating shaft.
10. in accordance with the method for claim 1, it is characterized in that, the card of described rotating disk arranges some fins, to increase the surface-area forming film.
11. in accordance with the method for claim 1, it is characterized in that, described rotating disk is along the arrangement of tank body vertical section radial symmetry, and rotating disk equal diameters or successively decrease successively along tank axial direction due to both sides from Guan Nei center, the maximum rotating disk diameter in tank central position is 20% ~ 40% of tank diameter.
12. in accordance with the method for claim 7, it is characterized in that, described tank body is arranged opening for feed, flash distillation gas phase discharge port and flash distillation liquid phase relief outlet, opening for feed is arranged on tank body upper gaseous phase section, enters along tank body axial direction due, connects feed distributor; Flash distillation gas phase discharge port is arranged on the air collector at tank body top, and flash distillation liquid phase relief outlet is arranged on the bottom of tank body, and there is Liquid level flash tank liquid phase region.
13. in accordance with the method for claim 1, it is characterized in that, described feed distributor is tubulose cellular type sparger or pipe distributor.
CN201210024897.2A 2012-02-06 2012-02-06 Deep reduced pressure flash tank and reduced pressure deep distillation method CN103242886B (en)

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Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1089298A (en) * 1992-11-30 1994-07-13 布斯公司 The deep processing technology of vacuum residuum in the crude oil refinery
CN102311769A (en) * 2010-07-07 2012-01-11 中国石油化工股份有限公司 Reduced-pressure flash tank and crude oil processing method

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1089298A (en) * 1992-11-30 1994-07-13 布斯公司 The deep processing technology of vacuum residuum in the crude oil refinery
CN102311769A (en) * 2010-07-07 2012-01-11 中国石油化工股份有限公司 Reduced-pressure flash tank and crude oil processing method

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