CN103242886A - 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 PDFInfo
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- CN103242886A CN103242886A CN2012100248972A CN201210024897A CN103242886A CN 103242886 A CN103242886 A CN 103242886A CN 2012100248972 A CN2012100248972 A CN 2012100248972A CN 201210024897 A CN201210024897 A CN 201210024897A CN 103242886 A CN103242886 A CN 103242886A
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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
Technical field
The invention belongs to the refining of petroleum field, relate to a kind of further depressurized flash tank and decompression deep drawing method and apparatus, relate in particular to a kind of crude oil working method and device that improves crude oil vacuum distillation process intermediate distillates yield.
Technical background
Refinery crude oil atmospheric vacuum distillation technology is first procedure of refining of petroleum, is that the method by distillation is divided into the component of different boiling range scopes with crude oil, to adapt to product and downstream unit to the processing requirement of raw material.The size of the height of its light oil yield and energy consumption directly influences the economic benefit of refining of petroleum.Usually in the energy consumption and vacuum residuum with total extracting rate of device benzoline, device＜500 ℃ of cuts or＜538 ℃ of cut content are as the indexs of weighing the device operation.Conventional crude oil atmospheric vacuum distillation technology adopts the flow process of " two stoves, three towers " more: enter primary tower (or flashing tower) after the crude oil upgrading, enter atmospheric tower through the atmospheric pressure kiln heating then, oil is delivered to vacuum distillation tower through the vacuum furnace heating by pressure-reducing line for oil-transferring at the bottom of the atmospheric tower, finish air distillation and underpressure distillation to crude oil, obtain to satisfy the product of specification of quality and the raw material of downstream unit.
Continuous growth along with scientific and technical develop rapidly and social life consumption, the world oil demand is along with expanding economy increases year by year, heavy oil and overweight oil supplying ratio progressively increase in the crude resources supply, and lightweight oil, middle matter oil supplying ratio continue to descend.Improve the extracting rate in the crude oil atmospheric vacuum distillation, obtain more light oil distillate oil, reduce the atmospheric and vacuum distillation unit energy consumption, improve the device economic benefit and become the common problem of paying close attention to of global refinery industry.And along with the fast development of Chinese national economy, the China's oil total quantity consumed is estimated to break through 6.5 hundred million tons at the year two thousand twenty, and the external interdependency of crude oil will reach 50%～60%.Rationally utilize crude resources, optimizing complete processing has been the imperative act of China's oil chemical industry.In device maximization and the integrated novel refinery design of refinery, crude oil atmospheric vacuum distillation device as " tap " rationalizes at utilization of resources maximization, energy utilization economized, running cost, the size investment optimizing, has critical role in the Sustainable development of realization China's oil chemical industry.Therefore, newly-built crude unit requires higher depth of cut, and cut content below 500 ℃ is less than the 5%(quality in the vacuum residuum), in addition lower; Many old atmospheric and vacuum distillation unit face process scale and can not satisfy the situation that treatment capacity requires and oil variety constantly changes when requiring higher cut point, need carry out capacity expansion revamping to device, eliminate " bottleneck ", improve the crude distillation ability.
For this reason, Chinese scholars compares deep research to decompression deep drawing technology, for improving the extracting rate of vacuum fractionation tower, has drawn a series of experience, and can be summed up as: (1) adopts advanced vacuum system, improves the vacuum tightness of vacuum fractionation cat head; (2) adopt novel, high efficiency packing, reduce the tower internal drop, make that flash zone keeps higher vacuum at the bottom of the tower; (3) improve the transfer line design, reduction transfer line pressure falls with temperature and falls; (4) optimize washing section design and operation, strengthen the fractionation concept of washing section; (5) adopt new and effective gas and liquid distributor etc.
Patent US7172686 has delivered a kind of method that improves crude distillation distillate yield, and method one is to extract gaseous stream out from the tower inside cord, separates obtaining product, and a part of gas phase is returned in the tower; Method two is incoming mixture by boiling point height heating and separating is lighting end, middle runnings, last running, enter at different feed entrance points respectively then and carry out fractionation in the tower, from side line extract out successively gently, last running.Method one is equivalent to side line and has added a stripping tower, has improved the distillate quality.But plant investment and energy consumption have to a certain degree been increased; Method two has been realized gently, the last running sectional feeding, improved the operation of crude distillation separation column, be conducive to improve the distillate yield, carry out fractionation in the tower but the lighting end of having separated sent into again from parallel feeding, 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 at the bottom of the tower and separates, and have a vacuum system interface to link to each other with the top vacuum system.This utility model separates the rectifying section of vacuum distillation tower and the deep drawing section of bottom by liquid seal device, oil quality and extracting rate can be paid attention to respectively, can relatively improve the decompression extracting rate, but the oil quality of deep drawing is difficult to satisfy downstream unit to the processing requirement of raw material, the tower structure complexity of this utility model simultaneously, top vacuum system loading height, plant energy consumption relatively can be high.
Patent CN1287872A has delivered a kind of crude oil atmospheric vacuum distillation method that has degree of depth stripping process, be at vacuum distillation tower side washing tank in parallel, 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 after cooling off, enter downward spray and the reverse mass-and heat-transfer of oil gas that makes progress by washing tank top, the top of vacuum distillation tower is returned in the tank deck oil gas discharging of washing tank, and a jar end discharging is returned vacuum distillation tower as washing oil.This technology makes the vacuum distillation tower stripping stage experience a steam stripped process of the degree of depth by setting up washing tank, is conducive to improve the decompression extracting rate.But this method has just carried out optimizing improvement to the vacuum distillation tower stripping stage, subtracts third fractional oil preferably as washing oil with quality, waits research in economic benefit.
Patent CN1884441A discloses the method that improves light oil yield of atmospheric and vacuum distillation of petroleum oil, and the additive that will contain rosin is added in the crude oil of atmospheric and vacuum distillation of petroleum tower, by changing the light oil yield that the intermolecular reactive force of crude oil improves atmospheric and vacuum distillation.But this method does not fundamentally change distillation technique in Technology, and will consume a large amount of additives, the operation easier that has increased device running cost and added chemical reagent.
Patent CN101376068A discloses a kind of atmospheric vacuum distillation method and equipment that has vacuum flasher, is that a vacuum flasher is set before long residuum is gone into vacuum furnace.The oil process furnace that advances to reduce pressure at the bottom of the flashing tower, flash distillation overhead gas enter that certain sideline product close with flash distillation overhead gas cut extract out mouthful above or below.This method reaches the raising treatment capacity by increasing the flow process that vacuum flasher improves atmospheric and vacuum distillation unit, improves extracting rate, the purpose that cuts down the consumption of energy.But oil is gone into flashing tower at the bottom of the atmospheric tower, because the temperature of oil is relatively low at the bottom of the atmospheric tower, the vacuum tightness of adding the stokehold flashing tower is not high relatively, the effect of flashing tower flash distillation gasification is limited, and flash distillation cat head gas phase is gone into vacuum distillation tower, be equivalent to vacuum distillation tower sectional feeding after the flash distillation, not in the fractionation that fundamentally changes vacuum distillation tower.
Summary of the invention
At the deficiencies in the prior art, the invention provides a kind of further depressurized flash tank and decompression deep drawing method and apparatus.Use the present invention can obviously improve the extracting rate in the crude oil vacuum distillation process, reduces plant energy consumption, increases the device economic benefit.
Vacuum flashing jar of the present invention comprises tank body and jar inner member, and tank body is horizontal type structure, and a jar long ratio with tank diameter is 2～5, comprises gas phase zone and the bottom liquid phase region on top in jar; The gather qi together device is set in the tank top, and the gather qi together device is communicated with upper gaseous phase section, in establish the foam removal net, connect the gas phase discharge port, gather qi together device internal diameter is 20%～70% of tank diameter; The jar inner member is included in the feed distributor that upper gaseous phase section arranges, the rotating disk thin-film evaporator that arranges at liquid phase region liquid level place, bottom, the rotating disk thin-film evaporator comprises rotating disk and rotating shaft, rotating shaft is horizontally set on the tank body axial direction due in the tank body, rotating shaft is 40%～60% of tank diameter apart from the go to the bottom distance of tangent line of jar, and rotating disk is fixed in the rotating shaft.20%～70% of rotating disk, preferred 30%～50% is immersed in jar below the liquid level of interior bottom liquid phase region.Electric motor driving or magnetic force driving are adopted in rotating shaft.
Opening for feed, flash distillation gas phase discharge port and flash distillation liquid phase relief outlet are set on the tank body of vacuum flashing jar of the present invention, and opening for feed is arranged on the tank body upper gaseous phase section, enters along the tank body axial direction due, connects feed distributor; Flash distillation gas phase discharge port is arranged on the gather qi together device at tank body top, and flash distillation liquid phase relief outlet is arranged on the bottom of tank body, and the flash tank liquid phase region has liquid level control.
The feed distributor of vacuum flashing jar of the present invention is tubulose cellular type sparger, also can adopt the pipe distributor of excellent property.
In the vacuum flashing jar of the present invention, rotating disk can be spiral rotating disk, also can be multi-disc perpendicular to the circular plate type rotating disk of rotating shaft, on the card of rotating disk some fins can be set, increase to form the surface-area of film.The quantity of rotating disk is determined according to the scale of vacuum flashing jar.Spacing between the pitch of spiral rotating disk or the per two board-like rotating disks of parallel cylindrical is generally 30～300mm.
The rotating disk of the rotating disk thin-film evaporator of vacuum flashing jar of the present invention is arranged along tank body vertical section radial symmetry, the rotating disk equal diameters or in the jar center successively decrease successively to both sides along the jar axial direction due, the disk track of the rotating disk of jar central position maximum is 20%～40% of tank diameter.The rotating speed of rotating disk can be determined according to the character of charging, scale and the operational requirement of device, generally can be 5～500 rev/mins.
A kind of decompression deep drawing of the present invention method comprises following content: crude oil oil (to call oil of the normal end in the following text) at the bottom of the atmospheric tower after the normal pressure distillation is entered vacuum still through pressure-reducing line for oil-transferring and is carried out underpressure distillation by the vacuum furnace heating; Extract the decompression benzoline out from the vacuum still side line, extract depressed heavy oil out at the bottom of the underpressure distillation Tata to enter a vacuum flashing jar; Vacuum flashing tank top gas phase (dodging top gas to call in the following text) connects pumped vacuum systems by knockout drum, keeps the higher vacuum tightness of vacuum flashing jar.The gas-liquid separation pot bottom is discharged vacuum distillate, the vacuum residuum at the bottom of the vacuum flashing jar after the flash distillation of the discharge degree of depth.
The present invention is reduced pressure in the deep drawing method, and described vacuum flashing jar is the above-mentioned vacuum flashing jar that the rotating disk thin-film evaporator is set of the present invention.
The present invention is reduced pressure in the deep drawing method, and depressed heavy oil enters the vacuum flashing jar, carries out gas-liquid separation by a feed distributor and distributes, and gas phase rises in the tank deck gather qi together device and discharged by the gas phase discharge port through the foam removal net, and liquid phase freely falls to a jar liquid phase region.When the rotating disk of liquid level below forwards the liquid level top to, the liquid phase of adhering on the rotation card is taken the gas-phase space of liquid level top to, card at rotating disk forms the liquid film district, constantly form new liquid film, evaporation in a short period of time under the condition of liquid film high vacuum, high temperature in jar, more light constituent is evaporated in the residual oil thereby make, and has improved the extracting rate of underpressure distillation.
The present invention is reduced pressure in the deep drawing method, and the depressed heavy oil of discharging at the bottom of the underpressure distillation Tata is introduced the vacuum flashing jar by hole enlargement pipeline step by step, lighting end in the vacuum residuum is depressed at the oil gas branch that reduces step by step be evaporated, finally in the complete flash distillation of vacuum flashing jar.
The present invention is reduced pressure in the deep drawing method, and the pressure of vacuum flashing jar is than the low 2kPa of vacuum still tower bottom pressure～5 kPa, and the depressed heavy oil that vacuum distillation tower is discharged is by going into the vacuum flashing jar from baric flow.
The present invention is reduced pressure in the deep drawing method, and the position height of vacuum flashing jar is in vacuum still, and vacuum flashing jar opening for feed is positioned at 30%～70% place of liquid level at the bottom of the underpressure distillation Tata, preferred 45%～55%.On the one hand guarantee that vacuum still can not be evacuated, prevent the underpressure distillation Tata on the other hand at the bottom of the liquid phase residual overlong time cause coking.
The present invention is reduced pressure in the deep drawing method, and described vacuum flashing jar is horizontal tank, to realize the bigger flash distillation face of vacuum flashing jar.
The present invention is reduced pressure in the deep drawing method, needs the logistics heat exchange of heating in vacuum flashing tank deck gas phase and oil of the normal end or the device, reduces plant energy consumption.
The present invention is reduced pressure in the deep drawing method, is extracted out the vacuum residuum of degree of depth flash distillation at the bottom of the vacuum flashing jar jar by pump, jar end liquid automatic control pump discharge flow.
The present invention is reduced pressure in the deep drawing method, and a cover pumped vacuum systems can be set, and vacuum still and vacuum flashing jar share a cover pumped vacuum systems vacuum pumping, and control device can be set, and control the vacuum tightness of vacuum still and flash tank respectively; Two cover pumped vacuum systems also can be set, the vacuum pumping respectively of vacuum still and vacuum flashing jar.The vacuum degree control of vacuum flashing jar is arranged on dodges on the top gas condenser knockout drum afterwards.The vacuum pumping of vacuum flashing jar and vacuum still can be adopted the method and apparatus of this area routine.
The present invention is reduced pressure in the deep drawing method, and other technology contents is technology contents well known to those skilled in the art as design and the operation of vacuum furnace, vacuum still, transfer line.
Another technical problem that the present invention solves provides a kind of crude oil decompression deep drawing device that improves extracting rate.Technical scheme is: a kind of decompression deep drawing device, comprise vacuum furnace, transfer line, vacuum still, the vacuum flashing jar, transfer line connects vacuum furnace and vacuum still, the underpressure distillation tower bottom is communicated with the vacuum flashing jar by the pipeline of hole enlargement step by step, and the vacuum flashing tank top is communicated with pumped vacuum systems by knockout drum.
Wherein said vacuum flashing jar is the vacuum flashing jar that the rotating disk thin-film evaporator is set recited above.
Compared with prior art, the present invention has the following advantages:
1) by the vacuum flashing jar is set behind vacuum still, make in the vacuum residuum relatively that lighter cut further obtains flash distillation, improve the decompression yield of this device on the one hand; Reduce downstream coking or visbreaking etc. on the other hand and handle the load of vacuum residuum device, reduce the cracking loss of benzoline.
2) working pressure of vacuum flashing jar is lower, realizes the complete flash distillation of decompression lighting end, make in the vacuum residuum＜cuts of 500 ℃ and＜538 ℃ reduce greatly.
3) adopt the suitable vacuum flashing jar of structure, the light constituent in the vacuum residuum is evaporated as much as possible, be conducive to reduce the yield of vacuum residuum.
4) the vacuum flashing jar can be used as the surge tank of discharging pump at the bottom of the tower, prevent tower at the bottom of discharging pump find time.
5) dodge top gas and carry out heat exchange with oil of the normal end, reduced the vacuum furnace load, reduce plant energy consumption.
6) Technology of the present invention is rationally advanced, and energy consumption level is low, and the vacuum residuum yield is low, for the transformation of old device, has that the scrap build amount is few, investment is low, and it is short to transform the duration, and the device income is advantage such as quick obviously; For the design and construction of new device, it is rationally advanced to have technology, and energy consumption level is low, characteristics such as vacuum distillate yield height.
Description of drawings
Fig. 1 is a kind of decompression deep drawing method process flow diagram.
Fig. 2 is vacuum flashing jar structure synoptic diagram of the present invention.
Wherein 1 is oil of the normal end (be atmospheric tower at the bottom of oil); 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 the sideline product discharging; 10 is vacuum distillate; 11 are the vacuum flashing jar; 12 are flash distillation tank deck knockout drum; 13 are vacuum flashing jar opening for feed; 14 is the rotary evaporation dish; 15 are rotating shaft; 16 are the foam removal net; 17 is gaseous phase outlet; 18 are the liquid phase outlet; 19 is the gather qi together device; 20 is feed distributor.
Embodiment
The inventive method adopts the vacuum flashing jar that has the rotating disk thin-film evaporator, makes oil of the normal end carry out vacuum flashing by the depressed heavy oil that vacuum furnace heats, introduces after vacuum still carries out underpressure distillation through transfer line under the condition of vacuum flashing jar condition of high vacuum degree, high temperature.Dodge top gas by tank deck warp and the oil heat exchange of the normal end, after the water cooler cooling, enter knockout drum again.The gas-liquid separation tank top connects pumped vacuum systems, keeps the higher relatively vacuum tightness of vacuum flashing jar; The bottom is extracted vacuum distillate out as product.Vacuum residuum is extracted out at the bottom of vacuum flashing jar jar.Connect a vacuum flashing jar by depressed heavy oil at the bottom of underpressure distillation Tata outlet, reduce as much as possible in the vacuum residuum＜content of 500 ℃ of cuts and＜538 ℃ of cuts, reach the requirement of underpressure distillation degree of depth cutting.Present method under the situation that main equipment reuses, can reduce the yield of vacuum residuum to the capacity expansion revamping of old device, reduces plant energy consumption, increases the device economic benefit; To new device, optimized the reduced pressure distillation process design, reduce the vacuum residuum yield, increase the oily profit of ton of device.
As shown in Figure 1, oil of the normal end 1 enters vacuum furnace 2 earlier after heat exchange rising temperature, temperature is heated to 400 ℃～420 ℃ by after 4 three grades of hole enlargement decompressions of transfer line in vacuum furnace, oil vaporization rate of the normal end reaches 45%～55%(mass percent, down together), enter the flash zone of vacuum still 3 then, under the effect of stripped vapor 7 and underpressure distillation cat head pumped vacuum systems 8, carry out underpressure distillation, obtain sideline product discharging 9 in the tower.Depressed heavy oil 5 by the underpressure distillation Tata at the bottom of discharging, introduce vacuum flashing jar 11 through hole enlargement pipeline step by step, under the condition of vacuum flashing jar high vacuum, the depressed heavy oil of high temperature obtains further flash distillation.Dodge top gas and enter knockout drum 12 after the heat exchange cooling, the separating tank top connects pumped vacuum systems, keeps the higher vacuum tightness of vacuum flashing jar 11, and the separating tank bottom is extracted vacuum distillate 10 out as the product discharging.Vacuum flashing jar liquid phase is extracted out at the bottom of by jar, as vacuum residuum 6 dischargings.
Vacuum flashing jar 11, vacuum still 3 and knockout drum 12 have Level Detection to show respectively.
Vacuum still described in the present invention can be the fuel type vacuum still, also can be lubricated oil type vacuum still; Can be wet distiller, wet distiller also can decline; Sideline product discharging number specifically arranges as required.
When the present invention goes into operation at device, can open big vacuum furnace load, heating is fed to 390 ℃～400 ℃, guarantees the underpressure distillation operation.Go into operation stable after, take full advantage of sensible heat and the latent heat that high temperature dodges top gas and give the oil heating of the normal end, can reduce the load of vacuum furnace, implement device is energy-conservation.
By reference to the accompanying drawings 2, temperature is that 380 ℃～400 ℃ depressed heavy oil 5 enters vacuum flashing jar 11 by vacuum flashing jar opening for feed 13, carry out preliminary gas-liquid separation through feed distributor 20, gas phase rises to gather qi together device 19 and dodges gaseous phase outlet 17 discharges in top through foam removal net 16 from flash tank, liquid phase drops to the flash tank liquid phase region, under the drive of rotating shaft 15, helical disk 14 is carried to the liquid level top to the liquid of liquid level below, on the helical disk card or the helical disk superjacent air space form the liquid film district, liquid film is high vacuum in jar, evaporation in a short period of time under the condition of high temperature, make the lighting end in the residual oil fully be evaporated to gas phase, through carrying out mass transfer with the residual oil liquid phase that descends, after the heat transfer, discharge from flash tank gaseous phase outlet 17 with dodging top gas.The material that is not evaporated is deposited at the bottom of the flash tank, sends from vacuum flashing jar liquid phase outlet 18.
The decompression deep drawing method that has the vacuum flashing jar behind the vacuum still of the present invention, improved the crude oil reduced pressure distillation process, the vacuum furnace heating and gasifying, underpressure distillation is carried out in the parallel feeding that contains 45%～55% gas phase after the transfer line hole enlargement decompression in vacuum still, obtain the vacuum distillation tower sideline product.The vacuum flashing jar that depressed heavy oil at the bottom of the tower enters condition of high vacuum degree carries out further flash distillation, make in the depressed heavy oil that the lighter complete flash distillation of cut is come out relatively, guarantee in the vacuum residuum＜500 ℃ cut content is reduced to minimum, thereby improve the extracting rate of underpressure distillation, increase the economic benefit of device.Calculate confirmation through Aspen flowsheeting software simulation, handle the vacuum residuum yield few 1%～2% of the existing operational path of identical raw material processing method of the present invention.
Below by specific embodiment method of the present invention is elaborated.Data are that Aspen flowsheeting software simulation calculates acquisition in embodiment and the comparative example.
Embodiment 1
Method of the present invention is used for certain newly-built crude oil atmospheric vacuum distillation Design of device, and relief portion division technique flow process is with identical shown in the accompanying drawing 1.
The treatment capacity of reliever is 5,500,000 tons/year, and the decompression flow process comprises vacuum furnace, vacuum still, vacuum flashing jar.Vacuum still is regular packed tower, adopts the wet process operation, and tower bottom blowing vapour amount is 1% of tower charging, and the cat head working pressure is 2 kPa, and full tower pressure drop is 685kPa.The vacuum flashing pressure tank is 1.2 kPa.Described vacuum flashing jar is a kind of vacuum flashing jar (as shown in Figure 2) that has spiral isometrical rotating disk thin-film evaporator.The long L of jar is 3 times of tank diameter D1, and gather qi together device inner diameter D 2 is 50% of tank diameter D1.Rotating disk disk track d is 30% of tank diameter D1, and 40% of rotating disk is immersed in jar liquid level of interior bottom liquid phase region, and rotating shaft is 50% of tank diameter apart from the go to the bottom distance h of tangent line of jar.
Oil 1 of the normal end is fed into vacuum distillation apparatus with 655 tons/hour, enters into vacuum still 3 by pressure-reducing line for oil-transferring transition section 4 after vacuum furnace 2 is heated to 420 ℃.The vacuum flashing jar directly is connected with discharging at the bottom of the decompression Tata, and flash tank pressure is 1.2 kPa.Dodge top gas behind the adiabatic flash and account for 1.41% of discharging at the bottom of the underpressure distillation Tata, oil is as the vacuum residuum discharging at the bottom of the vacuum flashing jar.Extract product 9 out from the vacuum distillation tower side line.Vacuum residuum is the 36.13%(quality to the yield of combined feed total feed), the cut point of decompressed wax oil reaches 593 ℃.
Comparative example 1
Relate to embodiment 1 newly-built 1,000 ten thousand tons of/year crude oil atmospheric vacuum distillation Design of device equally.The treatment capacity of reliever is 5,000,000 tons/year.Adopt the disclosed atmospheric vacuum distillation method that has vacuum flasher among the CN101376068A.Under same feedstock, processing condition, vacuum residuum is 37.64% to the yield of combined feed total feed, and the decompressed wax oil cut point is 565 ℃, and the 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 crude oil atmospheric and vacuum distillation unit, the normal pressure part is identical with conventional atmospheric and vacuum distillation unit, the decompression part adopts the crude oil working method process flow diagram shown in the accompanying drawing 1, mainly comprises vacuum furnace, vacuum distillation tower distillation, vacuum flashing jar.Vacuum still is regular packed tower, adopts the wet process operation, and tower bottom blowing vapour amount is 1% of tower charging, and the cat head working pressure is 2 kPa, and full tower pressure drop is 685Pa.The vacuum flashing pressure tank is 1.2 kPa.The further depressurized flash tank is a kind of vacuum flashing jar (as shown in Figure 2) that has spiral isometrical rotating disk thin-film evaporator.The long L of jar is 3 times of tank diameter D1, and the inner diameter D 2 of gather qi together device is 50% of tank diameter D1.Rotating disk disk track d is 30% of tank diameter D1, and 40% of rotating disk is immersed in jar liquid level of interior bottom liquid phase region, and rotating shaft is 50% of tank diameter apart from the go to the bottom distance h of tangent line of jar.
Oil 1 of the normal end is fed into vacuum distillation apparatus with 655 tons/hour, enters into vacuum still 3 by pressure-reducing line for oil-transferring transition section 4 after vacuum furnace 2 is heated to 420 ℃.The vacuum flashing jar directly is connected with discharging at the bottom of the decompression Tata, and flash tank pressure is 1.2 kPa.Dodge top gas behind the adiabatic flash and account for 1.38% of discharging at the bottom of the underpressure distillation Tata, oil is as the vacuum residuum discharging at the bottom of the vacuum flashing jar.Extract product 9 out from the vacuum distillation tower side line.Vacuum residuum is the 36.13%(quality to the yield of combined feed total feed), the cut point of decompressed wax oil reaches 593 ℃.
This device capacity expansion revamping relief portion is divided and is kept original vacuum furnace and vacuum distillation tower, and vacuum distillation tower internals and filler are transformed.Newly-increased main equipment is vacuum flashing jar, oil charging of the normal end/sudden strain of a muscle top gas interchanger.Transform back vacuum residuum yield and reduce by 1%～1.5%.
Comparative example 2
The capacity expansion revamping that relates to certain crude oil atmospheric vacuum distillation device among the embodiment 2 equally.The disclosed atmospheric vacuum distillation method that has vacuum flasher carries out capacity expansion revamping among the employing CN101376068A.
Under same feedstock, processing condition, vacuum residuum is 37.64% to the yield of combined feed total feed, and the decompressed wax oil cut point is 565 ℃, and the deep drawing degree is not as good as the present invention.
Calculate by 1,000 ten thousand tons of/year atmospheric and vacuum distillation unit, the charging of decompression part is about 655 tons/hour, embodiment 2 reduces residual oil yield 1.5%, comes for 300 yuan/ton in residual oil and mixed gatch price difference, and year is amounted to Renminbi: 655 * 1.5% * 300 * 8400=2475.9 ten thousand yuan.Add the part that device cuts down the consumption of energy, the device economic benefit highly significant of obtaining.
Claims (16)
1. further depressurized flash tank, comprise tank body and jar inner member, tank body is horizontal type structure, comprise the gas phase zone on top and the liquid phase region of bottom in jar, it is characterized in that jar inner member is included in the feed distributor that upper gaseous phase section arranges, the rotating disk thin-film evaporator that arranges at liquid phase region liquid level place, bottom, the rotating disk thin-film evaporator comprises rotating disk and rotating shaft, and rotating shaft is horizontally set on the tank body axial direction due in the tank body, and rotating disk is fixed in the rotating shaft.
2. according to the described vacuum flashing jar of claim 1, it is characterized in that, the gather qi together device is set in the tank top, the gather qi together device is communicated with upper gaseous phase section, in establish the foam removal net, connect the gas phase discharge port.
3. according to the described vacuum flashing jar of claim 1, it is characterized in that 20%～70% of described rotating disk is immersed in jar below the liquid level of interior bottom liquid phase region.
4. according to the described vacuum flashing jar of claim 1, it is characterized in that described rotating disk is that spiral rotating disk or multi-disc are perpendicular to the circular plate type rotating disk of rotating shaft.
5. according to claim 1 or 4 described vacuum flashing jars, it is characterized in that, some fins are set on the card of described rotating disk, to increase the surface-area that forms film.
6. according to the described vacuum flashing jar of claim 1, it is characterized in that, described rotating disk is arranged along tank body vertical section radial symmetry, the rotating disk equal diameters or in the jar center successively decrease successively to both sides along the jar axial direction due, the rotating disk diameter of jar central position maximum is 20%～40% of tank diameter.
7. according to the described vacuum flashing jar of claim 2, it is characterized in that opening for feed, flash distillation gas phase discharge port and flash distillation liquid phase relief outlet are set on the described tank body, and opening for feed is arranged on the tank body upper gaseous phase section, enter along the tank body axial direction due, connect feed distributor; Flash distillation gas phase discharge port is arranged on the gather qi together device at tank body top, and flash distillation liquid phase relief outlet is arranged on the bottom of tank body, and the flash tank liquid phase region has liquid level control.
8. according to the described vacuum flashing jar of claim 1, it is characterized in that described feed distributor is tubulose cellular type sparger or pipe distributor.
9. decompression deep drawing method, comprise following content: crude oil oil at the bottom of the atmospheric tower after the normal pressure distillation is heated by vacuum furnace, enters vacuum still through pressure-reducing line for oil-transferring and carries out underpressure distillation; Extract the decompression benzoline out from the vacuum still side line, extract depressed heavy oil out at the bottom of the underpressure distillation Tata to enter a vacuum flashing jar; Vacuum flashing tank top gas phase connects pumped vacuum systems by knockout drum, keeps the higher vacuum tightness of vacuum flashing jar; The gas-liquid separation pot bottom is discharged vacuum distillate, the vacuum residuum at the bottom of the vacuum flashing jar after the discharge flash distillation; Vacuum flashing jar wherein is the described vacuum flashing jar of the arbitrary claim of claim 1 to 8.
10. in accordance with the method for claim 9, it is characterized in that described depressed heavy oil enters the vacuum flashing jar, carry out gas-liquid separation by feed distributor and distribute, gas phase rises in the tank deck gather qi together device and is discharged by the gas phase discharge port through the foam removal net, and liquid phase freely falls to a jar liquid phase region.
11. in accordance with the method for claim 9, it is characterized in that, the depressed heavy oil of discharging at the bottom of the described underpressure distillation Tata is introduced the vacuum flashing jar by hole enlargement pipeline step by step, lighting end in the vacuum residuum is depressed at the oil gas branch that reduces step by step be evaporated, finally in the complete flash distillation of vacuum flashing jar.
12. in accordance with the method for claim 9, it is characterized in that the pressure of described vacuum flashing jar is than low 2 kPa of vacuum still tower bottom pressure～5 kPa.
13. in accordance with the method for claim 9, it is characterized in that the position height of described vacuum flashing jar is in vacuum still, vacuum flashing jar opening for feed is positioned at 30%～70% place of liquid level at the bottom of the underpressure distillation Tata.
14. in accordance with the method for claim 9, it is characterized in that heat exchange is carried out in the logistics that needs to heat in oil or the device at the bottom of vacuum flashing tank deck gas phase and the atmospheric tower.
15. in accordance with the method for claim 9, it is characterized in that, a cover pumped vacuum systems is set, vacuum still and vacuum flashing jar share a cover pumped vacuum systems vacuum pumping, control device is set, controls the vacuum tightness of vacuum still and vacuum flashing jar respectively.
16. in accordance with the method for claim 9, it is characterized in that, two cover pumped vacuum systems are set, the vacuum pumping respectively of vacuum still and vacuum flashing jar, the vacuum degree control of vacuum flashing jar is arranged on the vacuum flashing head space gas condenser knockout drum afterwards.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103865565A (en) * | 2014-03-03 | 2014-06-18 | 中山大学 | Crude oil reduced pressure distillation method for eliminating choke point in pressure reduction process |
| CN111876188A (en) * | 2020-08-03 | 2020-11-03 | 张家港保税区慧鑫化工科技有限公司 | Distillate oil recovery device and recovery method |
Citations (2)
| 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 |
-
2012
- 2012-02-06 CN CN201210024897.2A patent/CN103242886B/en active Active
Patent Citations (2)
| 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 |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103865565A (en) * | 2014-03-03 | 2014-06-18 | 中山大学 | Crude oil reduced pressure distillation method for eliminating choke point in pressure reduction process |
| CN103865565B (en) * | 2014-03-03 | 2015-08-05 | 中山大学 | A kind of crude oil vacuum distillation method eliminating decompression process bottleneck |
| CN111876188A (en) * | 2020-08-03 | 2020-11-03 | 张家港保税区慧鑫化工科技有限公司 | Distillate oil recovery device and recovery method |
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