CN103059919B - A kind of vacuum distillation method and device improving extracting rate - Google Patents
A kind of vacuum distillation method and device improving extracting rate Download PDFInfo
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Abstract
The invention discloses a kind of crude oil vacuum distillation method and device.Depressed heavy oil outlet increase reduced-pressure flash tank at the bottom of vacuum still tower, the depressed heavy oil that vacuum distillation tower tower bottom flow is gone out carries out flash distillation higher than under the condition of vacuum tightness at the bottom of vacuum distillation tower tower in reduced-pressure flash tank, vacuum flashing head space gas enters knockout drum after heat exchange and cooling, gas-liquid separation tank top connects pumped vacuum systems to maintain the vacuum tightness of flash tank, bottom extracts vacuum distillate out as product, at the bottom of reduced-pressure flash tank tank, extract vacuum residuum out.Vacuum distillation method of the present invention, improve crude oil reduced pressure distillation process, the reduced-pressure flash tank making depressed heavy oil enter 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.
Description
Technical field
The invention belongs to refining of petroleum field, relate in particular to the vacuum distillation method and the device that improve extracting rate in a kind of crude oil underpressure distillation.
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 ends content in the energy consumption of total extracting rate of device benzoline, device and vacuum residuum as the index weighing 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, one of the technical problem to be solved in the present invention is to provide a kind of vacuum distillation method improving extracting rate, can significantly improve the extracting rate in crude oil vacuum distillation process, increases device economic benefit.
A kind of vacuum distillation method improving extracting rate 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 flash tank.
The present invention improves in the vacuum distillation method of extracting rate, the depressed heavy oil of discharging at the bottom of vacuum still tower introduces reduced-pressure flash tank by expanding pipeline step by step, the lighting end in vacuum residuum is made to divide pressure to be evaporated at the oil gas reduced step by step, finally in the complete flash distillation of reduced-pressure flash tank.
The present invention improves in the vacuum distillation method of extracting rate, the pressure comparatively low 2kPa ~ 5kPa of vacuum still tower bottom pressure of reduced-pressure flash tank, and the depressed heavy oil that vacuum distillation tower is discharged flows into reduced-pressure flash tank by self-pressure.
The present invention improves in the vacuum distillation method of extracting rate, and 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.
The present invention improves in the vacuum distillation method of extracting rate, and described reduced-pressure flash tank is horizontal tank, to realize the larger flash distillation face of reduced-pressure flash tank.
The present invention improves in the vacuum distillation method of extracting rate, vacuum flashing head space gas phase and the normal end oil or device in need heat logistics heat exchange, reduce plant energy consumption.
The present invention improves in the vacuum distillation method of extracting rate, is extracted out the vacuum residuum of degree of depth flash distillation, liquid automatic control pump discharge flow at the bottom of tank at the bottom of reduced-pressure flash tank tank by pump.
The present invention improves in the vacuum distillation method of extracting rate, a set of pumped vacuum systems can be set, 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.
The present invention improves in the vacuum distillation method of extracting rate, 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 will solve is to provide a kind of crude oil vacuum distillation apparatus improving extracting rate.Technical scheme is: a kind of vacuum distillation apparatus improving extracting rate, 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.
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) 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.
4) 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.
5) 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 improves the vacuum distillation method process flow diagram of extracting rate.
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.
Embodiment
The inventive method is depressed heavy oil outlet connection reduced-pressure flash tank at the bottom of vacuum still tower, 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 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.
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.
With the 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 2kPa, and full tower pressure drop is 685kPa.Vacuum flashing pressure tank is 1.2kPa.
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 1.2kPa.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 36.22%(quality to the yield of combined feed total feed), the cut point of decompressed wax oil reaches 588 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 vacuum distillation method process flow diagram of the raising extracting rate 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 2kPa, and full tower pressure drop is 685Pa.Vacuum flashing pressure tank is 1.2kPa.
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 1.2kPa.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 36.22%(quality to the yield of combined feed total feed), the cut point of decompressed wax oil reaches 588 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 (8)
1. improve a vacuum distillation method for extracting rate, comprise 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, depressed heavy oil is extracted out at the bottom of vacuum still tower, a reduced-pressure flash tank is entered by expanding pipeline step by step, reduced-pressure flash tank top gas phase connects pumped vacuum systems by knockout drum, maintain 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; The pressure comparatively low 2kPa ~ 5kPa of vacuum still tower bottom pressure of wherein said reduced-pressure flash tank, the depressed heavy oil that vacuum still is discharged flows into reduced-pressure flash tank by self-pressure; 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 reduced-pressure flash tank is horizontal tank.
3. in accordance with the method for claim 1, it is characterized in that, cool again after oil first carries out heat exchange at the bottom of described reduced-pressure flash tank top gas phase and atmospheric tower.
4. in accordance with the method for claim 1, it is characterized in that, extracted out the vacuum residuum of degree of depth flash distillation at the bottom of described reduced-pressure flash tank tank by pump, liquid automatic control pump discharge flow at the bottom of tank.
5. in accordance with the method for claim 1, it is characterized in that, described vacuum still and reduced-pressure flash tank share a set of pumped vacuum systems, arrange control device and control respective vacuum tightness respectively.
6. in accordance with the method for claim 5, it is characterized in that, the vacuum degree control of described reduced-pressure flash tank is arranged on the knockout drum of reduced-pressure flash tank top gas phase.
7. 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 control vacuum tightness respectively.
8. one kind is improved the vacuum distillation apparatus of extracting rate, comprise vacuum furnace, vacuum still and reduced-pressure flash tank, it is characterized in that: 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, described reduced-pressure flash tank operates under the pressure of 2kPa ~ 5kPa lower than vacuum still tower bottom pressure; 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.
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| CN1089298A (en) * | 1992-11-30 | 1994-07-13 | 布斯公司 | The deep processing technology of vacuum residuum in the crude oil refinery |
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| CN101624535A (en) * | 2009-08-03 | 2010-01-13 | 中海石油炼化有限责任公司 | Atmospheric and vacuum distillation device and atmospheric and vacuum distillation method of high acid-content crude oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1072200A (en) * | 1991-11-03 | 1993-05-19 | 史万年 | A kind of process flow for petroleum distillation |
| CN1089298A (en) * | 1992-11-30 | 1994-07-13 | 布斯公司 | The deep processing technology of vacuum residuum in the crude oil refinery |
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| CN101624535A (en) * | 2009-08-03 | 2010-01-13 | 中海石油炼化有限责任公司 | Atmospheric and vacuum distillation device and atmospheric and vacuum distillation method of high acid-content crude oil |
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