CN102311768B - Reduced-pressure flash tank and crude oil reduced-pressure deep drawing method - Google Patents
Reduced-pressure flash tank and crude oil reduced-pressure deep drawing method Download PDFInfo
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Abstract
The invention discloses a reduced-pressure flash tank and a crude oil reduced-pressure deep drawing method. The reduced-pressure flash tank comprises a tank body, at least one rotary evaporation disc is arranged in a gas phase area in the upper part of the reduced-pressure flash tank, and the rotary evaporation disc is fixed on a rotating shaft fixed at a longitudinal axial center position of the tank body. In the crude oil reduced-pressure deep drawing method disclosed by the method, a reduced-pressure flash tank is arranged between a reduced-pressure furnace and a reduced-pressure distillation tower, the reduced-pressure distillation raw material is heated in the reduced-pressure durance and then enters the reduced-pressure flash tank for evaporation and gas-liquid separation, a liquid phase, namely bottom oil, discharged from the bottom of the reduced-pressure flash tank is introduced into the reduced-pressure distillation tower, and a gas phase, namely a top gas, discharged out from the top of the reduced-pressure flash tank is discharged out of the flash tank and condensed into a liquid phase to be led out of the device. When the reduced-pressure flash tank and the crude oil reduced-pressure deep drawing method are used, the drawing rate of a crude oil reduced-pressure distillation process is increased.
Description
Technical field
The invention belongs to refining of petroleum field, relate to a kind of reduced-pressure flash tank and crude oil decompression deep drawing method, relate to specifically a kind of method and apparatus that improves crude oil vacuum distillation process extracting rate.
Background technology
Crude oil atmospheric vacuum distillation technique is the first operation of refining of petroleum, is the component that by the method for distillation, crude oil is divided into different boiling range scopes, to adapt to product and the downstream unit processing requirement to raw material.The height of its light oil yield and the size of energy consumption directly affect the economic benefit of refining of petroleum.Conventional crude oil atmospheric vacuum distillation technique adopts the flow process of " two stove three towers " more: after crude oil upgrading, enter primary tower (or flashing tower), then through atmospheric pressure kiln heating, enter atmospheric tower, at the bottom of atmospheric tower, oil is delivered to vacuum distillation tower through vacuum furnace heating by pressure-reducing line for oil-transferring, complete air distillation and underpressure distillation to crude oil, obtain and meet the product of specification of quality and the raw material of downstream unit.
Along with expanding economy, the increase year by year of world petroleum demand amount, meanwhile, in world's crude resources supply, the ratio of heavy oil and extra heavy oil progressively increases, lightweight oil, middle matter oil supplying ratio continuous decrease.Therefore, improve the light oil extracting rate in crude oil atmospheric vacuum distillation, reduce atmospheric and vacuum distillation unit energy consumption, improve device economic benefit and become the common problem of paying close attention to of global Refining Chemical Industry.Along with the development of Chinese national economy, 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 in China will reach 50%～60%.Therefore, rationally utilize crude resources, optimization processing technology has been the imperative act of China's oil chemical industry.In device maximization and Integrated Refinery And Petrochemical novel refinery design, as the crude oil atmospheric vacuum distillation device of " tap " at utilization of resources maximization, energy utilization economized, running cost, rationalize, size investment optimizing, realize in the Sustainable development of China's oil chemical industry and there is very important status.
For this reason, the decompression deep drawing of Chinese scholars to Atmospheric Vacuum Unit, energy-saving and cost-reducing, reduce investment and compare deep research, made significant headway.Developing direction mainly concentrates on the following aspects: (1) optimizes vacuum system, improves the vacuum tightness of vacuum fractionation tower top; (2) adopt novel, high efficiency packing and direct contact type heat transfer type, reduce tower total pressure drop, keep higher flash zone vacuum tightness; (3) improve transfer line design, reduce transfer line pressure drop and temperature drop; (4) optimize washing section design and operation, the fractionation concept of strengthening washing section; (5) the efficient gas of development of new and liquid distributor; (6) adopt strengthening crude distillation method etc.
CN03108050.2 discloses a kind of atmospheric and vacuum distillation of petroleum technique, decompression part adopts second depressurized distillation, by newly increasing one-level vacuum still, transfer part normal pressure load and decompression stress are to one-level vacuum fractionation tower respectively, the requirement that improves amount of finish to meet device, has obtained good effect.But owing to having newly increased one-level vacuum fractionation tower and vacuum furnace, plant investment is larger.
US7172686 has delivered a kind of method that improves crude distillation distillate yield, and method one is to extract gaseous stream out from tower inside cord, separates and obtains product, and a part of gas phase is returned in tower; Method two is incoming mixture is lighting end, middle runnings, last running by boiling point height heating and separating, then at different feed entrance points, enter and in tower, carry out fractionation respectively, from side line extract out successively gently, last running.Method one is equivalent to side line and has added a stripping tower, has improved distillate quality.But plant investment and energy consumption have to a certain degree been increased; Method two has been realized gently, last running sectional feeding, improved the operation of crude distillation separation column, be conducive to improve distillate yield, but the lighting end of having separated from parallel feeding is again sent in tower and carried out fractionation, repetitive operation increases plant energy consumption and does not reduce the load of tower.
CN2242892Y discloses a kind of composite crude oil distillation vacuum distillation tower, is provided with a liquid seal device and top and separates, and have a vacuum system interface to be connected with top vacuum system at the bottom of tower.This utility model separates the deep drawing section of the rectifying section of vacuum distillation tower and bottom by liquid seal device, 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 complexity of this utility model simultaneously, top vacuum system loading is high, and plant energy consumption relatively can be high.
CN1884441A discloses the method that improves light oil yield of atmospheric and vacuum distillation of petroleum oil, and the additive containing rosin is added in the crude oil of atmospheric and vacuum distillation of petroleum tower, improves the light oil yield of atmospheric and vacuum distillation by changing the intermolecular reactive force of crude oil.But the 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.
US7172686 has delivered a kind of method that improves crude distillation distillate yield, and method one is to extract gaseous stream out from tower inside cord, separates and obtains product, and a part of gas phase is returned in tower; Method two is incoming mixture is lighting end, middle runnings, last running by boiling point height heating and separating, then at different feed entrance points, enter and in tower, carry out fractionation respectively, from side line extract out successively gently, last running.Method one is equivalent to side line and has added a stripping tower, has improved distillate quality, but has increased to a certain extent plant investment and energy consumption; Method two has been realized gently, last running sectional feeding, improved the operation of crude distillation separation column, be conducive to improve distillate yield, but the lighting end of having separated from parallel feeding is again sent in tower and carried out fractionation, repetitive operation increases plant energy consumption and does not reduce the load of tower.
CN1287872A has delivered a kind of crude oil atmospheric vacuum distillation method with degree of depth stripping process, at a vacuum distillation tower side washing tank in parallel, the feed zone of vacuum distillation tower and stripping stage are separated by fluid-tight isolation sparger, the oil gas of stripping stage is by entering the bottom of washing tank communicating pipe, take from absorption oil that vacuum distillation tower subtracts three line dischargings and by washing tank top, enter downward spray and the reverse mass-and heat-transfer of oil gas upwards after cooling, the top of vacuum distillation tower is returned in the tank deck oil gas discharging of washing tank, and at the bottom of tank, discharging is returned to vacuum distillation tower as washing oil.This technique makes vacuum distillation tower stripping stage experience a steam stripped process of the degree of depth by setting up washing tank, is conducive to improve decompression extracting rate.But the method is just optimized improvement to vacuum distillation tower stripping stage, subtract preferably third fractional oil as washing oil by quality, in economic benefit, wait research.
CN101376068A discloses a kind of atmospheric vacuum distillation method with vacuum flasher and equipment, is a vacuum flasher is set before long residuum enters vacuum furnace.The oil process furnace that enters to reduce pressure at the bottom of flashing tower, flashing tower top gas enter that certain sideline product close with flashing tower top gas cut extract out mouthful above or below.The method is improved 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 at the bottom of atmospheric tower, oil enters flashing tower, because the temperature of oil at the bottom of atmospheric tower is relatively low, the vacuum tightness of adding stokehold flashing tower is relatively not high, the effect of flashing tower flash distillation gasification is limited, 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 that fundamentally changes vacuum distillation tower.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of reduced-pressure flash tank and crude oil decompression deep drawing method, use flash tank of the present invention and decompression deep drawing method further to improve extracting rate, increase economic efficiency.
Reduced-pressure flash tank of the present invention comprises tank body, comprises gas phase zone and the liquid phase region, bottom on top in tank body, and at least one rotary evaporation dish is set in upper gaseous phase section, and rotary evaporation dish is fixed in the rotating shaft that is arranged on tank body longitudinal axis center position.
2～4 rotary evaporation dishes are preferably set in reduced-pressure flash tank of the present invention in same rotating shaft, and rotary evaporation dish is disc structure or for circle ring disk structure, the diameter of rotary evaporation dish is 20%～80% of reduced-pressure flash tank internal diameter.When two or more rotary evaporation dishes are set, the flow-stopping plate that prevents wall stream is set on the tank skin between every two rotary evaporation dishes.Flow-stopping plate is to be fixed on to become with tank skin on tank skin the closed circular sector structure of 15 °～45 °, fan-shaped top is fixed on tank skin, radius of a circle is 1/3～1/2 of lower floor's rotary evaporation dish radius below, flow-stopping plate sector structure has 3～6 gussets towards the face of tank skin, along tank radial equipartition, fixes flow-stopping plate on tank skin.Flow-stopping plate gets rid of upper strata rotary evaporation dish to the liquid phase on tank skin and collects and be drained on lower one deck rotary evaporation dish.Evaporating pan is fixed in a rotating shaft extending in flash tank, and rotating shaft adopts motor to drive or magnetic force driving.
Opening for feed, flashed vapour discharge port and flash distillation liquid phase relief outlet are set on the tank body of reduced-pressure flash tank, opening for feed is arranged on the top of uppermost position in fig-ure rotary evaporation dish, charging is caused to rotary evaporation dish, and flashed vapour discharge port is arranged on the top of tank body, and flash distillation liquid phase relief outlet is arranged on the bottom of tank body.At flashed vapour discharge port also portion, foam removal net can be set.The rotating speed of rotary evaporation dish can be determined according to the scale of the character of charging, device and operational requirement, generally can be 30～600 revs/min.
Crude oil decompression deep drawing method of the present invention comprises following content: between vacuum furnace and vacuum still, reduced-pressure flash tank is set, underpressure distillation raw material enters reduced-pressure flash tank after vacuum furnace heating, in reduced-pressure flash tank, evaporate and gas-liquid separation, the liquid phase (hereinafter referred to as dodging end oil) of discharging at the bottom of reduced-pressure flash tank is dodged end oil and is introduced vacuum still, the gas phase (hereinafter referred to as dodging top gas) that vacuum flashing tank deck is discharged dodge top gas discharge flash tank and be condensed into liquid phase after caterpillar.The reduced-pressure flash tank using in crude oil decompression deep drawing method of the present invention is the above-mentioned reduced-pressure flash tank with rotary evaporation dish of the present invention.
In crude oil decompression deep drawing method of the present invention, underpressure distillation raw material (being generally long residuum) enters reduced-pressure flash tank, by an initial distribution device, carry out gas-liquid separation distribution, gas phase rises and is discharged by tank deck gas phase discharge port, liquid phase is assigned on rotary evaporation dish, by acting on of centrifugal force, on rotary evaporation dish, diffuse into thinner, the liquid film being evenly distributed, liquid film is in high vacuum, evaporation in a short period of time under the condition of high temperature, on the one hand the gas phase in charging residual oil is separated completely, make on the other hand more light constituent in residual oil be evaporated, improve the extracting rate of underpressure distillation.
In the method for crude oil decompression deep drawing of the present invention, cancelled the setting of pressure-reducing line for oil-transferring in conventional atmospheric and vacuum distillation, vertical reduced-pressure flash tank is set between vacuum furnace and vacuum distillation tower, between flash tank and vacuum furnace, vacuum still, can compactly arrange, without considering to arrange the transfer line setting that is not less than 15 meters.Vertical flash tank is mainly used in the gas-liquid separation of the rear residual oil gas-liquid two-phase mixed flow of vacuum furnace heating, and more lighting end is evaporated from residual oil, to improve the extracting rate of vacuum distillation process.
In the method for crude oil decompression deep drawing of the present invention, other technology contents, if atmospheric distillation tower, vacuum furnace, vacuum still etc. are technology contents well known to those skilled in the art.
In the method for crude oil decompression deep drawing of the present invention, a set of pumped vacuum systems can be set, a set of pumped vacuum systems vacuum pumping for vacuum still and reduced-pressure flash tank, can arrange control device, controls respectively the vacuum tightness of vacuum still and flash tank; Two cover pumped vacuum systems also can be set, the vacuum pumping respectively of vacuum still and reduced-pressure flash tank.The vacuum degree control of reduced-pressure flash tank is arranged on dodges on top gas condenser knockout drum afterwards.The vacuum pumping of reduced-pressure flash tank and vacuum still can adopt the method and apparatus of this area routine.
In the method for crude oil decompression deep drawing of the present invention, other technology contents, if atmospheric distillation tower, vacuum furnace, vacuum still etc. are technology contents well known to those skilled in the art.
Compared with prior art, the present invention has the following advantages:
1, adopt the suitable reduced-pressure flash tank of structure, can improve gas-liquid separation effect on the one hand, can obviously improve on the other hand the rate of evaporation of light constituent in charging, be conducive to improve the extracting rate of raw material vacuum distillation process, reduce the operational load of vacuum still.
2, vacuum furnace outlet of still is directly communicated with and subtracts flash tank, and vacuum still is introduced in the discharging of reduced-pressure flash tank bottom liquid phases.Shortened long residuum heating one technical process that enters vacuum distillation tower, greatly reduced process pressure drop and the calorific loss of pressure-reducing line for oil-transferring in prior art, made vacuum furnace internal pressure lower, oil of normal end gasification point in vacuum furnace shifts to an earlier date, and outlet of still vaporization rate is higher.
3, by reduced-pressure flash tank being set between vacuum furnace and vacuum distillation tower, gas-liquid distribution apparatus is set in flash tank, has improved charging gas-liquid separation.
4, vacuum furnace outlet of still is directly communicated with reduced-pressure flash tank, and vacuum distillation tower is introduced in the discharging of flash tank bottom liquid phases.Cancel pressure-reducing line for oil-transferring, the transfer line thermal walking of having avoided extra heavy pipe footpath, large pipe range transfer line low speed segment to cause, has optimized reduced pressure distillation process design.Through adjusting, the cost of flash tank is starkly lower than the cost of extra heavy pipe footpath, large pipe range transfer line.
5, dodge end oil and enter separately vacuum still, dodge top gas and do not enter vacuum still, significantly reduce the processing load of vacuum still, eliminated " bottleneck " of vacuum distillation tower treatment capacity, be conducive to the capacity expansion revamping of old device.Dodge end oil and enter separately vacuum still, reduced to a certain extent the required theoretical stage of vacuum distillation tower, can suitably reduce tower height and tower diameter, economy system investment.Dodge end oil and enter separately vacuum still, dodge top gas and do not enter vacuum still, reduced the gas phase load of vacuum still, full tower pressure drop is reduced, be conducive to improve decompression extracting rate, and significantly reduced Top of Vacuum Tower condensation and vacuumized load.Underpressure distillation less energy-consumption, high vacuum, the operation of high extracting rate have been realized.Effectively reduce the yield that is worth low vacuum residuum.
6, dodge end oil and enter separately vacuum still, the Vapor Entrainment of having avoided gas-liquid mixed charging to cause, has guaranteed depressurised side line products quality.
7, sudden strain of a muscle top gas and oil of the normal end carry out heat exchange, have reduced vacuum furnace load, reduce plant energy consumption.
8, Technology of the present invention is rationally advanced, and vacuum residuum yield is low, for the transformation of old device, have scrap build amount few, invest lowly, the transformation duration is short, device income is the advantage such as quick obviously; For the design and construction of new device, there is technique rationally advanced, energy consumption level is low, and size investment is little, and equipment takes up an area the features such as few.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for a kind of crude oil decompression of the present invention deep drawing;
Fig. 2 is reduced-pressure flash tank structural representation of the present invention;
Fig. 3 is flow-stopping plate structural representation in reduced-pressure flash tank of the present invention.
Wherein 1 is crude oil after pre-treatment, 2 is vacuum furnace, 3 is vacuum still, 4 is reduced-pressure flash tank, 5 is atmospheric distillation tower, 6 is normal end oil/sudden strain of a muscle top gas interchanger, 7 is stripped vapor, 8 for dodging top product, 9 is vacuum distillation tower pumped vacuum systems, 10 is vacuum distillate, 11 is normal top product, 12 is vacuum residuum, 13 for dodging end oil, 14 for dodging top gas condenser, 15 is oil of the normal end, 16 is atmospheric distillate, 17 atmospheric pressure kilns, 18 flash tank gas-liquid separators, 19 is rotary evaporation dish, 20 is flow-stopping plate, 21 for dodging end oil export, 22 for dodging top gas outlet, 23 is rotating shaft, 24 is that flow-stopping plate is following, 25 is tank skin, 26 is gusset, 27 is flow-stopping plate top.
Embodiment
By reference to the accompanying drawings 1, a kind of technological process of the inventive method is: after pre-treatment, crude oil 1 is warmed up to 360 ℃～370 ℃ through atmospheric pressure kiln 17 and enters atmospheric distillation tower 5, distills out normal top product 11 and each side line atmospheric distillate 16.After long residuum 15 and the heat exchange of sudden strain of a muscle top gas heat up, enter vacuum furnace 2 and be heated to 380 ℃～400 ℃, by reduced-pressure flash tank gas-liquid separator 18, enter reduced-pressure flash tank, carry out preliminary gas-liquid separation.Gas phase rises and is discharged by tank deck gas phase discharge port, after normal end oil/sudden strain of a muscle top gas 6 heat exchange-sudden strain of a muscle top gas condenser 14 condensations, carry out gas-liquid separation, isolated liquid phase is as dodging top product 8, and it is 1.5kPa～4.0kPa that gas phase connects pumped vacuum systems control flash tank residual voltage; Liquid phase is evenly distributed on rotary evaporation dish 19, by the liquid film that on rotary evaporation dish, Rotational diffusion becomes as thin as a wafer, is evenly distributed that acts on of centrifugal force, liquid film is subject to thermal evaporation under the condition of high vacuum, high temperature within the extremely short time, the gas molecule in space being evaporated and the gas-liquid distributor liquid phase of getting off that distributes completes gas-liquid mass transfer, heat transfer, is mixed into flash tank and dodges in top gas and become and dodge top product.The material not evaporated throws away evaporating pan, is deposited at the bottom of flash tank and discharges as dodging end oil 13.Dodge end oil and enter vacuum still 3, VACUUM TOWER BOTTOM is blown into stripped vapor 7, and tower top connects pumped vacuum systems, keeps tower top pressure at 1.0kPa～3.0kPa.Distill out vacuum distillate 10, vacuum residuum 12 is discharged at the bottom of tower.
Vacuum still in the present invention can be fuel type vacuum still, can be also Lube Type vacuum still; Can be wet distiller, wet distiller also can decline; Lateral line discharging number specifically arranges as required.Atmospheric distillation tower in the present invention, reduced-pressure flash tank, vacuum still have respectively base level control system.
By reference to the accompanying drawings 2, intensification is that the oil of the normal end of 380 ℃～400 ℃ enters reduced-pressure flash tank 4, by flash tank gas-liquid separator 18, carry out preliminary gas-liquid separation, gas phase is dodged top gas outlet 22 from flash tank and is discharged, liquid phase drops on rotary evaporation dish 19, under the effect of rotation generation centrifugal force, rotate and diffuse into as thin as a wafer, the liquid film being evenly distributed, liquid film is in high vacuum, under the condition of high temperature, within the extremely short time, be subject to thermal evaporation, make the lighting end in residual oil fully be evaporated to gas phase, through carrying out mass transfer with the residual oil liquid phase declining, after heat transfer, with dodging top gas, from flash tank gaseous phase outlet 22, discharge.The material not evaporated throws away evaporating pan, by the secondary that is again distributed to of anti-wall flow baffle plate 20, rotates evaporating pan, again evaporates.At the bottom of final liquid phase material is deposited to flash tank, from dodging end oil export 21, send.
The rotary evaporation dish of the reduced-pressure flash tank in the present invention can be 1, also can be 2～4.
The feed distributor of the reduced-pressure flash tank in the present invention is endless tube shape cellular type sparger, also can adopt other well behaved feed distributors.
By reference to the accompanying drawings 3, the top 27 of flow-stopping plate 20 is connected with tank skin 25 use sealing welds, entirety becomes 15 °～45 ° angles with tank skin, following 24 formation radius of a circles are 1/3～1/2 of lower floor's evaporating pan radius, and there is the fixing flow-stopping plate of gusset 26 at the back side of flow-stopping plate on tank skin 25.The liquid phase throwing away on the evaporating pan of upper strata flows down along tank skin, through flow-stopping plate collection, uniform to lower floor's rotary evaporation dish.
After vacuum furnace of the present invention with vacuum distillation method and the equipment of centrifugal molecule flash distillation, improved crude oil atmospheric vacuum distillation technique, gas-liquid separation is carried out in the parallel feeding that vacuum furnace heating and gasifying is contained to 45%～55% gas phase in reduced-pressure flash tank, and utilize the centrifugal force of the evaporating pan generation of rotation that the lighting end in residual oil is evaporated as far as possible, greatly improved distillate extracting rate.Through analog calculation, confirm, process the residual oil yield few 2%～6% of the identical more existing operational path of raw material processing method of the present invention, and flash distillation tank deck accounts for sensible heat that the oil gas of charging 45%～55% contains and latent heat and is enough to, oil heat exchange to 390 of the normal end ℃～400 ℃, greatly save the load of vacuum furnace.
The present invention, when start up, can open large vacuum furnace load, and heating is fed to 390 ℃～400 ℃, guarantees underpressure distillation operation.Go into operation stable after, make full use of high temperature and dodge the sensible heat of top gas and latent heat to the oil heating of the normal end, can reduce the load of vacuum furnace, implement device is energy-conservation.
Claims (9)
1. a crude oil decompression deep drawing method, it is characterized in that: between vacuum furnace and vacuum still, reduced-pressure flash tank is set, underpressure distillation raw material enters reduced-pressure flash tank after vacuum furnace heating, in reduced-pressure flash tank, evaporate and gas-liquid separation, the liquid phase of discharging at the bottom of reduced-pressure flash tank is dodged end oil and is introduced vacuum still, the gas phase that vacuum flashing tank deck is discharged dodge top gas discharge flash tank and be condensed into liquid phase after caterpillar; Vacuum flashing jar structure is wherein: reduced-pressure flash tank comprises tank body, comprises gas phase zone and the liquid phase region, bottom on top in tank body, and at least one rotary evaporation dish is set in upper gaseous phase section, and rotary evaporation dish is fixedly installed in the rotating shaft of tank body longitudinal axis center position.
2. in accordance with the method for claim 1, it is characterized in that: cancel the setting of pressure-reducing line for oil-transferring in conventional atmospheric and vacuum distillation, vertical reduced-pressure flash tank is set between vacuum furnace and vacuum distillation tower.
3. in accordance with the method for claim 1, it is characterized in that: a set of pumped vacuum systems is set, and a set of pumped vacuum systems vacuum pumping for vacuum still and reduced-pressure flash tank, arranges control device, controls respectively the vacuum tightness of vacuum still and flash tank.
4. in accordance with the method for claim 1, it is characterized in that: two cover pumped vacuum systems are set, the vacuum pumping respectively of vacuum still and reduced-pressure flash tank.
5. it is characterized in that in accordance with the method for claim 1: 2～4 rotary evaporation dishes are set in same rotating shaft.
6. according to the method described in claim 1 or 5, it is characterized in that: rotary evaporation dish is disc structure or for circle ring disk structure, the diameter of rotary evaporation dish is 20%～80% of reduced-pressure flash tank internal diameter.
7. in accordance with the method for claim 5, it is characterized in that: when more than 2 or 2 rotary evaporation dish is set, the flow-stopping plate that prevents wall stream is set on the tank skin between every two rotary evaporation dishes.
8. in accordance with the method for claim 7, it is characterized in that: flow-stopping plate is to be fixed on to become with tank skin on tank skin the sealing sector structure of 15 °～45 °, upper strata rotary evaporation dish is got rid of to the liquid phase on tank skin and collects and be drained on the rotary evaporation dish of upper strata.
9. in accordance with the method for claim 1, it is characterized in that: opening for feed, flashed vapour discharge port and flash distillation liquid phase relief outlet are set on the tank body of reduced-pressure flash tank, opening for feed is arranged on the top of uppermost position in fig-ure rotary evaporation dish, charging is caused to rotary evaporation dish, flashed vapour discharge port is arranged on the top of tank body, and flash distillation liquid phase relief outlet is arranged on the bottom of tank body.
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| CN103242887B (en) * | 2012-02-06 | 2015-06-17 | 中国石油化工股份有限公司 | Crude oil reduced pressure distillation method and apparatus for reducing yield of residual oil |
| CN103157291A (en) * | 2013-04-01 | 2013-06-19 | 福建致尚生物质材料发展有限公司 | Low-boiling-point substance continuous desorption device of bio-ester plasticizer |
| CN103865565B (en) * | 2014-03-03 | 2015-08-05 | 中山大学 | A kind of crude oil vacuum distillation method eliminating decompression process bottleneck |
| US10072222B2 (en) * | 2014-12-17 | 2018-09-11 | Haldor Topsoe A/S | Process for conversion of a hydrocarbon stream |
| CN106753508B (en) * | 2017-03-22 | 2023-12-19 | 中国石油大学(华东) | Pressure-reducing deep drawing tower for fractionation |
| CN113772763B (en) * | 2021-10-08 | 2023-08-29 | 江西铂格洛智能制造有限公司 | Environment-friendly utilization equipment for heat treatment of wastewater |
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| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| CN101717658A (en) * | 2009-12-03 | 2010-06-02 | 中国石油天然气集团公司 | Multi-vaporization feeding method of oil product fractionator |
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| GB293430A (en) * | 1927-07-06 | 1929-10-07 | Kohlenveredlung Ag | Improved process for distilling, cracking and hydrogenating oils, tars and the like |
| CN1072443A (en) * | 1991-11-20 | 1993-05-26 | 史万年 | A kind of crude oil distillation method and equipment |
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| CN101717658A (en) * | 2009-12-03 | 2010-06-02 | 中国石油天然气集团公司 | Multi-vaporization feeding method of oil product fractionator |
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