CN103059919A - Vacuum distillation method for improving distillate yield and device - Google Patents
Vacuum distillation method for improving distillate yield and device Download PDFInfo
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Abstract
The invention discloses a crude oil vacuum distillation method and a device. According to the invention, a vacuum flash tank is added to a vacuum heavy oil outlet at a vacuum distillation tower bottom so as to make the vacuum heavy oil flowing out of the vacuum tower bottom undergo flashing in the vacuum flash tank under the condition of a vacuum degree higher than that of the vacuum tower bottom. A vacuum flash tank top gas enters a gas-liquid separation tank after heat exchange and cooling. The top of the gas-liquid separation tank is in connection with a vacuum-pumping system to maintain the vacuum degree of the flash tank. The vacuum distillate oil extracted from the bottom is taken as a product, and vacuum residual oil is extracted from the vacuum flash tank bottom. The vacuum distillation method disclosed in the invention improves the crude oil vacuum distillation process, and makes the vacuum heavy oil enter the vacuum flash tank with a high vacuum degree to undergo further flashing, thus acquiring relatively light distillate from the vacuum heavy oil by flashing completely and ensuring that the content of distillate lower than 500DEG C in vacuum residual oil is reduced to a minimum. Therefore, the distillate yield of vacuum distillation can be improved, and the economic benefits of the device can be increased.
Description
Technical field
The invention belongs to the 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 that crude oil is divided into different boiling range scopes by the method for distillation, 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 affects the economic benefit of refining of petroleum.Usually in the energy consumption and vacuum residuum with total extracting rate, the device of device benzoline＜500 ℃ of cut content are as the indexs of weighing the device operation.Conventional crude oil atmospheric vacuum distillation technique adopts the flow process of " two stoves, three towers " more: enter primary tower (or flashing tower) after the crude oil upgrading, then enter atmospheric tower through the atmospheric pressure kiln heating, 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 petroleum demand amount is along with expanding economy increases year by year, heavy oil and overweight oil supplying ratio progressively increase in the crude resources supply, lightweight oil, middle matter oil supplying ratio continuous decrease.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 Refining Chemical 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, 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, crude oil atmospheric vacuum distillation device as " tap " rationalizes at utilization of resources maximization, energy utilization economized, running cost, the size investment optimizing, has very important status 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 to 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, so that flash zone keeps higher vacuum at the bottom of the tower; (3) improve the transfer line design, reduce transfer line Pressure Drop and temperature and fall; (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, then enter at different feed entrance points respectively 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 of this utility model is complicated simultaneously, the 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, at 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 the absorption oil that vacuum distillation tower subtracts three line dischargings and after cooling, 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 discharging is returned vacuum distillation tower as washing oil at the bottom of the tank.This technique 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 the method just is optimized improvement to the vacuum distillation tower stripping stage, subtracts preferably third fractional oil 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, 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.
Patent 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 advances to reduce pressure at the bottom of the 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 the raising treatment capacity, improves extracting rate, reduces the purpose of energy consumption.But oil enters 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 relatively not high, the effect of flashing tower flash distillation gasification is limited, and the flash distillation top gaseous phase enters 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
For the deficiencies in the prior art, one of the technical problem to be solved in the present invention provides a kind of vacuum distillation method that improves extracting rate, can obviously improve the extracting rate in the crude oil vacuum distillation process, increases the device economic benefit.
A kind of vacuum distillation method that improves extracting rate of the present invention comprises following content: crude oil oil (hereinafter referred to as oil of the normal end) at the bottom of the atmospheric tower after the normal pressure distillation by the vacuum furnace heating, enters vacuum still through pressure-reducing line for oil-transferring and carries out underpressure distillation; From vacuum still lateral line withdrawal function decompression benzoline, extract depressed heavy oil out at the bottom of the vacuum still tower and enter a reduced-pressure flash tank; Vacuum flashing tank top gas phase (hereinafter referred to as dodging top gas) connects pumped vacuum systems by knockout drum, keeps the higher vacuum tightness of reduced-pressure flash tank.The gas-liquid separation pot bottom is discharged vacuum distillate, the vacuum residuum at the bottom of the flash tank after the flash distillation of the discharge degree of depth.
The present invention improves in the vacuum distillation method of extracting rate, the depressed heavy oil of discharging at the bottom of the vacuum still tower is introduced reduced-pressure flash tank by hole enlargement pipeline step by step, make lighting end in the vacuum residuum divide to depress at the oil gas that reduces step by step and be evaporated, finally in the complete flash distillation of reduced-pressure flash tank.
The present invention improves in the vacuum distillation method of extracting rate, and the pressure of reduced-pressure flash tank is than low 2 kPa of vacuum still tower bottom pressure ~ 5 kPa, 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 height of reduced-pressure flash tank is in vacuum still, and the reduced-pressure flash tank opening for feed is positioned at 30% ~ 70% place of liquid level at the bottom of the vacuum still tower, preferred 45% ~ 55%.On the one hand guarantee that vacuum still can not be evacuated, prevent on the other hand the vacuum still tower at the bottom of the liquid phase residual overlong time cause coking.
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, needs the logistics heat exchange of heating in vacuum flashing head space gas phase and oil of the normal end or the device, reduces 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 at the bottom of the reduced-pressure flash tank tank by pump, liquid automatic control pump discharge flow at the bottom of the tank.
The present invention improves in the vacuum distillation method of extracting rate, one cover pumped vacuum systems can be set, vacuum still and reduced-pressure flash tank share a cover pumped vacuum systems vacuum pumping, and control device can be set, and control respectively the vacuum tightness of vacuum still and flash tank; Two cover pumped vacuum systems also can be set, the respectively vacuum pumping of vacuum still and reduced-pressure flash tank.The vacuum degree control of reduced-pressure flash tank is arranged on dodges on the top gas condenser knockout drum afterwards.The vacuum pumping of reduced-pressure flash tank and vacuum still can be adopted the method and apparatus of this area routine.
The present invention improves in the vacuum distillation method of extracting rate, and other technology contents is technology contents well known to those skilled in the art such as design and the operation of vacuum furnace, vacuum still, transfer line.
Another technical problem that the present invention will solve provides a kind of crude oil vacuum distillation apparatus that improves extracting rate.Technical scheme is: a kind of vacuum distillation apparatus that improves extracting rate, comprise vacuum furnace, transfer line, vacuum still, reduced-pressure flash tank, transfer line connects vacuum furnace and vacuum still, the underpressure distillation tower bottom is communicated with reduced-pressure flash tank by the pipeline of hole enlargement step by step, and the 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 reduced-pressure flash tank is set behind vacuum still, make cut relatively light in the vacuum residuum further obtain flash distillation, improve on the one hand the decompression yield of this device; Reduce on the other hand downstream coking or visbreaking etc. and process the load of vacuum residuum device, 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, make in the vacuum residuum＜cuts of 500 ℃ and＜538 ℃ reduce greatly.
3) reduced-pressure flash tank 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.
4) dodge top gas and carry out heat exchange with oil of the normal end, reduced the vacuum furnace load, reduce plant energy consumption.
5) 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, transforms the duration short, and the device income is the advantage such as quick obviously; For the design and construction of new device, have technique rationally advanced, energy consumption level is low, vacuum distillate yield high.
Description of drawings
Fig. 1 improves the vacuum distillation method process flow diagram of extracting rate.
Wherein 1 is normal end oil (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 is reduced-pressure flash tank; 12 is flash tank top gas liquid separating tank.
Embodiment
The inventive method depressed heavy oil outlet at the bottom of the vacuum still tower connects a reduced-pressure flash tank, so that oil of the normal end carries 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 reduced-pressure flash tank condition of high vacuum degree.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 relatively high vacuum tightness of reduced-pressure flash tank; The bottom is extracted vacuum distillate out as product.Vacuum residuum is extracted out at the bottom of the reduced-pressure flash tank tank.
As shown in Figure 1, oil of the normal end 1 enters vacuum furnace 2 first 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 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 cat head pumped vacuum systems 8, carry out underpressure distillation, obtain sideline product discharging 9 in the tower.Depressed heavy oil 5 by the vacuum still tower at the bottom of discharging, introduce reduced-pressure flash tank 11 through hole enlargement 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 the heat exchange cooling, the separating tank top connects pumped vacuum systems, keeps the higher vacuum tightness of reduced-pressure flash tank 11, and the separating tank bottom is extracted vacuum distillate 10 out as product discharge.The reduced-pressure flash tank liquid phase is extracted out at the bottom of by tank, as vacuum residuum 6 dischargings.
Reduced-pressure flash tank 11, vacuum still 3 and knockout drum 12 have respectively Level Detection to show.
Vacuum still described in the present invention can be the fuel type vacuum still, also can be the Lube Type vacuum still; Can be wet distiller, wet distiller also can decline; Sideline product discharging number specifically arranges as required.
Behind the vacuum still of the present invention with the vacuum distillation method of reduced-pressure flash tank, 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 reduced-pressure flash tank that depressed heavy oil at the bottom of the tower enters condition of high vacuum degree carries out further flash distillation, so that the relatively light complete flash distillation of cut is out in the depressed heavy oil, guarantee in the vacuum residuum＜500 ℃ cut content is to minimum, thereby improve the extracting rate of underpressure distillation, increase the economic benefit of device.Calculate confirmation through Aspen flowsheeting software simulation, process 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 the design of certain newly-built crude oil atmospheric vacuum distillation 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 ton/years, and the decompression flow process comprises vacuum furnace, vacuum still, reduced-pressure flash tank.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.
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 ℃.Reduced-pressure flash tank directly is connected with discharging at the bottom of the vacuum distillation tower tower, 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 vacuum still tower, oil is as the vacuum residuum discharging at the bottom of the reduced-pressure flash tank.From vacuum distillation tower lateral line withdrawal function product 9.Vacuum residuum is the 36.22%(quality to the yield of combined feed total feed), the cut point of decompressed wax oil reaches 588 ℃.
Comparative example 1
Relate to equally the design of embodiment 1 newly-built 1,000 ten thousand ton/years of crude oil atmospheric vacuum distillation devices.The treatment capacity of reliever is 5,000,000 ton/years.Adopt disclosed atmospheric vacuum distillation method with 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 Atmospheric Vacuum Unit, the normal pressure part is identical with conventional atmospheric and vacuum distillation unit, the decompression part adopts the vacuum distillation method process flow diagram of the raising extracting rate shown in the accompanying drawing 1, mainly comprises vacuum furnace, vacuum distillation tower distillation, reduced-pressure flash tank.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.
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 ℃.Reduced-pressure flash tank directly is connected with discharging at the bottom of the vacuum distillation tower tower, 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 vacuum still tower, oil is as the vacuum residuum discharging at the bottom of the reduced-pressure flash tank.From vacuum distillation tower lateral line withdrawal function product 9.Vacuum residuum is the 36.22%(quality to the yield of combined feed total feed), the cut point of decompressed wax oil reaches 588 ℃.
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 reduced-pressure flash tank, oil charging of the normal end/sudden strain of a muscle top gas interchanger.The vacuum residuum yield reduces by 1%～1.5% after transforming.
Comparative example 2
The capacity expansion revamping that relates to equally certain crude oil atmospheric vacuum distillation device among the embodiment 2.Disclosed atmospheric vacuum distillation method with 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 ton/years of atmospheric and vacuum distillation unit, relief portion divides charging to be about 655 tons/hour, embodiment 2 reduces residual oil yields 1.5%, comes in 300 yuan/tons of residual oil and mixed gatch price differences, year amounts to Renminbi: 655 * 1.5% * 300 * 8400=2475.9 ten thousand yuan.Add the part of device reduction energy consumption, the device economic benefit highly significant of obtaining.
Claims (11)
1. vacuum distillation method that improves extracting rate comprises 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; From vacuum still lateral line withdrawal function decompression benzoline, extract depressed heavy oil at the bottom of the vacuum still tower out and enter a reduced-pressure flash tank, vacuum flashing tank top gas phase connects pumped vacuum systems by knockout drum, keep the higher vacuum tightness of reduced-pressure flash tank, the gas-liquid separation pot bottom is discharged vacuum distillate, discharges the vacuum residuum after the flash distillation at the bottom of the reduced-pressure flash tank.
2. in accordance with the method for claim 1, it is characterized in that, the depressed heavy oil of discharging at the bottom of the described vacuum still tower is introduced reduced-pressure flash tank by hole enlargement pipeline step by step, so that dividing to depress at the oil gas that reduces step by step, the lighting end in the depressed heavy oil is evaporated, and in the complete flash distillation of reduced-pressure flash tank.
3. in accordance with the method for claim 1, it is characterized in that, the pressure of described reduced-pressure flash tank is than low 2 kPa of vacuum still tower bottom pressure ~ 5 kPa.
4. in accordance with the method for claim 1, it is characterized in that, described reduced-pressure flash tank is horizontal tank.
5. in accordance with the method for claim 1, it is characterized in that, oil carries out first cooling off after the heat exchange again at the bottom of described vacuum flashing tank top gas phase and the atmospheric tower.
6. in accordance with the method for claim 1, it is characterized in that, the position height of described reduced-pressure flash tank is in vacuum still, and the reduced-pressure flash tank opening for feed is positioned at 30% ~ 70% place of liquid level at the bottom of the vacuum still tower.
7. 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 the described reduced-pressure flash tank tank by pump, liquid automatic control pump discharge flow at the bottom of the tank.
8. in accordance with the method for claim 1, it is characterized in that, described vacuum still and reduced-pressure flash tank share a cover pumped vacuum systems, control device is set controls respectively separately vacuum tightness.
9. in accordance with the method for claim 8, it is characterized in that, the vacuum degree control of described reduced-pressure flash tank is arranged on the knockout drum of vacuum flashing tank top gas phase.
10. in accordance with the method for claim 1, it is characterized in that, two cover pumped vacuum systems are set, and vacuum still and reduced-pressure flash tank are controlled respectively vacuum tightness.
11. vacuum distillation apparatus that improves 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, the underpressure distillation tower bottom is communicated with reduced-pressure flash tank by the pipeline of hole enlargement step by step, and the vacuum flashing tank top is communicated with pumped vacuum systems by knockout drum.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109613133A (en) * | 2018-12-19 | 2019-04-12 | 东营联合石化有限责任公司 | Each fraction of residual oil can extracting rate measuring method in a kind of crude oil |
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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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| 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 |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109613133A (en) * | 2018-12-19 | 2019-04-12 | 东营联合石化有限责任公司 | Each fraction of residual oil can extracting rate measuring method in a kind of crude oil |
| CN109613133B (en) * | 2018-12-19 | 2022-04-29 | 东营联合石化有限责任公司 | Method for measuring extractable rate of each fraction of residual oil in crude oil |
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