CN102309863B - Reduced pressure distillation method and device - Google Patents
Reduced pressure distillation method and device Download PDFInfo
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- CN102309863B CN102309863B CN 201010222356 CN201010222356A CN102309863B CN 102309863 B CN102309863 B CN 102309863B CN 201010222356 CN201010222356 CN 201010222356 CN 201010222356 A CN201010222356 A CN 201010222356A CN 102309863 B CN102309863 B CN 102309863B
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Abstract
The invention discloses a reduced pressure distillation method and a reduced pressure distillation device. A flash tower is arranged between a reduced pressure furnace and a reduced pressure distillation tower, an oil transfer line is canceled, a reduced pressure distillation raw material is heated in the reduced pressure furnace and then directly enters the flash tower, and gas-liquid separation is performed in the flash tower; the liquid phase, namely flash bottom oil, discharged from the bottom of the flash tower is introduced into the reduced pressure distillation tower; and the gas phase, namely flash top gas, discharged from the top of the flash tower is condensed into liquid phase, and the liquid phase is led out of the device. According to the reduced pressure distillation method and the reduced pressure distillation device using the flash tower in back of the reduced pressure furnace, on the one hand, the yield of reduced pressure distillate is improved; and on the other hand, the conventional reduced pressure oil transfer line is canceled, the operation load of the reduced pressure tower is reduced, and the diameter of the reduced pressure tower can be properly reduced so that the equipment investment is saved and the operation cost is lowered.
Description
Technical field
The invention belongs to the petroleum refining field, relate in particular to a kind of process and device of crude oil decompression distillation, more specifically say a kind of and be conducive to improve extracting rate, reduce energy consumption, the vacuum distillation method of reducing investment outlay and device.
Technical background
Crude oil atmospheric vacuum distillation technique is the first operation of petroleum refining, is crude oil to be divided into the component of different boiling range scopes by the method for distilling, to adapt to product and downstream unit to the technological requirement of raw material.The size of the height of its light oil yield and energy consumption directly affects the economic benefit of petroleum refining.Conventional crude oil atmospheric vacuum distillation technique adopts the flow process of " two stove three towers " more: enter primary distillation tower (or flash column) after Crude Pre, then enter atmospheric tower through the atmospheric pressure kiln heating, at the bottom of atmospheric tower, oil is delivered to vacuum tower through the vacuum furnace heating by pressure-reducing line for oil-transferring, complete air-distillation and decompression distillation to crude oil, obtain to satisfy the product of quality requirement and the raw material of downstream unit.
In recent years, the world petroleum demand amount increases year by year with the development of World Economics.In world's crude resources supply, heavy oil and overweight oil supplying ratio progressively increase, light oil, middle matter oil supplying ratio continuous decrease.Therefore, improve the light oil extracting rate in crude oil atmospheric vacuum distillation, 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 development of Chinese national economy, the China's oil total quantity consumed will be broken through 6.5 hundred million tons at the year two thousand twenty.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 " rationalize at utilization of resources maximization, using energy source economized, running cost, the size investment optimization, realize having very important status in the sustainable development of China's oil chemical industry.
For this reason, Chinese scholars compares deep research to the decompression deep drawing of Atmospheric Vacuum Unit, energy-saving and cost-reducing, reduce cost, has made significant headway.Developing direction mainly concentrates on the following aspects: (1) optimizes vacuum system, improves the vacuum of vacuum fractionation tower top; (2) adopt novel, high efficiency packing and direct contact type heat transfer type, reduce the tower overall presure drop, keep higher flash zone vacuum; (3) improve the oil transfer line design, reduce oil transfer line pressure drop and temperature drop; (4) optimize washing section design and operation, strengthen the fractionation concept of washing section; (5) the efficient gas of development of new and liquid distribution trough; (6) adopt the crude distillation method etc. of strengthening.
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 tower; Method two is that incoming mixture just heats by boiling point and is separated into light fraction, midbarrel, heavy distillat, then enter at different feed entrance points respectively and carry out fractionation in tower, from side line extract out successively gently, heavy distillat.Method one is equivalent to side line and has added a stripper, 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 heavy distillat sectional feeding, improved the operation of crude distillation fractionating column, be conducive to improve the distillate yield, carry out fractionation in tower but the light fraction of having separated is sent into again from mixed 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 tower, is provided with a liquid seal device and top at the bottom of tower and separates, and have a vacuum system interface to be connected with the top vacuum system.This utility model separates the rectifying section of vacuum 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 technological 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 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 active 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 operating cost and added chemical reagent.
Patent US4717468 has delivered a kind of distil process that utilizes minimum energy consumption to obtain maximum recovery, by sneak into inert gas in charging, thereby amplitude peak ground reduces the time of staying and the dividing potential drop of charging in heating furnace, optimize the furnace outlet temperature by keeping the certain rate of gasification of crossing of charging, keep minimum furnace outlet temperature, thereby reduce energy consumption.The method can avoid adding hot feed to amplitude peak under the prerequisite of oil product cracking, and reduces its dividing potential drop and improve the feeding gas rate, is conducive to improve extracting rate.But inert gas injecting has increased load and the device operating cost of overhead condensation and pumped vacuum systems, offsets it and reduces the consumption of heating furnace energy, and the energy consumption level of its device still requires study.
Patent CN1287872A has delivered a kind of crude oil atmospheric vacuum distillation method with degree of depth stripping process, at vacuum tower side washing tank in parallel, the feed zone of vacuum tower and stripping section are separated by fluid-tight isolation distributor, the oil gas of stripping section is by entering the bottom of washing tank communicating pipe, take from absorption oil that vacuum tower subtracts three line dischargings and enter downward spray and the reverse mass-and heat-transfer of oil gas that makes progress by washing tank top after cooling, the top of vacuum tower is returned in the tank deck oil gas discharging of washing tank, and at the bottom of tank, discharging is returned to vacuum tower as flushing oil.This technique makes the vacuum tower stripping section 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 tower stripping section, subtracts preferably third fractional oil as flushing oil with quality, waits research on economic benefit.
Patent CN101376068A discloses a kind of atmospheric vacuum distillation method with vacuum flasher and equipment, is a vacuum flasher is set before reduced crude enters vacuum furnace.The oil heating furnace that advances to reduce pressure at the bottom of flash column, flash column top gas enter that certain sideline product close with flash column 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 treating capacity, improves extracting rate, reduces the purpose of energy consumption.But at the bottom of atmospheric tower, oil enters flash column, because the temperature of oil at the bottom of atmospheric tower is relatively low, the vacuum of adding the stokehold flash column is relatively not high, the effect of flash column flash distillation gasification is limited, and the flash distillation top gaseous phase enters vacuum tower, be equivalent to vacuum tower sectional feeding after flash distillation, not in the fractionation that fundamentally changes vacuum tower.
In the last few years, replaced gradually high speed oil transfer line in the past with major diameter (more than generally diameter can reach 2m) low speed pressure-reducing line for oil-transferring technology in vacuum distillation apparatus, its objective is under the condition that guarantees vacuum tower feed zone vaporization minute rate, reduce as far as possible the vacuum furnace outlet temperature, to prevent tube coking.In other words, be under the heater outlet temperature of regulation, improve as far as possible tower feed zone vaporization rate, divide rate to improve product.For reaching this purpose, only have and reduce as far as possible boiler tube and oil transfer line pressure drop, make the oil product evaporation point in advance.(to guarantee liquid phase, certain separation time is arranged due to oil transfer line more than 15m must be adopted, be conducive to improve the quality of products and the vacuum tower extracting rate), therefore the oil transfer line of the long distance of major diameter accounts for the larger proportion of vacuum distillation apparatus investment, the factors such as thermal loss and pressure drop increase all are unfavorable for the operation of vacuum distillation tower simultaneously, and the thermal stress, the thermal walking that form cause certain difficulty to design and installation in security.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of vacuum distillation method and device, can obviously improve the extracting rate in vacuum distillation process, reduce plant energy consumption, and reduce plant investment.
Vacuum distillation method of the present invention comprises: cancel pressure-reducing line for oil-transferring, between vacuum furnace and vacuum distillation tower, flash column is set, the decompression distillation raw material enters flash column after heating through vacuum furnace, carry out gas-liquid separation in flash column, the liquid phase of discharging at the bottom of flash column (hereinafter referred to as dodging end oil) is introduced vacuum distillation tower, and the gas phase that the flash distillation tower top is discharged (hereinafter referred to as dodging top gas) is condensed into after liquid phase as product.
In vacuum distillation method of the present invention, be condensed into the liquid phase ejector after dodging top gas and entering vacuum furnace decompression distillation raw material heat exchange before, perhaps with a certain of vacuum distillation tower or certain several cut mixing ejector.The decompression distillation raw material is generally oil at the bottom of the atmospheric distillation tower tower (hereinafter referred to as oil of the normal end).
In vacuum distillation method of the present invention, cancelled the setting of pressure-reducing line for oil-transferring in conventional decompression distillation, vertical flash column is set between vacuum furnace and vacuum tower, can compactly arranges between flash column and vacuum furnace, vacuum distillation tower, need not to consider to arrange the oil transfer line setting that is not less than 15 meters.Vertical flash column is mainly used in gas-liquid separation, in tower, column plate can be set, and 1～3 block of column plate perhaps is set on top, and it is the void tower structure that column plate perhaps is not set.
In vacuum distillation method of the present invention, other technology contents is technology contents well known to those skilled in the art as vacuum furnace, vacuum distillation tower.
Vacuum distillation apparatus of the present invention comprises vacuum furnace, vacuum flasher and vacuum distillation tower, cancel oil transfer line between vacuum furnace and vacuum distillation tower, the vacuum furnace outlet directly connects flash column, the discharging of flash column bottom liquid phases is introduced vacuum distillation tower by pipeline, and flash column top and decompression distillation raw material heat-exchanger rig are with pipeline communication.
Vacuum distillation apparatus of the present invention can arrange a cover pumped vacuum systems, and vacuum distillation tower and flash column can arrange control device with a cover pumped vacuum systems vacuum pumping, control respectively the vacuum of vacuum distillation tower and flash column; Two cover pumped vacuum systems also can be set, the vacuum pumping respectively of vacuum distillation tower and flash column.The vacuum degree control of flash column is arranged on dodges on top gas condenser knockout drum afterwards.The vacuum pumping of flash column and vacuum distillation tower can be adopted the method and apparatus of this area routine.
Compared with prior art, the present invention has the following advantages:
1) outlet of still directly is communicated with vacuum flasher, and vacuum tower is introduced in the discharging of flash column bottom liquid phases.Shortened the technological process that oil of the normal end heats-enter vacuum tower, greatly reduced process pressure drop and the thermal loss of pressure-reducing line for oil-transferring in prior art, made the vacuum furnace internal pressure lower, oil of normal end gasification point in vacuum furnace shifts to an earlier date, and the outlet of still rate of gasification is higher.
2) by between vacuum furnace and vacuum tower, vacuum flasher being set, improved the charging gas-liquid separation.
3) outlet of still directly is communicated with vacuum flasher, and vacuum tower is introduced in the discharging of flash column bottom liquid phases.Cancel pressure-reducing line for oil-transferring, the reduced pressure distillation process design has been optimized in the oil transfer line thermal walking of having avoided extra heavy pipe footpath, large pipe range oil transfer line low speed segment to cause.Through adjusting, the cost of flash column is starkly lower than the cost of extra heavy pipe footpath, large pipe range oil transfer line.
4) dodge end oil and enter separately vacuum distillation tower, dodge top gas and do not enter vacuum distillation tower, significantly reduce the processing load of vacuum distillation tower, eliminated " bottleneck " of vacuum tower treating capacity, be conducive to the capacity expansion revamping of old device.
5) dodge end oil and enter separately vacuum distillation tower, reduced to a certain extent the required theoretical plate of vacuum tower, can suitably reduce tower height and tower diameter, the economy system investment.
6) dodge end oil and enter separately vacuum distillation tower, dodge top gas and do not enter vacuum distillation tower, reduced the gas phase load of vacuum distillation tower, full tower pressure drop is reduced, be conducive to improve the decompression extracting rate, and significantly reduced the Top of Vacuum Tower condensation and vacuumized load.Decompression distillation low energy consumption, high vacuum, the operation of high extracting rate have been realized.Effectively reduce the yield that is worth low decompression residuum.
7) dodge end oil and enter separately vacuum distillation tower, the Vapor Entrainment of having avoided the gas-liquid mixed charging to cause has guaranteed depressurised side line products quality.
8) dodge top gas and carry out heat exchange with oil of the normal end, reduced the vacuum furnace load, reduce plant energy consumption.
9) technology of the present invention is rationally advanced, and energy consumption level is low, and equipment investment is few, and the decompression residuum yield is low, for the transformation of old device, has that the scrap build amount is few, investment is low, and the transformation duration is short, and the device income is the advantage such as quick obviously; For the design and construction of new equipment, have technique rationally advanced, energy consumption level is low, and size investment is little, and equipment takes up an area the characteristics such as few.
The specific embodiment
The inventive method directly is communicated with a flash column in the vacuum furnace outlet, and vacuum tower is introduced in the discharging of flash column bottom liquid phases.The gas-liquid flash separation is carried out in the gas-liquid mixed charging that vacuum furnace heat air rate is very high under the condition of flash column condition of high vacuum degree.Dodge top gas by tank deck warp and vacuum furnace charging heat exchange, then after cooler is cooled to full liquid phase, as the discharging of product liquid phase.Dodge end oil and directly enter the vacuum distillation tower feed zone, further carry out fractionation in the vacuum distillation tower of stripped vapor at the bottom of with tower, from vacuum distillation tower lateral line withdrawal function vacuum distillate, decompression residuum is extracted out at the bottom of by tower, and tower top connects pumped vacuum systems.Cancel traditional oil transfer line, only use a small amount of common pipe.
Oil of the normal end first enters vacuum furnace after charging/sudden strain of a muscle top gas heat exchanger heat exchange rising temperature, after temperature is heated to 390 ℃～400 ℃ in vacuum furnace, oil gas rate of the normal end reaches 50%～60% (mass percent, lower same), then enter vacuum flasher, gas-liquid is separated fully in vacuum flasher, gas phase is discharged with oil of the normal end by tank deck through tank deck Froth demist net and is lowered the temperature in charging/sudden strain of a muscle top gas heat exchanger heat exchange, then is cooled to full liquid phase as dodging the top product discharge through dodging the top gas condenser.Liquid phase is dodged end oil and is directly entered the vacuum distillation tower feed zone, carries out decompression distillation under the effect of stripped vapor and decompression distillation tower top pumped vacuum systems, obtains sideline product and discharging in tower.Decompression residuum is by the VACUUM TOWER BOTTOM discharging.Vacuum flasher and vacuum distillation tower have respectively the liquid level detection display.
Vacuum distillation tower in the present invention can be the fuel type vacuum distillation tower, can be also the Lube Type vacuum distillation tower; Can be wet distiller, wet distiller also can decline; The lateral line discharging number specifically arranges as required.
After vacuum furnace of the present invention with vacuum distillation method and the equipment of flash column, improved the crude oil reduced pressure distillation process, lower pressure heat air rate in vacuum furnace is reached 50%～60% mixed feeding and carry out gas-liquid separation in vacuum flasher, need not establish again long pressure-reducing line for oil-transferring low speed segment and carry out gas-liquid separation (it is 15m that prior art requires oil transfer line low speed segment length), the horizontal thermal walking of oil transfer line of having avoided extra heavy pipe footpath, large pipe range low speed segment to cause.Flash distillation top gaseous phase and vacuum furnace charging are carried out after heat exchange, condensation directly as product, and liquid phase enters separately vacuum distillation tower.Thereby reduced the processing load of vacuum distillation tower, reduced to a certain extent the required theoretical plate of vacuum distillation tower, can suitably reduce tower height and tower diameter, significantly reduced the condensation of decompression distillation tower top and vacuumized load simultaneously; And the Vapor Entrainment that can avoid the gas-liquid mixed charging to cause, guaranteed depressurised side line products quality.Confirm through analog computation, process the residual oil yield few 1%～2% of the existing process route of identical raw material process of the present invention, and the flash distillation tower top accounts for sensible heat that the oil gas of charging 50%～60% contains and latent heat and is enough to the load of vacuum furnace is saved in oil heat exchange to 390 of the normal end ℃～400 ℃ greatly.
The present invention can open large vacuum furnace load when start up, heating is fed to 390 ℃～400 ℃, guarantees the decompression distillation operation.Go into operation stable after, take full advantage 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.
Embodiment 1:
Method of the present invention is used for the design of certain newly-built Atmospheric Vacuum Unit.
The treating capacity of relief portion separating device is 1,200,000 ton/years, and the decompression flow process comprises vacuum furnace, flash column, vacuum tower.Vacuum tower is regular packed tower, adopts the wet process operation, and tower bottom blowing vapour amount is 1% of tower charging, and the tower top operating pressure is 1.315kPa, and full tower pressure drop is 600Pa～750Pa.
Oil of the normal end is fed into vacuum distillation apparatus with 150 tons/hour, enters into vacuum flasher after vacuum furnace is heated to 390 ℃～400 ℃.Cancel oil transfer line, flash column directly is connected with vacuum tower, and flash column pressure is 10kPa.Dodge top gas after adiabatic flash and account for 45.67% of charging, dodge end oil and enter vacuum tower, from vacuum tower lateral line withdrawal function product.Decompression residuum discharging at the bottom of the tower.Tower top oil gas is cooling through condenser, and fixed gas is extracted out by vacuum pumping pump, keeps vacuum in tower.
Following table has been listed employing the present invention (option A) and has been adopted the Data Comparison that carries out analog study at aspects such as decompression extracting rate, plant energy consumption, investments with the atmospheric vacuum distillation method of vacuum flasher and the patent CN101376068A of equipment (option b).
Option A and option b contrast situation
As seen from the table, although aspect equipment investment the multiplex heat exchanger of option A, the vacuum tower tower diameter is less, investment reduces, corresponding tower internals and filler investment also will reduce; And vavuum pump power is well below option b; Although the lower slightly and option A of option b vacuum furnace load aspect plant energy consumption at steam consumption, overhead condensation with vacuumize load higher than option A, and does not recover energy; Result in option A aspect the decompression extracting rate is better than option b far away, and the degree of deep drawing is also relatively high.
Embodiment 2:
Method of the present invention is used for the capacity expansion revamping of certain Atmospheric Vacuum Unit, and the normal pressure part is identical with conventional atmospheric and vacuum distillation unit, and the decompression part mainly comprises vacuum furnace, flash column, vacuum tower.
Vacuum tower is regular packed tower, and the tower top operating pressure is 1.315kPa, and full tower pressure drop is 600Pa～750Pa.
Oil of the normal end enters vacuum distillation apparatus, enters into vacuum flasher after vacuum furnace is heated to 390 ℃～400 ℃.Cancel oil transfer line, flash column directly is connected with vacuum tower, and flash column pressure is 10kPa, dodges top gas after adiabatic flash and accounts for 45.67% of charging, dodges end oil and enters vacuum tower 15, from vacuum tower lateral line withdrawal function product 10,11.Go out decompression residuum at the bottom of tower, yield accounts for 34.43% (m) of combined feed.
This device capacity expansion revamping relief portion is divided and is kept original vacuum furnace and vacuum tower, and vacuum tower internals and filler are transformed.Remove the oil transfer line low speed segment, newly-increased main equipment is vacuum flasher, oil charging of the normal end/sudden strain of a muscle top gas heat exchanger.After transformation, device decompression part working ability can improve 20%～50%, and plant energy consumption reduces by 3%～5%, and the decompression residuum yield reduces by 2%～5%.
Following table has been listed employing the present invention (option A) and has been adopted the Data Comparison that certain atmospheric and vacuum distillation unit decompression part transformation situation is carried out analog study with the atmospheric vacuum distillation method of vacuum flasher and the patent CN101376068A of equipment (option b).
Option A and option b comparable situation
As can be seen from the table, adopt option A to carry out capacity expansion revamping to old device more less than the newly-built equipment of scheme B, engineering amount of reform is little, thereby construction investment is less, and the transformation duration is short; Also obviously better on the device income.Option A has larger rectification advantage.
Claims (7)
1. vacuum distillation method, it is characterized in that: cancel pressure-reducing line for oil-transferring, between vacuum furnace and vacuum distillation tower, flash column is set, the decompression distillation raw material enters flash column after heating through vacuum furnace, carry out gas-liquid separation in flash column, the liquid phase of discharging at the bottom of flash column is namely dodged end oil and is introduced vacuum distillation tower, the gas phase that the flash distillation tower top is discharged is namely dodged top gas and is condensed into after liquid phase as product.
2. in accordance with the method for claim 1, it is characterized in that: be condensed into the liquid phase ejector after dodging top gas and entering vacuum furnace decompression distillation raw material heat exchange before, perhaps with a certain of vacuum distillation tower or certain several cut mixing ejector.
3. it is characterized in that in accordance with the method for claim 1: the decompression distillation raw material is oil at the bottom of the atmospheric distillation tower tower.
4. vacuum distillation apparatus, comprise vacuum furnace, vacuum distillation tower, it is characterized in that: also comprise vacuum flasher, cancel oil transfer line between vacuum furnace and vacuum distillation tower, the vacuum furnace outlet directly connects flash column, the discharging of flash column bottom liquid phases is introduced vacuum distillation tower by pipeline, and flash column top and decompression distillation raw material heat-exchanger rig are with pipeline communication.
5. according to device claimed in claim 4, it is characterized in that: flash column is used for gas-liquid separation, and column plate is set in tower, is perhaps the void tower structure.
6. according to device claimed in claim 4, it is characterized in that: vacuum distillation apparatus arranges a cover pumped vacuum systems, and vacuum distillation tower and flash column share a cover pumped vacuum systems vacuum pumping.
7. according to device claimed in claim 4, it is characterized in that: two cover pumped vacuum systems are set, the vacuum pumping respectively of vacuum distillation tower and flash column.
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| CN 201010222356 CN102309863B (en) | 2010-07-07 | 2010-07-07 | Reduced pressure distillation method and device |
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| CN102309863B true CN102309863B (en) | 2013-11-06 |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103242896B (en) * | 2012-02-06 | 2015-02-18 | 中国石油化工股份有限公司 | Reduced pressure distillation method with low energy consumption and deep total distillation rate |
| 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 |
| CN103540357B (en) * | 2012-07-09 | 2015-04-08 | 中国石油化工集团公司 | Heavy oil treatment process |
| CN103540354B (en) * | 2012-07-09 | 2015-11-25 | 中国石油化工集团公司 | A kind of combination heavy oil treatment processes |
| CN103224806A (en) * | 2013-01-10 | 2013-07-31 | 盘锦兴达沥青有限公司 | Different pressure distillation apparatus and process method |
| CN106590715B (en) * | 2017-01-23 | 2022-06-14 | 中冶焦耐(大连)工程技术有限公司 | Light oil and wide fraction separation process and equipment suitable for tar distillation |
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| CN1100746A (en) * | 1994-01-24 | 1995-03-29 | 杨华臣 | Up flow type heavy oil viscosity reducing and cracking process and equipment |
| CN2242892Y (en) * | 1996-02-09 | 1996-12-18 | 清华大学 | Compound crude-oil decompression tower |
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| ATE485355T1 (en) * | 2000-11-03 | 2010-11-15 | Sanford P Brass | METHOD FOR REDUCING EMISSIONS DURING ASPHAL PRODUCTION |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1100746A (en) * | 1994-01-24 | 1995-03-29 | 杨华臣 | Up flow type heavy oil viscosity reducing and cracking process and equipment |
| CN2242892Y (en) * | 1996-02-09 | 1996-12-18 | 清华大学 | Compound crude-oil decompression tower |
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