CN102309863A - Reduced pressure distillation method and device - Google Patents
Reduced pressure distillation method and device Download PDFInfo
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- CN102309863A CN102309863A CN2010102223561A CN201010222356A CN102309863A CN 102309863 A CN102309863 A CN 102309863A CN 2010102223561 A CN2010102223561 A CN 2010102223561A CN 201010222356 A CN201010222356 A CN 201010222356A CN 102309863 A CN102309863 A CN 102309863A
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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, a kind of vacuum distillation method and device of improving extracting rate, cut down the consumption of energy, reducing investment outlay of helping of more specifically saying so.
Technical background
Crude oil atmospheric vacuum distillation technology is first procedure of petroleum refining, is that the method through distillation is divided into the component of different boiling range scopes with crude oil, to adapt to product and the downstream unit technological requirement to raw material.The size of the height of its light oil yield and energy consumption directly influences the economic benefit of petroleum refining.Conventional crude oil atmospheric vacuum distillation technology adopts the flow process of " two stoves, three towers " more: get into primary distillation tower (or flash column) after the Crude Pre; Get into atmospheric tower through the atmospheric pressure kiln heating then; Oil is delivered to vacuum tower through the vacuum furnace heating by pressure-reducing line for oil-transferring at the bottom of the atmospheric tower; Completion obtains to satisfy the product of quality requirement and the raw material of downstream unit to the air-distillation and the decompression distillation of crude oil.
In recent years, the world oil demand increases with the development of World Economics year by year.Heavy oil and overweight oil supplying ratio progressively increase in world's crude resources supply, and light oil, middle matter oil supplying ratio continue to descend.Therefore, improve the light oil extracting rate in the 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 refinery 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, optimizing processing technology has been the imperative act of China's oil chemical industry.In device maximization and the integrated novel refinery design of refinery; Crude oil atmospheric vacuum distillation device as " tap " rationalizes at utilization of resources maximization, using energy source economized, running cost, the size investment optimization, has critical role in the sustainable development of realization China's oil chemical industry.
For this reason, Chinese scholars to the decompression deep drawing of crude oil atmospheric and vacuum distillation unit, energy-saving and cost-reducing, reduce investment and carried out more deep research, made significant headway.Developing direction mainly concentrates on the following aspects: the decompression vacuum pumping system is optimized in (1), improves the vacuum of vacuum fractionation cat head; (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, the fractionation notion of reinforced washing section; (5) development of new gas and liquid distribution trough efficiently; (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 the tower; Method two is an incoming mixture by boiling point height heating and separating is light fraction, midbarrel, heavy distillat, in different feed entrance points gets into tower, carries out fractionation respectively then, 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; Help improving the distillate yield, carry out fractionation in the tower but send into the light fraction of from mixed feeding, having separated once more, 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 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 tower and the deep drawing section of bottom through liquid seal device; Can oil quality and extracting rate be paid attention to respectively; Can relatively improve the decompression extracting rate, but the oil quality of deep drawing is difficult to satisfy the technological requirement of downstream unit to 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, through changing the light oil yield that the intermolecular active force of crude oil improves atmospheric and vacuum distillation.But this method does not fundamentally change distillation technique in technology, and will consume a large amount of additives, has increased device operating cost and the operation easier of adding chemical reagent.
Patent US4717468 has delivered a kind of distil process that utilizes minimum energy consumption to obtain maximum recovery; Be through in charging, sneaking into inert gas; Thereby amplitude peak ground reduces the time of staying and the dividing potential drop of charging in heating furnace; Optimize the furnace outlet temperature through keeping the certain rate of gasification of crossing of charging, keep minimum furnace outlet temperature, thereby cut down the consumption of energy.This method can add hot feed in amplitude peak ground under the prerequisite of avoiding the oil product cracking, and reduces its dividing potential drop and improve the charging rate of gasification, helps improving extracting rate.But inert gas injecting has increased the 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 that has degree of depth stripping process; Be at washing tank of vacuum tower side parallel connection; The feed zone of vacuum tower and stripping section are isolated distributor by fluid-tight and are separated; The oil gas of stripping section gets into the bottom of washing tank through communicating pipe; Take from the oily reverse mass-and heat-transfer of oil gas that after cooling, is got into downward spray and made progress by washing tank top of absorption that vacuum tower subtracts three-way discharging, the top of vacuum tower is returned in the tank deck oil gas discharging of washing tank, and a jar end discharging is returned vacuum tower as flushing oil.This technology makes the vacuum tower stripping section experience a steam stripped process of the degree of depth through setting up washing tank, helps improving the decompression extracting rate.But this method has just carried out optimizing improvement to the vacuum tower stripping section, subtracts third fractional oil preferably as flushing oil with quality, on economic benefit, waits research.
Patent CN101376068A discloses a kind of atmospheric vacuum distillation method and equipment that has vacuum flasher, is that a vacuum flasher is set before reduced crude is gone into vacuum furnace.The oil heating furnace that advances to reduce pressure at the bottom of the flash column, flash distillation tower overhead gas get into certain sideline product close with flash distillation tower overhead gas cut extract out mouth above or below.This method reaches the raising treating capacity through increasing the flow process that vacuum flasher improves atmospheric and vacuum distillation unit, improves extracting rate, the purpose that cuts down the consumption of energy.But oil is gone into flash column at the bottom of the atmospheric tower; Because the temperature of oil is relatively low at the bottom of the atmospheric tower; The vacuum of adding the stokehold flash column is not high relatively, and the effect of flash column flash distillation gasification is limited, and flash distillation cat head gas phase is gone into vacuum tower; Be equivalent to vacuum tower sectional feeding after the flash distillation, not in the fractionation that fundamentally changes vacuum tower.
In the last few years; Replaced high speed oil transfer line in the past gradually with major diameter (general diameter can reach more than the 2m) low speed pressure-reducing line for oil-transferring technology in the vacuum distillation apparatus; Its objective is under the condition that guarantees vacuum tower feed zone vaporization branch rate; Reduce the vacuum furnace outlet temperature as far as possible, to prevent tube coking.In other words, be under the heater outlet temperature of regulation, improve tower feed zone vaporization rate as far as possible, divide rate to improve product.For reaching this purpose, have only and reduce boiler tube and oil transfer line pressure drop as far as possible, make the oil product evaporation point in advance.Because oil transfer line must adopt 15m above (to guarantee that gas-liquid has certain separation time mutually; Help improving 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; 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 degree of difficulty to design and installation in security.
Summary of the invention
To the deficiency of prior art, the present invention provides a kind of vacuum distillation method and device, can obviously improve the extracting rate in the vacuum distillation process, reduces plant energy consumption, and reduces plant investment.
Vacuum distillation method of the present invention comprises: the cancellation pressure-reducing line for oil-transferring; Between vacuum furnace and vacuum distillation tower, flash column is set; The decompression distillation raw material gets into flash column through vacuum furnace heating back; In flash column, carry out gas-liquid separation, the liquid phase of discharging at the bottom of the flash column (dodging end oil to call in the following text) is introduced vacuum distillation tower, and the gas phase that the flash distillation cat head is discharged (dodging top gas to call in the following text) is condensed into after the liquid phase as product.
In the vacuum distillation method of the present invention, be condensed into the liquid phase ejector after dodging top gas and getting into vacuum furnace decompression distillation raw material heat exchange before, perhaps with a certain of vacuum distillation tower or a few kinds of cut mixing ejectors.The decompression distillation raw material is generally oil at the bottom of the air-distillation Tata (to call oil of the normal end in the following text).
In the vacuum distillation method of the present invention; Cancelled the setting of pressure-reducing line for oil-transferring in the conventional decompression distillation; Vertical flash column is set between vacuum furnace and vacuum tower, can compactly be provided with between flash column and vacuum furnace, the vacuum distillation tower, need not to consider to be provided with the oil transfer line setting that is not less than 15 meters.Vertical flash column is mainly used in gas-liquid separation, in the 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 the vacuum distillation method of the present invention, other technology contents is a technology contents well known to those skilled in the art like 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 the vacuum distillation tower; The vacuum furnace outlet directly connects flash column; The discharging of flash column bottom liquid phases is introduced vacuum distillation tower through pipeline, and the flash column top is communicated with pipeline with decompression distillation raw material heat-exchanger rig.
Vacuum distillation apparatus of the present invention can be provided with a cover pumped vacuum systems, and vacuum distillation tower and flash column can be provided with control device with a cover pumped vacuum systems vacuum pumping, control the vacuum of vacuum distillation tower and flash column respectively; 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 the top gas condenser knockout drum afterwards.The vacuum pumping of flash column and vacuum distillation tower can be adopted the conventional method and apparatus in this area.
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 of normal end oil heating-entering vacuum tower, greatly reduced the process pressure drop and the thermal loss of pressure-reducing line for oil-transferring in the 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) through 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.The cancellation 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, big pipe range oil transfer line low speed segment to be caused.Through adjusting, the cost of flash column is starkly lower than the cost of extra heavy pipe footpath, big pipe range oil transfer line.
4) dodge end oil and get into vacuum distillation tower separately, dodge top gas and do not get into vacuum distillation tower, significantly reduce the processing load of vacuum distillation tower, eliminated " bottleneck " of vacuum tower treating capacity, help the capacity expansion revamping of old device.
5) dodge end oil and get into vacuum distillation tower separately, reduced the required theoretical plate of vacuum tower to a certain extent, can suitably reduce tower height and tower diameter, the economy system investment.
6) dodge end oil and get into vacuum distillation tower separately, dodge top gas and do not get into vacuum distillation tower, reduced the gas phase load of vacuum distillation tower, full tower pressure drop is reduced, help improving the decompression extracting rate, and significantly reduced the decompression overhead 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 get into vacuum distillation tower separately, the gas phase of having avoided the gas-liquid mixed charging to be caused is carried secretly, has guaranteed depressurised side line products quality.
8) dodge top gas and carry out heat exchange, reduced the vacuum furnace load, reduce plant energy consumption with oil of the normal end.
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 advantages such as the scrap build amount is few, investment is low, and the transformation duration is short, and the device income is obviously quick; For the design and construction of new equipment, it is rationally advanced to have technology, and energy consumption level is low, and size investment is little, and equipment takes up an area of 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 heating and gasifying 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, again after cooler is cooled to full liquid phase, as the discharging of product liquid phase.Dodge end oil and directly get into the vacuum distillation tower feed zone, at the bottom of having tower, further carry out fractionation in the vacuum distillation tower of stripped vapor, extract vacuum distillate out from the vacuum distillation tower side line, decompression residuum is extracted cat head connection pumped vacuum systems out at the bottom of by tower.Cancel traditional oil transfer line, only use a small amount of common pipe.
Oil of the normal end gets into vacuum furnace earlier after charging/sudden strain of a muscle top gas heat exchanger heat exchange rising temperature; After temperature was heated to 390 ℃～400 ℃ in vacuum furnace, oil rate of gasification of the normal end reached 50%～60% (mass percent, down together); Get into vacuum flasher then; Gas-liquid is separated fully in vacuum flasher, and gas phase is discharged with oil of the normal end by tank deck through the broken foam demist net of tank deck and lowered the temperature in charging/sudden strain of a muscle top gas heat exchanger heat exchange, is cooled to full liquid phase as dodging top product discharging through dodging the top gas condenser again.Liquid phase is dodged end oil and is directly got into the vacuum distillation tower feed zone, under the effect of stripped vapor and decompression distillation cat head pumped vacuum systems, carries out decompression distillation, obtains sideline product and discharging in the tower.Decompression residuum is by the VACUUM TOWER BOTTOM discharging.Vacuum flasher and vacuum distillation tower have Level Detection to show respectively.
Vacuum distillation tower among the present invention can be the fuel type vacuum distillation tower, also can be lubricated oil type vacuum distillation tower; Can be wet distiller, wet distiller also can decline; Side line discharging number specifically is provided with as required.
The vacuum distillation method and the equipment that have flash column behind the vacuum furnace of the present invention; Improved the crude oil reduced pressure distillation process; Reach lower pressure heating and gasifying rate in vacuum furnace 50%～60% mixed feeding and in vacuum flasher, carry out gas-liquid separation; Need not establish long pressure-reducing line for oil-transferring low speed segment again 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, big pipe range low speed segment to be caused.Flash distillation cat head gas phase and vacuum furnace charging are carried out after heat exchange, the condensation directly as product, and liquid phase gets into vacuum distillation tower separately.Thereby reduced the processing load of vacuum distillation tower, reduced the required theoretical plate of vacuum distillation tower to a certain extent, can suitably reduce tower height and tower diameter, significantly reduced the condensation of decompression distillation cat head and vacuumized load simultaneously; And the gas phase that can avoid the gas-liquid mixed charging to be caused carries secretly, guaranteed depressurised side line products quality.Confirm through analog computation; Handle 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 cat head accounts for sensible heat that the oil gas of charging 50%～60% contains and latent heat and is enough to save the load of vacuum furnace to oil heat exchange to 390 of the normal end ℃～400 ℃ greatly.
When the present invention goes into operation at device, can open big vacuum furnace load, heating is fed to 390 ℃～400 ℃, guarantees the decompression distillation operation.Go into operation stable after, make full use of the sensible heat that high temperature dodges top gas and heat for oil of the normal end with latent heat, 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 crude oil atmospheric and vacuum distillation unit.
The treating capacity of decompression partial devices is 1,200,000 tons/year, and the decompression flow process comprises vacuum furnace, flash column, vacuum tower.Vacuum tower is a regular packed tower, adopts the wet process operation, and tower bottom blowing vapour amount is 1% of tower charging, and the cat head 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, after vacuum furnace is heated to 390 ℃～400 ℃, enters into vacuum flasher.The cancellation oil transfer line, flash column directly is connected with vacuum tower, and flash column pressure is 10kPa.Dodge top gas behind the adiabatic flash and account for 45.67% of charging, dodge end oil and get into vacuum tower, extract product out from the vacuum tower side line.Decompression residuum discharging at the bottom of the tower.Cat head oil gas cools off through condenser, and fixed gas is extracted out by vacuum pumping pump, keeps vacuum in the tower.
Following table has been listed employing the present invention (option A) and has been adopted and had the atmospheric vacuum distillation method of vacuum flasher and the patent CN101376068A of equipment (option b) carry out analog study at aspects such as decompression extracting rate, plant energy consumption, investments data contrast.
Option A and option b contrast situation
Visible from table, though use a heat exchanger in option A aspect the equipment investment, the vacuum tower tower diameter is less more, and investment reduces, and corresponding tower internals and filler investment also will reduce; And vavuum pump power is well below option b; Though the lower slightly and option A of option b vacuum furnace load aspect plant energy consumption at steam consumption, overhead condensation with vacuumize load and be 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 higher relatively.
Embodiment 2:
Method of the present invention is used for the capacity expansion revamping of certain crude oil atmospheric and vacuum distillation 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 a regular packed tower, and the cat head operating pressure is 1.315kPa, and full tower pressure drop is 600Pa～750Pa.
Oil of the normal end gets into vacuum distillation apparatus, after vacuum furnace is heated to 390 ℃～400 ℃, enters into vacuum flasher.The cancellation oil transfer line, flash column directly is connected with vacuum tower, and flash column pressure is 10kPa, dodges top gas behind the adiabatic flash and accounts for 45.67% of charging, dodges end oil and gets into vacuum tower 15, extracts product 10,11 out from the vacuum tower side line.Go out decompression residuum at the bottom of the 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.Transform back device decompression part working ability and can improve 20%～50%, 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 and had the atmospheric vacuum distillation method of vacuum flasher and the patent CN101376068A of equipment (option b) carry out analog study to certain atmospheric and vacuum distillation unit decompression part transformation situation data contrast.
Option A and option b comparable situation
Can find out that from table it is more less than the newly-built equipment of scheme B to adopt option A that old device is carried out capacity expansion revamping, engineering amount of reform is little, thereby construction investment is less, and it is short to transform the duration; Also obviously better on the device income.Option A has bigger rectification advantage.
Claims (7)
1. a vacuum distillation method 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 gets into flash column through vacuum furnace heating back; In flash column, carry out gas-liquid separation, the liquid phase of discharging at the bottom of the flash column is promptly dodged end oil and is introduced vacuum distillation tower; The gas phase that the flash distillation cat head is discharged is promptly dodged top gas and is condensed into after the liquid phase as product.
2. according to the described method of claim 1, it is characterized in that: be condensed into the liquid phase ejector after dodging top gas and getting into vacuum furnace decompression distillation raw material heat exchange before, perhaps with a certain of vacuum distillation tower or a few kinds of cut mixing ejectors.
3. according to the described method of claim 1, it is characterized in that: the decompression distillation raw material is an oil at the bottom of the air-distillation Tata.
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 the vacuum distillation tower, the vacuum furnace outlet directly connects flash column; The discharging of flash column bottom liquid phases is introduced vacuum distillation tower through pipeline, and the flash column top is communicated with pipeline with decompression distillation raw material heat-exchanger rig.
5. according to the described device of claim 4, it is characterized in that: flash column is used for gas-liquid separation, and column plate is set in the tower, perhaps is the void tower structure.
6. according to the described device of claim 4, it is characterized in that: vacuum distillation apparatus is provided with a cover pumped vacuum systems, the shared cover pumped vacuum systems vacuum pumping of vacuum distillation tower and flash column.
7. according to the described device of 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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| Application Number | Priority Date | Filing Date | Title |
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| CN 201010222356 CN102309863B (en) | 2010-07-07 | 2010-07-07 | Reduced pressure distillation method and device |
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| CN 201010222356 CN102309863B (en) | 2010-07-07 | 2010-07-07 | Reduced pressure distillation method and device |
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| CN102309863A true CN102309863A (en) | 2012-01-11 |
| CN102309863B CN102309863B (en) | 2013-11-06 |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103242896A (en) * | 2012-02-06 | 2013-08-14 | 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 |
| CN103242887A (en) * | 2012-02-06 | 2013-08-14 | 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 |
| CN103484145A (en) * | 2013-01-10 | 2014-01-01 | 盘锦兴达沥青有限公司 | Differential pressure distillation equipment and processing method |
| CN103540354A (en) * | 2012-07-09 | 2014-01-29 | 中国石油化工集团公司 | Combined heavy oil treatment process |
| CN103540357A (en) * | 2012-07-09 | 2014-01-29 | 中国石油化工集团公司 | Heavy oil treatment process |
| CN106590715A (en) * | 2017-01-23 | 2017-04-26 | 中冶焦耐(大连)工程技术有限公司 | Light oil and wide fraction separation technology and equipment applicable to 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 |
| US20020053531A1 (en) * | 2000-11-03 | 2002-05-09 | Kenneth Hucker | Process for reduction of emissions in asphalt production |
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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 |
| US20020053531A1 (en) * | 2000-11-03 | 2002-05-09 | Kenneth Hucker | Process for reduction of emissions in asphalt production |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103242896A (en) * | 2012-02-06 | 2013-08-14 | 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 |
| CN103242887A (en) * | 2012-02-06 | 2013-08-14 | 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 |
| 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 |
| CN103540354A (en) * | 2012-07-09 | 2014-01-29 | 中国石油化工集团公司 | Combined heavy oil treatment process |
| CN103540357A (en) * | 2012-07-09 | 2014-01-29 | 中国石油化工集团公司 | Heavy oil treatment process |
| 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 |
| CN103484145A (en) * | 2013-01-10 | 2014-01-01 | 盘锦兴达沥青有限公司 | Differential pressure distillation equipment and processing method |
| CN106590715A (en) * | 2017-01-23 | 2017-04-26 | 中冶焦耐(大连)工程技术有限公司 | Light oil and wide fraction separation technology and equipment applicable to tar distillation |
| 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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| Publication number | Publication date |
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| CN102309863B (en) | 2013-11-06 |
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