CN106318435A - Normal pressure distillation method - Google Patents
Normal pressure distillation method Download PDFInfo
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- CN106318435A CN106318435A CN201510338571.0A CN201510338571A CN106318435A CN 106318435 A CN106318435 A CN 106318435A CN 201510338571 A CN201510338571 A CN 201510338571A CN 106318435 A CN106318435 A CN 106318435A
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Abstract
The invention discloses a normal pressure distillation method. The method comprises the following steps: raw oil is heated in a heating furnace, the heated raw oil enters a normal pressure tower provided with a plurality of lateral lines, products are extracted from the lateral lines, the products respectively enter a normal pressure stripping tower and are in contact with non-condensable gas to carry out stripping, a liquid phase product obtained after the stripping is discharged from the normal pressure stripping tower, and a gas phase obtained after the stripping is mixed with oil gas at the top of the normal pressure tower; and the non-condensable gas enters the bottom of the normal pressure tower and is used to carry out stripping on normal pressure bottom oil, the stripped normal pressure bottom oil is discharged from the normal pressure tower, and the obtained stripped gas phase is mixed with oil gas in the normal pressure tower. The method has the advantages of reduction of the use amount of steam, reduction of the discharge amount of sewage, reduction of the condensation cooling load of the tower top, and reduction of the energy consumptions of above devices.
Description
Technical field
The invention belongs to petroleum refining field, relate in particular to a kind of crude oil processing method, more specifically one
Plant the air-distillation method reducing energy consumption.
Background technology
Crude oil atmospheric vacuum distillation technique is the first operation of petroleum refining, is that the method by distillation is by crude oil
It is divided into the component of different boiling range scope, to adapt to product and the downstream unit technological requirement to raw material.Conventional
The many employings of crude oil atmospheric vacuum distillation skill " three towers " flow process: crude oil enters primary distillation tower (or flash distillation after heat exchange
Tower), then enter atmospheric distillation tower through atmospheric pressure kiln heating, atmospheric distillation tower base oil is heated through subtracting by vacuum furnace
Pressure oil transfer line delivers to vacuum distillation tower, completes the air-distillation to crude oil and decompression distillation, it is thus achieved that meet quality
The product required and the raw material of downstream unit.
In recent years, world petroleum demand amount increases year by year with the development of World Economics.World's crude resources supply
Middle heavy oil and overweight oil supplying ratio are stepped up, and light oil, middle matter oil supplying constant decline.
Therefore, improve the light oil extracting rate in crude oil atmospheric vacuum distillation, reduce atmospheric and vacuum distillation unit energy consumption, improve device
Economic benefit becomes the problem that whole world Refining Chemical Industry is paid close attention to jointly.And along with quickly sending out of Chinese national economy
Exhibition, China's oil total quantity consumed is at the year two thousand twenty by breakthrough 6.5 hundred million tons, and the external dependence degree of crude oil is up to
50%～60%, Appropriate application crude resources, optimization processing technology has been the act that China's oil chemical industry is imperative.
In the novel refinery of larger-scale unit and Integrated Refinery And Petrochemical designs, as the crude oil atmospheric vacuum distillation of " leading "
Device maximum resource utilization, utilization of energy economized, running cost rationalize, size investment optimization,
There is in the sustainable development realizing China's oil chemical industry very important status.
Therefore, newly-built CDU requires higher depth of cut, in decompression residuum538℃Hereinafter evaporate
Dividing content to be less than 5 mass %, even lower, many old atmospheric and vacuum distillation units are requiring higher cut point
Meanwhile, face and the situation that treating capacity requires and oil variety is continually changing under process scale, can not be met, need
Device is carried out capacity expansion revamping, eliminates " bottleneck ", improve crude capacity.
To this end, Chinese scholars to the deep vacuum distillation of Atmospheric Vacuum Unit, can lower consumption, reduce invest into
Go and compared in-depth study, made significant headway.Developing direction is concentrated mainly on the following aspects:
Optimize vacuum system, improve the vacuum of vacuum fractionation tower top；Use novel, high efficiency packing and straight
Connect contact heat transfer type, reduce tower overall presure drop, keep higher flash zone vacuum；Improvement oil transfer line sets
Meter, reduces oil transfer line pressure drop and temperature drop；Optimize washing section design and operation, the fractional distillation concept of strengthening washing section；
Develop new and effective gas and liquid distribution trough；Use strengthening crude distillation method etc..
Patent US7172686 has delivered a kind of method improving crude distillation distillate yield, method one be from
Tower inside cord extracts gaseous stream out, carries out isolated product, and a part of gas phase returns in tower；Method two is
Incoming mixture is separated into light fraction, midbarrel, heavy distillat, the most respectively not by boiling point height heating
Same feed entrance point carries out fractional distillation in entering tower, extracts light, heavy distillat successively out from side line.Method one is equivalent to
Side line has added a stripper.Improve distillate quality.But to a certain degree add plant investment and energy consumption；
Method two achieves gently, heavy distillat sectional feeding, improves the operation of crude distillation fractionating column, is conducive to carrying
High distillate yield, but carry out in the light fraction separated from mixed feeding is fed again into tower point
Evaporating, 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 at the bottom of tower
Seal apparatus separates with top, and has a vacuum system interface to be connected with top vacuum system.This utility model
By liquid seal device, the rectifying section of vacuum distillation tower and the deep drawing section of bottom are separated, can be by oil quality
Pay attention to respectively with extracting rate, can relatively improve decompression extracting rate, but the oil quality of deep drawing is difficult to
Meeting the downstream unit technological requirement to raw material, the tower structure of this utility model is complicated simultaneously, top vacuum system
System load is high, and plant energy consumption relatively can be high.
Patent CN1884441A discloses the method improving light oil yield of atmospheric and vacuum distillation of petroleum oil, by containing Colophonium
Additive is added in the crude oil of atmospheric and vacuum distillation of petroleum tower, improves by changing the intermolecular active force of crude oil
The light oil yield of atmospheric and vacuum distillation.But the method does not fundamentally change distillation technique in Technology, and
Consume substantial amounts of additive, add plant running cost and add the operation easier of chemical reagent.
Patent US4717468 has delivered a kind of distillation technique utilizing minimum energy consumption to obtain maximum recovery,
It is by being mixed into noble gas in charging, thus when amplitude peak ground reduces charging stop in heating furnace
Between and dividing potential drop, by maintaining the certain rate of gasification of crossing of charging to optimize furnace outlet temperature, keep minimum
Furnace outlet temperature, thus reduce energy consumption.The method can on the premise of avoiding oil product cracking the most significantly
Degree ground adds hot feed, and reduces its dividing potential drop, improves feeding gas rate, is conducive to improving extracting rate, but injects
Noble gas adds overhead condensation and the load of pumped vacuum systems and plant running cost is offset it and reduced heating
Capacity of furnace consumes, 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, is
A washing tank in parallel in vacuum distillation tower side, the feed zone of vacuum distillation tower is isolated by fluid-tight with stripping section
Distributor separates, and the oil gas of stripping section enters the bottom of washing tank by communicating pipe, takes from vacuum distillation tower and subtracts
The oil that absorbs of three line dischargings is entered spray and the reverse mass transfer of oil gas upwards downwards by washing tank top after cooling
Heat transfer, the tank deck oil gas discharging of washing tank returns to the top of vacuum distillation tower, and tank bottoms discharging is returned as washing oil
Return vacuum distillation tower.This technique makes vacuum distillation tower stripping section experienced by a degree of depth vapour by setting up washing tank
The process carried, is conducive to improving decompression extracting rate.But vacuum distillation tower stripping section is simply carried out by the method
Optimal improvements, preferably subtracts third fractional oil oily as washing by quality, waits research in economic benefit.
Patent CN101376068A discloses a kind of atmospheric vacuum distillation method with vacuum flasher and equipment,
It is that a vacuum flasher is set before reduced crude enters vacuum furnace.Flash column base oil enters heating under reduced pressure stove, dodges
Steam tower overhead gas to enter above or below certain sideline product outlet port close with flash column top gas fraction.Should
Method improves the flow process of atmospheric and vacuum distillation unit by increasing vacuum flasher, reaches to improve treating capacity, and raising is extracted
Rate, reduces the purpose of energy consumption.But atmospheric distillation tower base oil enters flash column, due to the temperature of atmospheric distillation tower base oil
Spending relatively low, the vacuum adding stokehold flash column is relatively the highest, and the flash vaporized effect of flash column has
Limit, and flash distillation top gaseous phase enters vacuum distillation tower, is equivalent to vacuum distillation tower sectional feeding after flash distillation, does not has
Have in the fractionation fundamentally changing vacuum distillation tower.
In prior art, atmospheric tower bottom blowing enters superheated steam, to reduce 350 DEG C of components in the past in normal base oil,
Advantage is provided for deep vacuum distillation.Typically it is blown into 1～2 weight % that quantity of steam is reduced crude.It addition,
Stripped vapor the most often it is blown into, in order to meet the requirement to flash-point in product quality at the bottom of atmospheric side draw stripper tower.
These are used as steam stripped steam, finally rise to Atmospheric Tower in tower, after heat exchange, condensation cooling
Becoming oil-containing sour water send sewage stripping device to process.The stripped vapor needed exist for adds device
Energy consumption, the sewage of generation further adds energy consumption, and the condensation cooling of this part water vapour of tower top adds
Circulation water consumption, and add the scale of downstream wastewater processing means.Obviously, if stripped vapor can be eliminated,
The most just decrease sewage discharge simultaneously, reduce energy consumption.
Summary of the invention
The present invention provides a kind of air-distillation method, overcomes in prior art at the bottom of atmospheric tower and atmospheric side draw stripping
Tower bottom blowing enters material consumption, the energy consumption height that stripped vapor brings, overhead condensation cooling load increase, many lacking of sewage
Point.
A kind of air-distillation method, the heated stove of raw oil enters atmospheric tower after heating up, and atmospheric tower is provided with multiple
Side line extraction product, each product respectively enters atmospheric stripping tower and contacts with fixed gas and strip, after stripping
Liquid-phase product goes out device, the gas phase after stripping and the air-fuel mixture of atmospheric tower tower top；Fixed gas enters at the bottom of atmospheric tower
Stripping atmospheric tower base oil, after stripping, atmospheric tower base oil goes out device, the gas phase after stripping and atmospheric tower tower
Interior air-fuel mixture.
Described fixed gas is the non-congealable oil gas of oil industry, consisting of: C1～C6Organic substance, nitrogen,
The components, preferably C such as hydrogen, oxygen, carbon dioxide, hydrogen sulfide, a small amount of empty gas and water1～C3Organic substance,
C1～C2Organic substance, fixed gas accounts for 0.5～4.0 weight % being for reduced crude, preferably 1～2 weight %
Described fixed gas is at least from this device, other devices and the one of synergic system.
Compared with prior art, one air-distillation method of the present invention has the advantage that
1 reduces atmospheric and vacuum distillation unit steam consumption.
2 reduce atmospheric and vacuum distillation unit quantity of wastewater effluent.
3 reduce overhead condensation cooling load.
4 reduce plant energy consumption.
Accompanying drawing explanation
Fig. 1 is one vacuum distillation method schematic flow sheet of the present invention
Wherein: 1. atmospheric tower, 2. atmospheric stripping tower, 3. tower tray, 4 often push up one-level knockout drum, 5. often push up two
Level knockout drum, 6. tower top fixed gas, 7. atmospheric tower charging, 8. atmospheric stripping tower fixed gas, the 9. normal end
Oil, 10. atmospheric tower base oil stripping fixed gas.
In order to describe the present invention in detail, by embodiment, one vacuum distillation method of the present invention is illustrated below,
But it does not limit the scope of the invention.
Embodiment 1 (prior art)
Atmospheric distillation tower treating capacity is 874330kg/h, and raw material is first base oil, and obtaining reduced crude is 560850
Kg/h, stripped vapor used by atmospheric distillation tower product stripping section is 700kg/h, strips atmospheric tower sideline product,
Stripped vapor 7000kg/h used by reduced crude stripper, tower top total amount of heat 681 × 104KCal/h, tower top is arranged
Put sewage quantity 7700kg/h.
Embodiment 2 (present invention)
Atmospheric distillation tower treating capacity is 874330kg/h, and raw material is first base oil, and obtaining reduced crude is 560850
Kg/h, atmospheric distillation tower product stripping section utilizes fixed gas to strip, and fixed gas used is system dry gas,
It mainly comprises as C1、C2Gas, tolerance is 700kg/h, reduced crude stripping fixed gas 7000kg/h used,
Account for 1.25 weight % of reduced crude, tower top total amount of heat 355 × 104kCal/h.Fixed gas used is system
Dry gas (mainly comprises as C1～C2), the present invention relatively shows device and saves 0.3MPa steam 7700kg/h, tower top
Reduce sewage effluent 7700kg/h.Tower top dry gas all recycles.Only steam one can save fund every year
7700000 yuans.
Embodiment 3 (present invention)
Atmospheric distillation tower treating capacity is 874330kg/h, and raw material is first base oil, and obtaining reduced crude is 560850
Kg/h, atmospheric distillation tower product stripping section utilizes fixed gas to strip, and fixed gas used is system dry gas,
It mainly comprises as C1、C2Gas, tolerance is 8200kg/h, fixed gas 910 used by reduced crude stripper
Kg/h, accounts for 1.62 weight % of reduced crude, tower top total amount of heat 415 × 104kCal/h.Fixed gas used
(mainly comprise as C for often pushing up fixed gas1～C4Light hydrocarbon component), tower top fixed gas recycles.The present invention is relatively
Existing device saves 0.3MPa steam 7700kg/h, and tower top reduces sewage effluent 7700kg/h.Only steam one
Item can save fund 7,700,000 yuans every year.Annual about 1,110,000 yuan of aerator power consumption needed for circulation fixed gas
RMB, while it is true, still can save fund about 6,590,000 yuans every year.
Claims (7)
1. an air-distillation method, the heated stove of raw oil enters atmospheric tower after heating up, and atmospheric tower is provided with multiple side
Line extraction product, each product respectively enters atmospheric stripping tower and contacts with fixed gas and strip, the liquid after stripping
Phase product goes out device, the gas phase after stripping and the air-fuel mixture of atmospheric tower tower top；Fixed gas enters at the bottom of atmospheric tower pair
Atmospheric tower base oil strips, and after stripping, atmospheric tower base oil goes out device, in the gas phase after stripping and atmospheric tower tower
Air-fuel mixture.
2. according to a kind of air-distillation method described in claim 1, it is characterised in that: described fixed gas is stone
The non-congealable oil gas of oiling industry, consisting of: C1～C6Organic substance, nitrogen, hydrogen, oxygen, titanium dioxide
The components such as carbon, hydrogen sulfide, a small amount of empty gas and water.
3. according to a kind of air-distillation method described in claim 1, it is characterised in that: described fixed gas composition
For: C1～C3Organic substance.
4. according to a kind of air-distillation method described in claim 1, it is characterised in that: described fixed gas composition
For: C1～C2Organic substance.
5. according to a kind of air-distillation method described in claim 1, it is characterised in that: described fixed gas account for into
0.5～4.0 weight % of reduced crude.
6. according to a kind of air-distillation method described in claim 1, it is characterised in that: described fixed gas account for into
1～2 weight % of reduced crude
7. according to a kind of air-distillation method described in claim 1, it is characterised in that: described fixed gas is at least
For from this device, other devices and the one of synergic system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510338571.0A CN106318435A (en) | 2015-06-18 | 2015-06-18 | Normal pressure distillation method |
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| CN201510338571.0A CN106318435A (en) | 2015-06-18 | 2015-06-18 | Normal pressure distillation method |
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| CN106318435A true CN106318435A (en) | 2017-01-11 |
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| CN201510338571.0A Pending CN106318435A (en) | 2015-06-18 | 2015-06-18 | Normal pressure distillation method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107699273A (en) * | 2017-11-15 | 2018-02-16 | 中国石油大学(北京) | A kind of anhydrous atmospheric and vacuum distillation technique and device |
| CN109628133A (en) * | 2018-12-12 | 2019-04-16 | 中石化炼化工程（集团）股份有限公司 | A kind of atmospheric distillation of reduction often top cooling system corrosion |
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| WO2011091206A2 (en) * | 2010-01-21 | 2011-07-28 | Shell Oil Company | Hydrocarbon composition |
| CN102443407A (en) * | 2010-10-13 | 2012-05-09 | 中国石油化工股份有限公司 | Crude oil deep drawing process method |
| CN103242885A (en) * | 2012-02-06 | 2013-08-14 | 中国石油化工股份有限公司 | Flash-strengthened crude oil reduced pressure deep distillation process |
| CN104611005A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Process method for increasing coking diesel fuel yield |
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2015
- 2015-06-18 CN CN201510338571.0A patent/CN106318435A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011091206A2 (en) * | 2010-01-21 | 2011-07-28 | Shell Oil Company | Hydrocarbon composition |
| CN102443407A (en) * | 2010-10-13 | 2012-05-09 | 中国石油化工股份有限公司 | Crude oil deep drawing process method |
| CN103242885A (en) * | 2012-02-06 | 2013-08-14 | 中国石油化工股份有限公司 | Flash-strengthened crude oil reduced pressure deep distillation process |
| CN104611005A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Process method for increasing coking diesel fuel yield |
Non-Patent Citations (1)
| Title |
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| 林世雄: "《石油炼制工程》", 31 July 2000 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107699273A (en) * | 2017-11-15 | 2018-02-16 | 中国石油大学(北京) | A kind of anhydrous atmospheric and vacuum distillation technique and device |
| CN109628133A (en) * | 2018-12-12 | 2019-04-16 | 中石化炼化工程（集团）股份有限公司 | A kind of atmospheric distillation of reduction often top cooling system corrosion |
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Application publication date: 20170111 |