CN102911716A - Sectional feeding vacuum distillation method and apparatus for crude oil - Google Patents
Sectional feeding vacuum distillation method and apparatus for crude oil Download PDFInfo
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- CN102911716A CN102911716A CN201110217569XA CN201110217569A CN102911716A CN 102911716 A CN102911716 A CN 102911716A CN 201110217569X A CN201110217569X A CN 201110217569XA CN 201110217569 A CN201110217569 A CN 201110217569A CN 102911716 A CN102911716 A CN 102911716A
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Abstract
The invention discloses a sectional feeding vacuum distillation method and an apparatus for crude oil. The method comprises the steps of omitting relatively long transfer line from the outlet of a vacuum furnace to the vacuum tower; arranging a flashing tower between the vacuum tower and a vacuum distillation tower; passing superheated steam through the bottom of the flashing tower; introducing the raw materials of vacuum distillation to the flashing tower through the vacuum furnace after being heated; educing relative light components (hereinafter referred to flashing top gas) in the flashing tower from the tower top after steam stripping evaporation; entering below a packing layer of some fractioning section of the vacuum distillation tower; and introducing the liquid phase (hereinafter referred to flashing bottom oil) educed from the bottom of the flashing tower to the feeding section of the vacuum distillation tower to perform vacuum distillation. The sectional feeding vacuum distillation method and the apparatus for the crude oil can obviously increase pull-out rate of the vacuum distillation process and improve the quality of the vacuum distillates.
Description
Technical field
The invention belongs to the refining of petroleum field, relate in particular to a kind of crude oil vacuum distillation method of sectional feeding.
Technical background
Refinery crude oil atmospheric vacuum distillation technique is the first operation of refining of petroleum, is that the method by distillation is divided into the component of different boiling range scopes with crude oil, to adapt to product and downstream unit to the processing requirement of raw material.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.
In recent years, the demand of China's oil fuel is along with the development of national economy presents continuous growing trend.Many existing 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; And have many atmospheric and vacuum distillation unit to obtain higher cut point, but the quality product of the bottom side of underpressure distillation line does not often satisfy the secondary processing device to the index request of raw material, mostly bottom side line products is sneaked into again among the vacuum residuum.And replaced gradually high speed transfer line in the past with major diameter (general diameter can reach more than the 2m) low speed pressure-reducing line for oil-transferring technology in the existing vacuum distillation apparatus, its objective is under the condition that guarantees vacuum still feed zone vaporization minute rate, reduce as far as possible the vacuum furnace temperature out, 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 transfer line pressure drop, make the oil product evaporating point in advance.15m is above (to have certain separation time to guarantee liquid phase because transfer line must adopt, be conducive to improve the quality of products and the vacuum still extracting rate), therefore the transfer line of the long distance of major diameter accounts for the larger proportion of vacuum distillation apparatus investment, the factors such as calorific loss and pressure drop increase all are unfavorable for the operation of vacuum still simultaneously, and the thermal stresses, the thermal walking that form cause larger difficulty to design and installation in security.
For this reason, vast oil refining worker conducts in-depth research for decompression deep drawing, capacity expansion revamping, quality product, the pressure-reducing line for oil-transferring optimization design of Atmospheric Vacuum Unit, has made significant headway.CN1287872A discloses a kind of crude oil atmospheric vacuum distillation method with degree of depth stripping process, at vacuum still side washing tank in parallel, the feed zone of vacuum still 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 still 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 still is returned in the tank deck oil gas discharging of washing tank, and discharging is returned vacuum still as washing oil at the bottom of the tank.This technique makes the vacuum still 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, improves the sideline product quality.But the method just is optimized improvement to the vacuum still stripping stage, subtracts preferably third fractional oil as washing oil with quality, waits research in economic benefit.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 distillation tower, because the temperature of oil is relatively low at the bottom of the atmospheric distillation tower, the vacuum tightness of adding the stokehold flashing tower is relatively not high, and the effect of flashing tower flash distillation gasification is limited.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of crude oil vacuum distillation method and device of sectional feeding, can obviously improve the extracting rate in the vacuum distillation process, improve the reduced pressure distillate oil quality.
The crude oil vacuum distillation method of sectional feeding of the present invention comprises following content: the cancellation vacuum furnace exports to the transfer line between the vacuum distillation tower, between vacuum furnace and vacuum still flashing tower is set, and passes into superheated vapour at the bottom of the flash distillation Tata; The underpressure distillation raw material is introduced flashing tower after heating through vacuum furnace, and component relatively light in flashing tower is drawn (hereinafter referred to as dodging top gas) by cat head after the stripping vaporization, dodge the below that top gas enters vacuum still distillation stage filling batch; The liquid phase of discharging at the bottom of the flashing tower (hereinafter referred to as dodging end oil) is introduced the vacuum still feed zone, carries out underpressure distillation.Vacuum still arranges the quantity of side line extraction product as required, is generally 2 ~ 4 side line extraction products can be set in the situation, obtains vacuum 1st side cut distillate, Light lube oil, subtracts three line distillates and subtracts four line distillates.
In the crude oil vacuum distillation method of sectional feeding of the present invention, dodge that top gas enters that certain sideline product of the vacuum still close with dodging the top gas cut extracts out mouthful above or below, be generally that vacuum 1st side cut distillate or Light lube oil extract out mouthful above or below.The underpressure distillation raw material is generally oil at the bottom of the air distillation Tata (hereinafter referred to as oil of the normal end).
In the crude oil vacuum distillation method of invention sectional feeding, establish 6 ~ 12 blocks of column plates in the flashing tower, vapor flow of stripper is 0.1% ~ 1% of underpressure distillation charging quality at the bottom of the tower.The temperature that enters the superheated vapour of flashing tower preferably is higher than and enters 5 ~ 20 ℃ of flashing tower temperature of charge.Dodge top gas and account for 30% ~ 60% of oil quality of the normal end.
The crude oil vacuum distillation apparatus of sectional feeding of the present invention comprises vacuum furnace, vacuum flasher and vacuum still, cancel transfer line between vacuum furnace and the vacuum still, the vacuum furnace outlet directly connects flashing tower, the discharging of flashing tower bottom liquid phases is introduced the vacuum still feed zone by pipeline, and vacuum still distillation stage filling batch below is introduced by pipeline in the flashing tower top.
The present invention improves in the vacuum distillation method of extracting rate, and other technology contents is such as vacuum furnace, vacuum still, to vacuumize be technology contents well known to those skilled in the art.
Compared with prior art, the present invention has the following advantages:
1) cancelled pressure-reducing line for oil-transferring, the horizontal thermal walking of transfer line of having avoided extra heavy pipe footpath, large pipe range transfer line low speed segment to cause, the investment that greatly reduces (the flashing tower investment of setting is far below pressure-reducing line for oil-transferring).
2) behind the vacuum furnace flashing tower is set, dodges top gas and enter vacuum still middle and upper part pressure lower position, so that the working pressure of flashing tower is lower, service temperature is higher, and the gas phase amount that flashes off increases greatly.So that the pressure decreased in the vacuum furnace is conducive to improve the outlet of still vaporization rate, reduce the vacuum furnace load simultaneously.
3) dodge end oil and dodge the top gas segmentation and enter vacuum still, the gas phase entrainment of having avoided the gas-liquid mixed charging to cause, thus improved the bottom side of tower line products quality.
4) segmentation enters vacuum still with the sudden strain of a muscle top gas to dodge end oil, has reduced the process pressure drop of tower feed distributor, makes tower flash zone oil gas dividing potential drop lower, has strengthened the effect of tower flash zone and stripping stage, is conducive to improve extracting rate.
5) dodge the middle and upper part that top gas enters vacuum still, reduced the gas-liquid load of vacuum still bottom, improved the processing power of tower, be conducive to the capacity expansion revamping of old device.
6) dodge top gas and enter vacuum still and carry out fractionation, eliminated and dodged top gas to the carrying secretly of drop, guaranteed to extract the quality of distillate.
7) Technology of the present invention is rationally advanced, and energy consumption level is low, and the vacuum residuum yield is low, and the reduced pressure distillate oil quality is good, for the transformation of old device, has that the scrap build amount is few, investment is low, and it is short to transform the duration, and the device income is the advantage such as quick obviously; For the design and construction of new device, it is rationally advanced to have technique, and energy consumption level is low, and equipment takes up an area the characteristics such as few.
Description of drawings
Fig. 1 is crude oil vacuum distillation method and the device technique schematic flow sheet of sectional feeding.
Wherein 1 is oil of the normal end; 2 is vacuum furnace; 3 is vacuum still; 4 is vacuum flasher; 5 for dodging top gas; 6 is the flashing tower stripped vapor; 7 is the vacuum still stripped vapor; 8 is the vacuum residuum discharging; 9 is pumped vacuum systems; 10 is vacuum 1st side cut distillate product; 11 is the Light lube oil product; 12 for dodging end oil.
Embodiment
The inventive method connects a flashing tower in the vacuum furnace outlet, so that the gas-liquid flash separation is carried out in the very high gas-liquid mixed charging of vaporization rate under the condition of flashing tower condition of high vacuum degree after the vacuum furnace heating.Dodge the below that top gas is introduced vacuum still middle and upper part distillation stage filling batch; Dodge end oil and directly enter the vacuum still feed zone, further carry out fractionation in the vacuum still of stripped vapor at the bottom of with tower, from vacuum still lateral line withdrawal function vacuum distillate, vacuum residuum is extracted out at the bottom of by tower, and cat head connects pumped vacuum systems.
As shown in Figure 1, oil of the normal end 1 enters vacuum furnace 2, temperature enters vacuum flasher 4 after being heated to 390 ℃～420 ℃ in vacuum furnace, and under 6 effects of vacuum flasher stripped vapor, component relatively light in the oil of the normal end out enters the vacuum still middle and upper part as dodging top gas by flash overhead.Liquid phase is dodged end oil 12 and is directly entered vacuum still 3 feed zones, carries out underpressure distillation under the effect of stripped vapor 7 and underpressure distillation cat head pumped vacuum systems 9, obtains vacuum 1st side cut distillate product 10 and Light lube oil product 11 in the tower.Vacuum residuum 8 is by the VACUUM TOWER BOTTOM discharging.Vacuum flasher 4 and vacuum still 3 have respectively Level Detection to show.
Vacuum still among 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.
Crude oil vacuum distillation method and the device of sectional feeding of the present invention, improved the crude oil reduced pressure distillation process, containing 45%～55%(quality behind the vacuum furnace heating and gasifying) parallel feeding of gas phase carries out gas-liquid separation and stripping flash distillation 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 transfer line low speed segment length), the horizontal thermal walking of transfer line of having avoided extra heavy pipe footpath, large pipe range low speed segment to cause.The flash distillation top gaseous phase enters the vacuum still middle and upper part, can further eliminate the liquid phase of dodging top gas and carry secretly, from the up-to-standard product of vacuum still lateral line withdrawal function.Liquid phase enters the vacuum still feed zone at the bottom of the flashing tower, and the Vapor Entrainment of avoiding the gas-liquid mixed charging to cause has guaranteed depressurised side line products quality.Confirm through analog calculation, process the few 2%～5%(quality of residual oil yield of the existing operational path of identical raw material processing method of the present invention), underpressure distillation Tata diameter can reduce 20% ~ 40%.
Embodiment 1:
Method of the present invention is used for the design of certain newly-built Atmospheric Vacuum Unit, and relief portion division technique flow process is with identical shown in the accompanying drawing 1.
The treatment capacity of reliever is 550 tons/hour, and the decompression flow process comprises vacuum furnace, flashing tower, vacuum distillation tower.Vacuum distillation tower is regular packed tower, adopts the wet process operation, and tower bottom blowing vapour amount is 1% of tower charging quality, and the cat head working pressure is 1.315 kPa, and full tower pressure drop is 600 Pa～750Pa.
Oil 1 of the normal end is fed into vacuum distillation apparatus with 550 tons/hour, enters into vacuum flasher 4 after vacuum furnace 2 is heated to 390 ℃～420 ℃.The flashing tower cat head dodges top gas and directly enters the vacuum distillation tower middle and upper part, dodge end oil at the bottom of the flash distillation Tata and enter vacuum distillation tower 3 flash zones, from vacuum distillation tower lateral line withdrawal function reduced pressure distillate oil production 10,11, extract vacuum residuum at the bottom of the tower out, vacuum residuum is the 35.29%(quality to the yield of combined feed total feed), the cut point of decompressed wax oil reaches 583 ℃.Same feedstock, processing condition are calculated with the described method of CN101376068A, and vacuum residuum is the 37.64%(quality to the yield of combined feed total feed), the decompressed wax oil cut point is 565 ℃, 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 crude oil vacuum distillation method and the device technique schematic flow sheet of the sectional feeding shown in the accompanying drawing 1, mainly comprises vacuum furnace, flashing tower, vacuum distillation tower.Vacuum distillation tower is regular packed tower, and the cat head working pressure is 1.315 kPa, and full tower pressure drop is 600 Pa～750Pa.
Oil of the normal end 1 enters vacuum distillation apparatus, enters into vacuum flasher 4 after vacuum furnace 2 is heated to 390 ℃～420 ℃.The flashing tower cat head dodges top gas and directly enters the vacuum distillation tower middle and upper part, dodge end oil at the bottom of the flash distillation Tata and enter vacuum distillation tower 3 flash zones, from vacuum distillation tower lateral line withdrawal function reduced pressure distillate oil production 10,11, extract vacuum residuum at the bottom of the tower out, vacuum residuum is the 35.29%(quality to the yield of combined feed total feed), the cut point of decompressed wax oil reaches 583 ℃.
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.Remove transfer line, newly-increased main equipment is vacuum flasher.Device decompression part working ability can improve 20%～50%(quality after transforming), plant energy consumption reduces by 3%～5%, the vacuum residuum yield reduces by 2%～5%(quality).Calculate by 1,000 ten thousand ton/years of atmospheric and vacuum distillation unit, relief portion divides charging to be about 550 tons/hour, reduces residual oil yield 2%(quality), come in 250 yuan/tons of residual oil and mixed gatch price differences, year amount to Renminbi: 550 * 2% * 250 * 840,0=2,310 ten thousand yuan.Add the part of device reduction energy consumption, the device economic benefit highly significant of obtaining.
Claims (8)
1. the crude oil vacuum distillation method of a sectional feeding is characterized in that: the cancellation vacuum furnace exports to the transfer line between the vacuum distillation tower, between vacuum furnace and vacuum still flashing tower is set, and passes into superheated vapour at the bottom of the flash distillation Tata; The underpressure distillation raw material is introduced flashing tower through after the vacuum furnace heating, and relatively light component is drawn by cat head after the stripping vaporization and namely dodged top gas in flashing tower, dodges the below that top gas enters vacuum still distillation stage filling batch; The liquid phase of discharging at the bottom of the flashing tower is namely dodged end oil, dodges end oil and introduces the vacuum still feed zone, carries out underpressure distillation.
2. it is characterized in that in accordance with the method for claim 1: vacuum still arranges 2 ~ 4 side line extraction products.
3. according to claim 1 or 2 described methods, it is characterized in that: above or below dodging that top gas enters that certain sideline product of the vacuum still close with dodging the top gas cut extracts out mouthful.
4. it is characterized in that in accordance with the method for claim 3: above or below dodging that top gas enters that vacuum 1st side cut distillate or Light lube oil extract out mouthful.
5. it is characterized in that in accordance with the method for claim 1: establish 6 ~ 12 blocks of column plates in the flashing tower.
6. according to claim 1 or 5 described methods, it is characterized in that: vapor flow of stripper is 0.1% ~ 1% of underpressure distillation charging quality at the bottom of the tower.
7. it is characterized in that in accordance with the method for claim 6: dodge top gas and account for 30% ~ 60% of oil quality of the normal end.
8. the crude oil vacuum distillation apparatus of a sectional feeding, comprise vacuum furnace, vacuum flasher and vacuum still, it is characterized in that: cancel transfer line between vacuum furnace and the vacuum still, the vacuum furnace outlet directly connects flashing tower, the discharging of flashing tower bottom liquid phases is introduced the vacuum still feed zone by pipeline, and vacuum still distillation stage filling batch below is introduced by pipeline in the flashing tower top.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201110217569XA CN102911716A (en) | 2011-08-01 | 2011-08-01 | Sectional feeding vacuum distillation method and apparatus for crude oil |
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| CN201110217569XA CN102911716A (en) | 2011-08-01 | 2011-08-01 | Sectional feeding vacuum distillation method and apparatus for crude oil |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108211406A (en) * | 2018-03-20 | 2018-06-29 | 刘彦昌 | A kind of vacuum distillation equipment for waste lubricating oil pretreatment |
| CN114836234A (en) * | 2021-02-02 | 2022-08-02 | 中国石油化工股份有限公司 | Gasoline fractionating tower and application thereof |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| CN101717658A (en) * | 2009-12-03 | 2010-06-02 | 中国石油天然气集团公司 | Multi-vaporization feeding method of oil product fractionator |
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2011
- 2011-08-01 CN CN201110217569XA patent/CN102911716A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| CN101717658A (en) * | 2009-12-03 | 2010-06-02 | 中国石油天然气集团公司 | Multi-vaporization feeding method of oil product fractionator |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108211406A (en) * | 2018-03-20 | 2018-06-29 | 刘彦昌 | A kind of vacuum distillation equipment for waste lubricating oil pretreatment |
| CN114836234A (en) * | 2021-02-02 | 2022-08-02 | 中国石油化工股份有限公司 | Gasoline fractionating tower and application thereof |
| WO2022166751A1 (en) * | 2021-02-02 | 2022-08-11 | 中国石油化工股份有限公司 | Fractionating column |
| CN114836234B (en) * | 2021-02-02 | 2023-01-03 | 中国石油化工股份有限公司 | Gasoline fractionating tower and application thereof |
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Application publication date: 20130206 |