CN107699273B - A kind of anhydrous atmospheric and vacuum distillation technique and device - Google Patents
A kind of anhydrous atmospheric and vacuum distillation technique and device Download PDFInfo
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- CN107699273B CN107699273B CN201711129325.XA CN201711129325A CN107699273B CN 107699273 B CN107699273 B CN 107699273B CN 201711129325 A CN201711129325 A CN 201711129325A CN 107699273 B CN107699273 B CN 107699273B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/06—Vacuum distillation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/12—Controlling or regulating
Abstract
The present invention provides a kind of anhydrous atmospheric and vacuum distillation technique and devices.The technique includes: atmospheric tower and vacuum tower by the way of four vaporization feedings, crude oil is fed after normal pressure stove heating from atmospheric tower tower reactor, tower reactor is not passed through water vapour, and each sideline product is heated using reboiler, and normal pressure column overhead carries out alkali cleaning through tower top dry gas of the condensation after cooling；Vacuum flasher is added between atmospheric tower and vacuum furnace, the atmospheric residue come out from atmospheric tower tower reactor enters vacuum flasher；Several side lines are arranged to extract product out in vacuum flasher, and the product of the first lateral line withdrawal function is recycled into atmospheric tower, and tower reactor heavy oil, which enters, enters vacuum tower after vacuum furnace further heats；The pressure of vacuum flasher controls between atmospheric tower and the pressure of vacuum tower.The present invention also provides anhydrous atmospheric and vacuum distillation units.It is able to solve the low-temperature dew point corrosion problem of Atmospheric Tower using the device and technique, reduces oil refining sewerage, improves the diesel oil extracting rate of atmospheric residue, alleviates the serious entrainment of vacuum tower, reduces deep vacuum distillation vacuum degree.Improve long period, the safe and stable runnability of device.
Description
Technical field
The present invention relates to a kind of anhydrous atmospheric and vacuum distillation technique and devices, belong to crude oil atmospheric vacuum distillation technical field.
Background technique
Crude(oil)unit is petroleum refining " faucet " industry, be most crude oil enter behind refinery by first
Procedure, the stability of operating status not only affect the economic benefit of atmospheric and vacuum distillation unit, also determine following process process
Quality.Fig. 1 is the old process schematic diagram of conventional atmospheric vacuum distillation process, and the bottom of atmospheric tower 3 is stripped equipped with atmospheric tower
Section 7.Atmospheric and vacuum distillation unit processing capacity is very big, and the height of energy consumption is directly related to entire oil plant energy consumption level and economic benefit,
Modern crude distillation tower energy consumption in oil plant is huge, accounts for about the 15%-20% of refinery's total energy consumption, single to comment from energy consumption index
The distilling apparatus energy consumption of valence, China has been in more advanced level, oily for 9.2-9.5kg mark oil/ton, but this energy consumption index
It is to be obtained in the case where product quality, light oil yield and relatively low total extracting rate, the energy consumption of atmospheric and vacuum distillation unit is a surprising
Number, all there may be great economic benefit and social benefits for any technical progress.It can be seen from the above often subtracting
Press distillation technique operation stability and its energy consumption level to the equipment investment of enterprise, operational management, energy saving optimizing and economic benefit
Aspect is particularly important.
In recent years, oil refining enterprise, China is faced with the problem of crude oil heaviness, in poor quality, salt content, the acid of crude oil mostly
Value etc. is higher and higher, this also causes the desalination of crude electric desalter, dehydrating effect to become the great difficult problem that refinery faces.With
The influence of the factors such as heaviness, in poor quality and the tertiary oil recovery hardening agent of crude oil, electric desalting technology are difficult to meet primary distillation tower original
Oil charging salt content is not more than the production Con trolling index of 3mg/L, and the low-temperature dew point corrosion of atmospheric and vacuum distillation unit overhead system is increasingly tight
Weight.For the impurity in removing crude oil more as far as possible, refinery generally uses second level even three-level electric desalting technology, electric desalting apparatus
Enlargement more highlight crude electric desalter production effect be deteriorated reality, not only increase cost of equipment and sewage
Discharge capacity, the also different production requirement for surely reaching electro-desalting.
The impurity such as inorganic villaumite, the sulfide not removed during electro-desalting, enter during following process with crude oil.
When these impurity enter in atmospheric and vacuum distillation unit with crude oil, it can hydrolyze, easily be decomposed under high temperature at a certain temperature, especially be passed through
After crossing atmospheric pressure kiln, corrosive media HCl and H are generated2S gas.Butter is mainly NaCl, CaCl2、MgCl2, common
Hydrolysis is as follows:
NaCl+H2O=NaOH+2HCl
MgCl2+2H2O=Mg (OH)2+2HCl
CaCl2+2H2O=Ca (OH)2+2HCl
In the case where 360 DEG C of normal pressure heater outlet temperature or so, there is nearly 90% MgCl2With nearly 16% CaCl2Water occurs
Solution generates HCl gas.Decomposition, equipment green coke, the difficult target-seeking restriction of reboiler heat source, traditional atmospheric and vacuum distillation under by crude oil high temperature
The steam stripped technique of water vapour is used without reboiler, the following tower section of charging using vaporization feeding of heating furnace, tower bottom.HCl and H2S
Gas is non-corrosive under the situation existing for no liquid water, is safe from harm substantially to the operating characteristics of tower, therefore will not influence
The operation of the lower part and middle section of destilling tower.Normal pressure column overhead temperatures are generally 100-140 DEG C, and overhead reflux temperature is generally controlled
For system at 40-50 DEG C, water vapour easily condenses into liquid water, HCl and H with this condition2S gas tower top be condensed water absorb, shape
At HCl-H2S-H2O or HCl-H2O system has very strong corrosiveness, causes to corrode in the tower top device of atmospheric and vacuum distillation unit,
I.e. so-called low-temperature dew point corrosion, this process are the most serious in normal pressure column overhead.
To solve the problems, such as low-temperature dew point corrosion, " de- three notes " technology, including electrical oil dewatering are generally taken in technique at present
Salt and water filling, note neutralizer, note corrosion inhibiter in overhead condensation cooling system, the purpose is to reduce the salt in crude oil as far as possible
Content inhibits the generation of HCl, neutralizes generated acidic corrosive media, changes the pH value of environment, and form one in equipment surface
Layer protective film, hinders corrosive medium to contact with metal surface.This alleviates the tight of tower top low-temperature dew point corrosion to a certain extent
Principal characteristic, but the fluctuation of pH value is larger, is difficult to control.Neutralizer generally infuses inorganic ammonia at present, generates amine hydrochlorate and amine carbonic acid
Salt etc. easily leads to anticaustic, and can accumulate in Atmospheric Tower, causes fouling corrosion etc., blocking pipeline." de- three notes " are very big
Ground increases production cost, and is readily incorporated not degradable and regenerated new pollutant, cannot fundamentally solve low temperature dew point
Etching problem.
In addition, traditional atmospheric and vacuum distillation technique uses the steam stripped method of water vapour, the low temperature of overhead system is not only resulted in
Dew point corrosion problem can also generate a large amount of oil refining sewerage, not only contain petroleum-type, sulfide etc. in sewage, also containing a huge sum of money
Belong to, serious harm can be caused to the mankind and ecological environment.A large amount of water is needed in refinery's production process, although part water can be with
It being recycled, but still many oil refining sewerages can be generated, quantity even can achieve the 60%-70% of crude runs, wherein
The sewage that atmospheric and vacuum distillation generates accounts for greatly.Oil refining sewerage complicated component, organic matter especially hydro carbons and its derivative
Content is high, and containing various heavy, harm is serious, it is necessary to could discharge after treatment.In addition to organic matter, there are also greases, phenol
The substances such as class, sulfide, ammonia nitrogen, COD content is higher, and hard-degraded substance is more, and regenerability is poor, and processing energy consumption is high, expensive.Refining
Oily water generally has three kinds of physical treatment, chemical treatment, biological treatment methods, removes oil slick, oil emulsion, suspended matter in waste water
Deng, reduce waste water COD, BOD, fat content, phenols, sulfide content etc. reach discharge standard.In recent years, with
The adjustment of energy crisis and energy resource structure, environmental requirement is also increasingly strict, proposes the items such as water-saving, reduction quantity of wastewater effluent and refers to
Mark, energy-saving and emission-reduction are also current atmospheric and vacuum distillation technique problem in the urgent need to address.
Compared with oil product, the latent heat of vaporization of water is very big, and former Water in oil will increase fuel energy consumption in process, such as crude oil
Water content increases by 1%, due to additional more absorption heats, the heat-exchange temperature of crude oil can be made to reduce by 10 DEG C, it is negative to be equivalent to heating furnace heat
Lotus increases 5% or so.When crude oil water containing exchanges heat through heat exchanger, temperature is gradually risen, and water is easy to overheat, opposite due to water
Molecular mass is smaller than oil product average molecular mass, and volume sharply increases after a small amount of water vapor in crude oil, is formed very big
Resistance increases system pressure drop and power consumption, oil flow is caused to decline, and heat-exchange system pressure increases, even meeting when serious
Heat exchanger is caused to suppress leakage.
In addition, water vapour stripping causes liquid phase power load distributing in destilling tower extremely uneven, the vapour phase load of vaporization section is very
Height is very easy to the excessive entrainment phenomenon of generation mainly for atmospheric residue and decompression residuum and has seriously affected each side line
Product quality, reduce the property of secondary operation crude oil, make troubles for subsequent oil product process.Once water steams in atmospheric tower
The control of vapour dosage is bad, and operating effect is bad, will lead to excessive diesel oil distillate and distillates from vacuum 1st side cut, vacuum tower excess mist folder
Band is serious, so that its operation, extracting rate is affected, product quality is deteriorated, especially lube type vacuum tower, base oil coloration
It is heavier, fraction is wider, seriously constrain the production of thick oil base oil.
For fuels-type vacuum tower, predominantly catalytic cracking, offer raw material is provided, decompression extracting rate and extract fraction
Quality have a great impact to the economic benefit of the whole audience, deep vacuum distillation technology can be carried out, the yield of high Sulfur Residual Oil is reduced, subtract
The secondary operation amount of few residual oil.Generally at 560 DEG C or more, external some advanced technologies often subtract the cutting temperature of deep vacuum distillation
The true boiling-point (TBP) cutting of pressure device can even reach 600 DEG C or more, and the depth that China's decompression is extracted is obviously relatively low, generally 540
Under DEG C, this and maturity, the deep vacuum distillation operating condition severity height of China's atmospheric and vacuum distillation technology etc. have relationship.Decompression
Deep drawing generally requires raising decompression heater outlet temperature, but heater outlet temperature is higher, the coking problem generated by oil-cracking, condensation
It is more serious, the blocking of equipment is caused, the stability of production operation is influenced；It also can be realized decompression deeply by reducing decompression pressure tower
It pulls out, but due to the limitation of pumped vacuum systems load, the limitation of tower inner member pressure drop can all increase the difficulty of deep vacuum distillation technology
Degree.How mild deep vacuum distillation technology, and bottleneck one of that at present China atmospheric and vacuum distillation technology encounter are realized.
Faucet device of the atmospheric and vacuum distillation unit as petroleum industry, steady production are particularly important.Normal pressure column overhead
Low-temperature dew point corrosion can make the operational stability of device be deteriorated, and on-stream time greatly shortens.Oil refining sewerage largely generates, greatly
The energy consumption for increasing device, also increase the workload and operating cost of subsequent sewage disposal process.Phase is negative in tower simultaneously
Lotus is unevenly distributed, and the processing capacity of tower is caused to reduce, and vaporization section excess entrainment is serious, especially vacuum tower, not only makes
At oil distillation column lower part sideline product overlapping, product quality is deteriorated, and carbon residue, content of beary metal etc. are exceeded, influences two
The quality of secondary process raw material, and the energy consumption in separation process is considerably increased, reduce the treating capacity of fractionating column.
Although industrial applicability is strong, but still there are some in conclusion traditional atmospheric and vacuum distillation process technology maturation
Bottleneck, such as overhead system low-temperature dew point corrosion, oil refining sewerage yield is big, excessive entrainment is serious, deep vacuum distillation technical difficulty
Deng if without technical innovation, it will be difficult to overcome these difficulties.
Although having carried out a large amount of research work, traditional Atmospheric vacuum process base for Atmospheric vacuum technology both at home and abroad
It is used till today always in sheet.Research to Atmospheric Tower low-temperature dew point corrosion problem, the development for essentially consisting in novel corrosion inhibitor are opened
Hair.Patent application of the Fan Yuguang et al. at entitled " dew point controlled corrosion proof device for ordinary decompression column top system "
(CN1864789A) it is proposed in, anticorrosion tank is set before atmospheric and vacuum tower and condenser, liquid is set in anticorrosion tank
Water and corrosion inhibiter is added in body distributor and non-metallic fillers, the purpose is to by the sour gas corrosion medium in oil gas in anti-corrosion
It loses in tank and absorbs, prevent equipment such as condenser thereafter etc. from dew point corrosion phenomenon occurs.Although the device can prevent condenser
Etching problem, improve the service life of equipment, but normal pressure column overhead due to temperature it is lower, water vapour condensation in part can also inhale
It receives corrosive gas HCl and forms acid solution, etching problem does not obtain solution substantially.
About Atmospheric vacuum process energy consumption problem, Arjmand et al. was proposed in 2011 by improving steam feed import tower
Board position carries out the energy saving optimizing of atmospheric tower, and the gas-phase feed after prefractionation is introduced separately into the upper section of destilling tower, is made cold
Condenser load saves energy 12.6%.
About excessive entrainment problem, Yuan Yifu et al. is in entitled " atmospheric and vacuum distillation unit vapour-liquid load transfer skill
It is proposed that the primary distillation tower before atmospheric pressure kiln increases side line, and sideline product is injected in the patent (application No. is 98101068.7) of art "
Atmospheric tower appropriate location, and flash column is added before vacuum furnace, the purpose is to by crude oil after primary distillation tower flash distillation and atmospheric tower
The light component not being vaporized after distillation carries out flash separation, so as to mitigate the load of subsequent heating furnace and tower.
But because flash process is arranged before oil product enters heating furnace, oil product potential temperature is not high at this time, evaporating capacity very little, so for drop
The problem of gas-liquid phase load of low fractionating column (especially vacuum tower) vaporization section, reduction entrainment, improvement product overlapping, acts on
It is limited.
About deep vacuum distillation problem, Yuan Qing, Zhang Zhanzhu et al. are in a kind of entitled " vacuum distillation for improving extracting rate
It proposed in the patent application (CN102676211A) of method " after vacuum furnace, add vaporization tower before vacuum tower, reduced crude is through subtracting
It enters back into vacuum tower and is fractionated into progress part vaporization, vapo(u)rizing oil in vaporization tower after pressing stove heating, non-vaporization gasoline is straight
Connect as residual oil from device draw, the purpose is to reduce because of oil transfer line temperature drop and pressure drop caused by energy loss, improve vacuum tower
Extracting rate.But the process is higher to the outlet temperature requirements of vacuum furnace, even up to 460 DEG C of heater outlet temperature, crude oil
Middle high boiling fraction thermostability is poor, easily decomposes under high temperature, product quality is caused to decline, while making coking and blocking in pipeline, shadow
Ring the stable operation of device.
Zhang Lvhong, Zhang Daoguang et al. are at entitled " atmospheric vacuum distillation method and equipment with vacuum flasher "
It is proposed in patent application (CN101376068A) and adds vacuum flasher before vacuum furnace, flash column base oil enters vacuum furnace
Enter vacuum tower after heating, flash distillation tower overhead gas then enters in vacuum tower near certain sideline product outlet port similar in fraction, to reach
To treating capacity is improved, extracting rate is improved, the purpose of energy consumption is reduced.But tower overhead gas is injected vacuum tower top, phase by the flash column
Vacuum tower sectional feeding after in flash distillation, not in the fractionation for fundamentally changing vacuum tower, to the improvement effect for the treatment of capacity
It is unobvious.Vacuum flasher and vacuum tower do not share a set of pumped vacuum systems, considerably increase the expense of ancillary equipment.
Zhang Long, Qi Huimin, Wang Haibo et al. are in entitled " a kind of crude oil deep vacuum distillation technique for strengthening flash distillation "
It proposes to increase three stages of flashing tank in patent application (CN103242885A), atmospheric tower base oil enters level-one gasification furnace, heats laggard
Enter the separation of primary flash tank, gas phase enters vacuum tower top distillation stage, and liquid phase enters second level gasification furnace；Enter second level after heated
Flash tank, gas phase enter distillation stage in the middle part of vacuum tower, and liquid phase enters three-level gasification furnace；Enter three stages of flashing tank, gas after heated
Mutually enter vacuum tower lower part distillation stage, liquid phase enters vacuum tower flash zone；Each section feeding is evaporated under reduced pressure in vacuum tower, is subtracted
Tower lateral line withdrawal function sideline product is pressed, tower bottom extracts decompression residuum out, to improve the extracting rate in crude oil vacuum distillation process.This side
Method is additionally arranged three flash tanks, and oil product will be by heating before entering each flash tank, hence it is evident that increases device
Energy consumption and equipment investment cost, and the inlet temperature of third level flash tank reaches 420 DEG C, and the easy coking of oil product reduces
The operation stability of device.
Summary of the invention
In order to solve the above technical problems, the purpose of the present invention is to provide a kind of anhydrous atmospheric and vacuum distillation technique and device,
By way of adding vacuum flasher, replace the water vapour stripping of atmospheric tower tower bottom, mainly solves the low temperature dew of Atmospheric Tower
Spot corrosion phenomenon improves long period, the safe and stable runnability of device；The consumption for substantially reducing fresh water in refinery, subtracts
The generation of few oil refining sewerage, expense needed for reducing subsequent sewage disposal process, energy consumption respond energy-saving and emission-reduction policy, realize green
Color Atmospheric vacuum technique；Gas phase load in atmospheric tower is substantially reduced, overhead condenser duty is reduced, reduces energy consumption, improves atmospheric tower
Processing capacity；The diesel oil extracting rate of atmospheric residue is improved, the serious entrainment of vacuum tower is alleviated, reduces deep vacuum distillation vacuum
Degree.
In order to solve the above technical problems, the present invention provides a kind of anhydrous atmospheric and vacuum distillation techniques comprising:
Atmospheric tower and vacuum tower are by the way of four vaporization feedings, and crude oil is by normal pressure stove heating later from atmospheric tower tower
Kettle charging, atmospheric tower tower reactor are not passed through water vapour, and each sideline product is heated using reboiler, and normal pressure column overhead is cold through condensing
But the tower top dry gas after carries out alkali cleaning；
Vacuum flasher is added between atmospheric tower and vacuum furnace, the atmospheric residue come out from atmospheric tower tower reactor enters decompression
Flash column tower reactor；
Several side lines are arranged to extract product out, wherein the product of the first lateral line withdrawal function is recycled into normal pressure in vacuum flasher
Tower, bottom of tower heavy oil enters vacuum furnace and is further heated, subsequently into vacuum tower；
The pressure of vacuum flasher controls between atmospheric tower and the pressure of vacuum tower.
In above-mentioned anhydrous atmospheric and vacuum distillation technique, the operation in primary distillation tower does not change, and crude oil is by electric desalting and dewatering
Enter primary distillation tower after reason, the oil plant of primary distillation tower tower reactor outflow enters atmospheric pressure kiln and heated.Crude oil changes after electric desalting and dewatering
Heat is to 230 DEG C.
The outlet temperature of atmospheric pressure kiln may be controlled to 340-400 DEG C, preferably 360-380 DEG C.By improving atmospheric pressure kiln
Outlet temperature can reduce the re-injection flow of the first side line of vacuum flasher.
2-8 block hydraulic barrier is equipped with below the feedboard of atmospheric tower bottoms.It is no longer passed through water vapour in atmospheric tower and carries out vapour
It mentions, improves the heater outlet temperature (preferably 340-400 DEG C, more preferable 360-380 DEG C) of atmospheric pressure kiln, atmospheric tower charging can be increased
Vaporization rate partially makes up the reduction because of 350 DEG C of front-end volatiles extracting rate caused by lacking water vapour stripping, and crude oil is in atmospheric tower
Inside carry out fractionation production dry gas, liquefied gas, perfectly straight gasoline fraction, light diesel fuel fraction, heavy diesel fuel fraction, kerosene distillate and normal pressure weight
Oil.
Each side stripper of atmospheric tower no longer uses water vapour to strip, but uses the stripping section with reboiler, i.e., boils again
Stripper.Product quality can be reduced, such as increase the freezing point of aviation kerosine to avoid moisture is mixed into product by boiling stripper again
Deng.It is stripped using reboiler, comparison water vapour stripping, the volume flow of water vapour, does not reduce the gas phase load in tower, mention
The high processing capacity of tower.And the efficiency of reboiler is much larger than the steam stripped efficiency of water vapour.
Caustic treater is added after the condenser system of Atmospheric Tower to absorb HCl, H in tower top dry gas2The corrosivity gas such as S
Body.It may include two caustic treaters in parallel in caustic treater, it is few to add increased cost of equipment needed for caustic treater, can eliminate
The low-temperature dew point corrosion problem of Atmospheric Tower, substantially reduces equipment maintenance cost.Two caustic treaters periodically switch, and are conducive to alkali cleaning
The update of liquid improves device operation stability.
Due to lacking water vapour stripping, contains more light component in the heavy oil at atmospheric tower bottom, add and subtract after atmospheric tower
Flash column is pressed, the heavy oil at atmospheric tower bottom, which enters in depressurized system, further to be vaporized, and the fraction before 350 DEG C is vaporized and is extracted, and
Re-injection enters in atmospheric tower to be fractionated again.Reduced crude is fed from vacuum flashing tower reactor, tower bottom dry-steam stripping.Pass through regulation
The vacuum degree of vacuum flasher can control the extracting rate of diesel oil distillate, and it is 0.1-1.0kg/cm that tower pressure interior force, which recommends control,2,
Preferably 0.1-0.5kg/cm2.By regulating and controlling the pressure of vacuum flasher, mild deep vacuum distillation can be realized.
Vacuum flasher recommendation uses packed tower, because of small more of the pressure drop ratio plate column of packed tower, can reduce pumping very
Empty set system operational load.Filler is without anticorrosion material, because belonging to waterless operation in tower, and HCl, H2S corrosivity are situated between
Matter is completely drawn out substantially in atmospheric tower, will not generate etching problem.
2-4 side line can be set in vacuum flasher, and regulation middle section circulation takes heat to control the matter of lateral line withdrawal function oil
Amount reaches fraction cutting requirement, and the fraction before 350 DEG C of extraction of the control of the first side line, general re-injection enters in atmospheric tower to be divided again
It evaporates, if its quality meets product requirement, can extract out directly as product and converge with atmospheric tower heavy diesel fuel side line, be taken out as product
Out.Second side line can extraction section second line of distillation fraction, to further decrease the load of vacuum tower.
The position of vacuum flasher the first side line re-injection atmospheric tower, depending on the quality of the side run-off, preferably in normal pressure
Between tower light diesel fuel and the extraction side line of heavy diesel fuel, because the fraction of the first side line of vacuum flasher is essentially diesel oil distillate, return
The similar position section of oil quality in atmospheric tower is injected, it can the opposite consumption for reducing energy.
It can be equipped with 3-8 block theoretical plate, preferably 4-6 block in vacuum flasher, rough fractionation is carried out to oil plant, is being met
Under technique requires, number of theoretical plate is the smaller the better, can reduce tower pressure drop, reduces the operational load of pumped vacuum systems.Vacuum furnace
Outlet temperature control be 380-420 DEG C；Preferably, which includes the step for improving decompression heater outlet temperature and realizing deep vacuum distillation
Suddenly.Vacuum flasher and vacuum tower can use same pumped vacuum systems, can reduce the cost of equipment of pumped vacuum systems.
Pressure and middle section circulation in vacuum flasher take heat, depending on the overall processing side of crude quality and product requirement
Depending on case.By the pressure in regulation vacuum flasher, light component extracting rate can control, not only improve each side in atmospheric tower
The yield of line product, especially diesel product, and the thermic load of subsequent heating under reduced pressure furnace can be lowered, lower in vacuum tower
Vapour phase load substantially improves its excessive entrainment situation, improves fractionating column lower part sideline product overlapping, gum level
The problems such as height, product colour difference.
It is high to depressurize heater outlet temperature, vaporization rate is high, and oil product extracting rate is high, and the vacuum degree that vacuum tower carries out deep drawing needs can also
To reduce, but depressurize that heater outlet temperature is excessively high can cause oil coke.Vacuum flasher tower reactor heavy oil through decompression stove heating into
Enter vacuum tower, the heater outlet temperature of vacuum furnace generally between 380-420 DEG C, mentions depending on vacuum tower sideline product extracting rate
Height decompression heater outlet temperature, may be implemented deep vacuum distillation technology.Due to adding for vacuum flasher, deep vacuum distillation goes out vacuum furnace
The requirement of mouthful temperature substantially reduces, it is possible to reduce decomposition that oil product is generated because temperature is excessively high, coking cause under product yield
The problems such as drop, equipment coking.By the height of regulation decompression heater outlet temperature, it can determine that vacuum tower carries out the true of deep vacuum distillation
Reciprocal of duty cycle.
Dry type or wet type can be used in the action type for needing to select vacuum tower according to production.Vacuum tower can be adopted
With fuels-type vacuum tower or lube type vacuum tower.Wherein, water vapour stripping can be used in fuels-type vacuum tower, can also also adopt
With waterless operation (the steam stripped mode of dry-steam), main task is for catalytic cracking, is hydrocracked and provides raw material, is being controlled
Extracting rate is improved as far as possible under the premise of colloid, asphalitine and content of beary metal in distillate oil, it is not too many to the width of boiling range
Limitation.Lube type vacuum tower be recommended to use water vapour stripping, separation accuracy compared with fuels-type vacuum tower height, fractionating effect it is excellent
The bad quality for directly affecting following process process and lube product, requires boiling range narrow to a certain extent, therefore uses water vapour
It is preferable to strip product quality obtained.
The present invention also provides a kind of anhydrous atmospheric and vacuum distillation unit, which can be used for above-mentioned technique.The device
It include: primary distillation tower, atmospheric pressure kiln, atmospheric tower, vacuum flasher, vacuum furnace, vacuum tower, condenser, caustic treater, reboiler；
Wherein, the tower reactor of the primary distillation tower is connected to the atmospheric pressure kiln；
The oil plant outlet of the atmospheric pressure kiln is connected to the bottom inlet of the atmospheric tower；
The bottom of the atmospheric tower is without stripping section, also, the atmospheric tower is equipped with several side lines；
The side line of the atmospheric tower is connected to reboiler respectively；
The top exit of the atmospheric tower is connected to the condenser, and the condenser is connected to the caustic treater；
The outlet at bottom of the atmospheric tower is connected to the entrance of the vacuum flasher, and the re-injection of the vacuum flasher goes out
Mouth is connected to the re-injection entrance of the atmospheric tower；
The outlet at bottom of the vacuum flasher is connected to the vacuum furnace；
The vacuum furnace is connected to the bottom inlet of the vacuum tower, and the vacuum tower is equipped with several side lines.
Specific embodiment according to the present invention, it is preferable that above-mentioned anhydrous atmospheric and vacuum distillation unit include: primary distillation tower, often
Press furnace, atmospheric tower, vacuum flasher, vacuum furnace, vacuum tower, condenser, caustic treater, reboiler；
Wherein, the primary distillation tower is equipped with crude oil entrance, outlet at bottom and top exit；Crude oil entrance is for inputting by electricity
The crude oil of desalting and dewatering processing, outlet at bottom are used to be discharged the fraction of fore-running for exporting treated oil plant, top exit；
The atmospheric pressure kiln is equipped with fuel inlet, oil product entrance, exhanst gas outlet and oil plant outlet, and the bottom of the primary distillation tower goes out
Mouth is connected to the oil product entrance of the atmospheric pressure kiln；Atmospheric pressure kiln is for heating the oil plant from primary distillation tower, fuel inlet
For inputting the oil plant of heating, oil product entrance is used to input the oil plant for needing to heat, and exhanst gas outlet is for being discharged heating process
The flue gas of middle generation, oil plant outlet is for inputting the oil plant by heating to atmospheric tower；
The atmospheric tower is equipped with bottom inlet, outlet at bottom, the outlet of the first side line, re-injection entrance, the second side line export, the
The outlet of three side lines, top exit；The oil plant outlet of the atmospheric pressure kiln is connected to the bottom inlet of the atmospheric tower；The atmospheric tower
Bottom without stripping section, also, the outlet of the first side line, the outlet of the second side line, the outlet of third side line of the atmospheric tower connect respectively
It is connected to reboiler；Atmospheric tower is used to carry out oil plant normal pressure fractionation, and for inputting oil plant to be processed, bottom goes out bottom inlet
Mouth is used respectively for exporting the heavy oil generated in fractional distillation process, the outlet of the first side line, the outlet of the second side line, the outlet of third side line
In heavy diesel fuel fraction, light diesel fuel fraction, kerosene distillate that output fractionation obtains, re-injection entrance comes from vacuum flasher for injecting
Fraction, top exit be used for condenser input oil gas；
The condenser is equipped with entrance, fuel dispensing outlet and dry gas outlet；The top exit of the atmospheric tower and the condensation
The entrance of device is connected to；Condenser isolates gasoline and dry gas, dry gas enters caustic treater and handled for condensing to oil gas
After be discharged among atmosphere；
The dry gas outlet of the caustic treater and the condenser, caustic treater are absorbed for handling dry gas
HCl、H2The corrosive gas such as S；
The vacuum flasher is equipped with outlet at bottom, entrance, 2-4 side line outlet, re-injection outlet, top exit；It is described
The outlet at bottom of atmospheric tower is connected to the entrance of the vacuum flasher, re-injection outlet and the normal pressure of the vacuum flasher
The re-injection entrance of tower is connected to；Vacuum flasher is used to further be fractionated, and outlet at bottom is obtained for being discharged after fractionation
The heavy oil arrived, entrance is for inputting the heavy oil from atmospheric tower, the oil product that side line outlet is obtained for exporting fractionation, top exit
For vacuumizing, re-injection outlet for atmospheric tower input need to participate in again fractionation fraction or output meet product requirement
Oil product；
The vacuum furnace is equipped with fuel inlet, oil product entrance, exhanst gas outlet and oil plant outlet；The bottom of the vacuum flasher
Portion outlet is connected to the oil product entrance of the vacuum furnace；Vacuum furnace is used to heat the heavy oil from vacuum flasher,
Fuel inlet is used to input the oil plant of heating, and oil product entrance is used to input the heavy oil for needing to heat, and exhanst gas outlet is for being discharged
The flue gas generated in heating process, oil plant outlet is for inputting the heavy oil by heating to vacuum tower；
The vacuum tower is equipped with bottom inlet, steam entry, outlet at bottom, top exit, vacuum 1st side cut outlet, second line of distillation
It exports, subtracting three, line exports, subtracting four, line exports；The oil plant outlet of the vacuum furnace is connected to the bottom inlet of the vacuum tower；Subtract
Pressure tower is for being stripped, and to obtain corresponding oil product, bottom inlet is used to input the heavy oil by heating, steam entry
For inputting water vapour required for water vapour strips, outlet at bottom is used for generated decompression residuum, top exit to be discharged
In vacuumizing, vacuum 1st side cut outlet, second line of distillation outlet, subtracting three, line is exported, subtracting four, line outlet is respectively used to export different products.
In above-mentioned anhydrous atmospheric and vacuum distillation unit, the internal structure of primary distillation tower and operation are same as the prior art.
Vacuum flasher of the present invention can be plate column or packed tower, preferably packed tower.Vacuum tower can be with
It is fuels-type vacuum tower or lube type vacuum tower.
The present invention has the advantages that
(1) atmospheric tower is heated by reboiler replaces water vapour stripping, realizes the waterless operation condition in atmospheric tower, utilizes corruption
The small feature of corrosion gas corrosivity under the conditions of anhydrous not can ensure that the feelings of desalting effect in electro-desalting and demulsifier technology
Under condition, Atmospheric Tower low-temperature dew point corrosion can be thoroughly solved the problems, such as, improve long period, the safe and stable runnability of device；
Atmospheric tower separating effect resulting from reduces can be by adding the side of vacuum flasher after atmospheric tower, before vacuum furnace
Method is made up, and the diesel oil extracting rate of atmospheric residue can be not only increased, but also can reduce vacuum tower entrance because of gas phase load
Excess entrainment caused by excessive realizes load transfer technology, improves the treating capacity of vacuum distillation；
(2) HCl and H generated in atmospheric tower2The corrosive gas such as S as oil gas rises in tower, and are entered with dry gas
In tower top condensing system (condenser), caustic treater is added after tower top condensing system, absorbs corrosive gas in dry gas, it will not
It pollutes the environment；
(3) atmospheric tower tower reactor does not have water vapour to be passed through, and greatly reduces the usage amount of water vapour in refinery, reduces and often subtracts
The generation of oil refining sewerage in pressure Distallation systm, expense needed for reducing subsequent sewage disposal process, energy consumption, active response country
Energy-saving and emission-reduction policy realizes the atmospheric and vacuum distillation operation of green；
(4) dry-steam strips in atmospheric tower, and sideline product is stripped using reboiler, improves vapour in atmospheric tower well
The larger problem of liquid phase load, substantially reduces gas phase load in tower, especially stripping section, increases the processing capacity of atmospheric tower,
The load of overhead condenser is reduced simultaneously, saves cooling water amount, improves the efficiency of side line tower, reduces water content in product,
Stablize the quality of sideline product；
(5) atmospheric tower bottom crude oil feeding plate lower end can add hydraulic barrier, be the building for assisting vapour-liquid contact, increase tower
The contact area of interior liquid phase improves vapour-liquid distribution, is conducive to the progress of mass transfer, the light fraction carried secretly in bottom of tower heavy oil is made to the greatest extent may be used
Separation more than energy improves extracting rate；
(6) atmospheric residue carries out decompression prefractionation in vacuum flasher, gently evaporating before the first 350 DEG C of lateral line withdrawal function
Point, the extracting rate of diesel oil is improved, by the regulation of vacuum flasher operating pressure, can control the cutting accuracy of diesel oil, is realized
Ideal segmentation improves the problem that excessive entrainment is serious in oil distillation column, especially vacuum tower, further solves fractionating column
Lower part sideline product overlapping, gum level are high, product color value is poor, product quality is difficult the problems such as up to standard, reduce secondary add
Expenses of labour is used, and improves product quality, while improving the operational stability of device；
(7) for fuels-type vacuum tower, by changing the operating pressure of vacuum flasher, depressurizing the items such as heater outlet temperature
Part, improves the cutting accuracy of product, and controls and develop mild deep vacuum distillation technology.Regulate and control vacuum flasher operating pressure, drop
The content of light fraction in the low oil plant into vacuum tower reduces fixed gas content, improves the efficiency of pumped vacuum systems, can subtract
Deep vacuum distillation is realized in the pressure lower situation of heater outlet temperature, reduces the energy consumption of vacuum furnace, improves vacuum tower internal cause oil plant temperature
Situation of the cracking, condensation green coke that degree is high and generates to cause equipment to block, under mild conditions, deep vacuum distillation technology
The true boiling point of crude oil cutting can achieve 560 DEG C it is even higher；
(8) vacuum flasher is added, in the case where cost of equipment increases few, it is rotten to have reached elimination tower top low temperature dew point
Erosion, energy-saving and emission-reduction increase atmospheric and vacuum distillation unit processing capacity, improve excessive entrainment serious situation, realize the clear of diesel oil
It cuts, realize mild deep vacuum distillation technical equivalences fruit, be the bottleneck for breaking traditional atmospheric and vacuum distillation technology, realize green Atmospheric vacuum
The innovative technique of technique.
Detailed description of the invention
Fig. 1 is the flow diagram of conventional atmospheric vacuum distillation process.
Fig. 2 is the structure and flow diagram for the anhydrous atmospheric and vacuum distillation unit that embodiment 1 provides.
Fig. 3 is the tower bottom baffle arrangement schematic diagram of the atmospheric tower in embodiment 1.
Fig. 4 is the relational graph of light ends content in vacuum flashing pressure tower and the discharging of tower bottom tower.
Main Reference label declaration:
1- primary distillation tower 2- atmospheric pressure kiln 3- atmospheric tower 4- condenser 5- vacuum furnace 6- vacuum tower 7-
Atmospheric tower stripping section 8- caustic treater 9- vacuum flasher 10- normal pressure baffle plate section
Specific embodiment
In order to which technical characteristic of the invention, purpose and beneficial effect are more clearly understood, now to skill of the invention
Art scheme carries out described further below, but should not be understood as that limiting the scope of the invention.
Embodiment 1
A kind of anhydrous atmospheric and vacuum distillation unit is present embodiments provided, structure is as shown in Figure 2.The anhydrous atmospheric and vacuum distillation
Device include: primary distillation tower 1, atmospheric pressure kiln 2, atmospheric tower 3, vacuum flasher 9, vacuum furnace 5, vacuum tower 6, condenser 4, caustic treater 8,
Reboiler；
Wherein, primary distillation tower 1 is equipped with crude oil entrance, outlet at bottom and top exit；
Atmospheric pressure kiln 2 be equipped with fuel inlet, oil product entrance, exhanst gas outlet and oil plant outlet, the outlet at bottom of primary distillation tower 1 and often
Press the oil product entrance connection of furnace 2；
Atmospheric tower 3 is equipped with bottom inlet, outlet at bottom, the outlet of the first side line, the outlet of re-injection entrance, the second side line, third
Side line outlet, top exit；The oil plant outlet of atmospheric pressure kiln 2 is connected to the bottom inlet of atmospheric tower 3；The bottom of atmospheric tower 3 is without vapour
Section is proposed, also, the outlet of the first side line, the outlet of the second side line, the outlet of third side line of atmospheric tower 3 are connected separately with reboiler；It returns
The position of inlet exports between the outlet of the second side line in the first side line；3 bottom of atmospheric tower is equipped with normal pressure baffle plate section 10, interior
Equipped with 4 pieces of hydraulic barriers, as shown in Figure 3；
Condenser 4 is equipped with entrance, fuel dispensing outlet and dry gas outlet；The top exit of atmospheric tower 3 and the entrance of condenser 4 connect
It is logical；
The dry gas outlet of caustic treater 8 and condenser 4；
Vacuum flasher 9 is equipped with outlet at bottom, entrance, the outlet of the first side line, the outlet of the second side line, re-injection outlet, top
Outlet；The outlet at bottom of atmospheric tower 3 is connected to the entrance of vacuum flasher 9, the re-injection outlet of vacuum flasher 9 and atmospheric tower 3
Re-injection entrance connection；
Vacuum furnace 5 is equipped with fuel inlet, oil product entrance, exhanst gas outlet and oil plant outlet；The outlet at bottom of vacuum flasher 9
It is connected to the oil product entrance of vacuum furnace 5；
Vacuum tower 6 goes out equipped with bottom inlet, steam entry, outlet at bottom, top exit, vacuum 1st side cut outlet, second line of distillation
Mouth, subtracting three, line exports, subtracting four, line exports；The oil plant outlet of vacuum furnace 5 is connected to the bottom inlet of vacuum tower 6.
Embodiment 2
A kind of anhydrous atmospheric and vacuum distillation new process is present embodiments provided, is carried out using the device of embodiment 1,
Process is as shown in Figure 2.The technique the following steps are included:
Crude oil exchanges heat after electric desalting and dewatering to 230 DEG C or so, into primary distillation tower 1；
1 tower bottom oil plant of primary distillation tower enters atmospheric pressure kiln 2, and atmospheric tower 3 is entered after being heated to 360-370 DEG C and is fractionated, respectively
A side line is stripped by reboiler, obtains naphtha, heavy diesel fuel, light diesel fuel, kerosene, and the dry gas for being fractionated generation passes through tower top
Condenser 4 after enter caustic treater 8, by HCl, H therein2S gas is sloughed, and the gasoline that condenser 4 obtains is defeated as product
Out；
Also the front-end volatiles containing 350 DEG C of part are not cut completely in the heavy oil of 3 tower reactor of atmospheric tower, are heated being passed through vacuum furnace 5
Before, it is introduced into vacuum flasher 9, which controls in 0.1-0.5kg/cm2Between, before in atmospheric residue 350 DEG C
Fraction further separate, improve decompression before extracting rate, so that bottom of tower heavy oil is reached the requirement into vacuum tower 6；
The product of first lateral line withdrawal function of vacuum flasher 9 is returned atmospheric tower 3 and is fractionated again, 9 tower reactor of vacuum flasher
Heavy oil enter vacuum furnace and be heated to 390-420 DEG C, be fractionated into vacuum tower 6, to prevent equipment coking, vacuum tower 6 is adopted
With the steam stripped mode of water vapour.
Embodiment 3
Flowsheeting is carried out using heavier Da Liya crude oil as the raw material of atmospheric and vacuum distillation unit, 20 DEG C of density are 0.9078g/
cm3.500,000 tons/year of conventional atmospheric and vacuum distillation units and anhydrous atmospheric and vacuum distillation unit are separately designed, device parameter comparison is shown in Table 1.
It is simulated by 9.2 software of PRO/II, the effect of available routine Atmospheric vacuum technology and anhydrous Atmospheric vacuum new technology
Comparison, is shown in Table 2 and table 3.
In the anhydrous Atmospheric vacuum process it can be seen from the data in table 2 and table 3, water vapour is not passed through in atmospheric tower,
Therefore water recovery is not had in Atmospheric Tower, corrosive media HCl cannot be dissolved in water and form strong acid, as oil gas enters alkali
It is removed in cleaning of evaporator, eliminates the low-temperature dew point corrosion problem of Atmospheric Tower.In anhydrous Atmospheric vacuum process, each side line of atmospheric tower is produced
Product, which are done, slightly to be increased, and naphtha makes improve 2.20%, and the total output of the output increased 0.88% of aviation kerosine, diesel oil drops
Low 0.49%, diesel oil process broadens.Add vacuum flasher, light ends content is reduced to 2.67% before 350 DEG C in bottom of tower heavy oil,
The extracting rate of light fraction improves.Decompression residuum yield reduces 4.17% compared with old process in anhydrous process, total extracting rate of crude oil
It improves.Side line substantially saves energy 5.60Mkcal/h after boiling substitution side line water vapour stripping again.1 year uptime of device
It is 8450 hours, Nian Jieyue heat is 47360.63Mkcal/a.
Embodiment 4
Other operating conditions are constant, change the normal pressure heater outlet temperature of anhydrous Atmospheric vacuum process, the results are shown in Table 4-6.By table
Data in 4-6 can be seen that the raising with normal pressure furnace temperature, and the gas phase fraction of charging increases, the sideline product of atmospheric tower
In, naphtha, aviation kerosine, light diesel fuel yield be improved, the yield relative reduction of heavy diesel fuel, overflash oil mass increase.
When normal pressure heater outlet temperature is 365 DEG C, atmospheric residue flow is 41641.0kg/h, and temperature is increased to 370 DEG C, atmospheric residue
Flow-reduction about 2.44% (mass fraction) is 40623.7kg/h.
After temperature increases, light component is vaporized more in charging, and the fractionating effect of atmospheric tower makes moderate progress, some in temperature
The light component being dissolved in heavy diesel fuel fraction when spending lower is pulled out, and is entered in the side line of front, therefore naphtha, aviation coal
Oily, light diesel fuel yield respectively increased.
1 Atmospheric vacuum common process of table and anhydrous new process operating parameter compare
2 Atmospheric vacuum common process of table and anhydrous new process Comparative result
| Anhydrous Atmospheric vacuum | Conventional Atmospheric vacuum | |
| Atmospheric tower extracting rate | 30.87% | 41.60% |
| 350 DEG C of front-end volatiles contents of normal pressure bottom of tower heavy oil | 14.15% | 3.54% |
| Into 350 DEG C of front-end volatiles contents in vacuum tower material | 2.67% | 3.54% |
| Atmospheric tower gasoline production, kg/h | 2097.74 | 2042.76 |
| Kerosene yield, kg/h | 3416.82 | 3386.92 |
| Light diesel fuel yield, kg/h | 8721.66 | 9581.97 |
| Heavy diesel fuel yield, kg/h | 4834.84 | 4041.67 |
| Vacuum 1st side cut product yield, kg/h | 310.62 | 200.75 |
| Second line of distillation product yield, kg/h | 6699.53 | 7147.09 |
| Subtract three line product yield, kg/h | 6757.40 | 8739.50 |
| Subtract four line product yield, kg/h | 2315.42 | 2154.92 |
| Decompression residuum, kg/h | 15257.18 | 15921.06 |
Atmospheric tower product quality compares in 3 two schemes of table
4 vacuum tower extracting rate of table is with the variation DEG C for depressurizing heater outlet temperature
The energy of stripped vapor and reboiler compares in 5 atmospheric tower of table
Note: the conversion relationship of water vapour and energy is 0.01155Mkcal/kg
The influence of 6 normal pressure heater outlet temperature of table variation
Embodiment 5
Influence of the vacuum flashing pressure tower to light ends content in the discharging of its tower bottom tower is studied, vacuum flashing column overhead is controlled
Pressure is in 0.1-0.4kg/cm2Between, light component (fraction before 350 DEG C) content in bottom of tower heavy oil is compared, such as Fig. 4 institute
Show.As can be seen that the content of 350 DEG C of front-end volatiles increases in bottom of tower heavy oil with the raising of vacuum flasher tower top pressure, when
Pressure is controlled in 0.4kg/cm2When following, ends content is controllable before 350 DEG C in the heavy oil of vacuum flasher tower reactor in this process
System is under 5%.
Claims (26)
1. a kind of anhydrous atmospheric and vacuum distillation technique comprising:
Atmospheric tower and vacuum tower by the way of four vaporization feedings, crude oil by after normal pressure stove heating from atmospheric tower tower reactor into
Material, atmospheric tower tower reactor are not passed through water vapour, and each sideline product is heated using reboiler, and normal pressure column overhead is through condensation cooling
Tower top dry gas afterwards carries out alkali cleaning；
Vacuum flasher is added between atmospheric tower and vacuum furnace, the atmospheric residue come out from atmospheric tower tower reactor enters vacuum flashing
Tower tower reactor；
Several side lines are arranged to extract product out, wherein the product of the first lateral line withdrawal function is recycled into atmospheric tower, tower in vacuum flasher
Bottom heavy oil enters vacuum furnace and is further heated, subsequently into vacuum tower；
The pressure of vacuum flasher controls between atmospheric tower and the pressure of vacuum tower.
2. technique according to claim 1, wherein the outlet temperature control of the atmospheric pressure kiln is 340-400 DEG C.
3. technique according to claim 2, wherein the outlet temperature control of the atmospheric pressure kiln is 360-380 DEG C.
4. technique according to claim 1, wherein be equipped with 2-8 block baffling below the feedboard of the atmospheric tower bottoms and keep off
Plate.
5. technique according to claim 1, wherein the pressure control of the vacuum flasher is 0.1-1.0kg/cm2。
6. technique according to claim 5, wherein the pressure control of the vacuum flasher is 0.1-0.5kg/cm2。
7. technique according to claim 6, wherein the technique includes the pressure realization deep vacuum distillation for regulating and controlling vacuum flasher
The step of.
8. technique according to claim 1, wherein 2-4 side line is arranged in the vacuum flasher；
Wherein, the product of the first lateral line withdrawal function of the vacuum flasher is diesel oil distillate, is recycled into atmospheric tower and is fractionated again.
9. technique according to claim 5, wherein 2-4 side line is arranged in the vacuum flasher；
Wherein, the product of the first lateral line withdrawal function of the vacuum flasher is diesel oil distillate, is recycled into atmospheric tower and is fractionated again.
10. technique according to claim 6, wherein 2-4 side line is arranged in the vacuum flasher；
Wherein, the product of the first lateral line withdrawal function of the vacuum flasher is diesel oil distillate, is recycled into atmospheric tower and is fractionated again.
11. technique according to claim 7, wherein 2-4 side line is arranged in the vacuum flasher；
Wherein, the product of the first lateral line withdrawal function of the vacuum flasher is diesel oil distillate, is recycled into atmospheric tower and is fractionated again.
12. technique according to claim 8, wherein re-injection position is between light diesel fuel and the extraction plate of heavy diesel fuel.
13. technique according to claim 9, wherein re-injection position is between light diesel fuel and the extraction plate of heavy diesel fuel.
14. technique according to claim 10, wherein re-injection position is between light diesel fuel and the extraction plate of heavy diesel fuel.
15. technique according to claim 11, wherein re-injection position is between light diesel fuel and the extraction plate of heavy diesel fuel.
16. according to claim 1, the described in any item techniques of 5-15, wherein it is theoretical to be equipped with 3-8 block in the vacuum flasher
Plate.
17. according to claim 1, technique described in any one of 5-15, wherein the outlet temperature of the vacuum furnace, which controls, is
380-420℃。
18. technique according to claim 16, wherein the outlet temperature control of the vacuum furnace is 380-420 DEG C.
19. according to claim 1, technique described in any one of 5-15,18, wherein the vacuum flasher and the decompression
Tower uses same pumped vacuum systems, determines that vacuum tower carries out the vacuum of deep vacuum distillation by the height of regulation decompression heater outlet temperature
Degree.
20. technique according to claim 16, wherein the vacuum flasher is vacuumized with the vacuum tower using same
System determines that vacuum tower carries out the vacuum degree of deep vacuum distillation by the height of regulation decompression heater outlet temperature.
21. technique according to claim 17, wherein the vacuum flasher is vacuumized with the vacuum tower using same
System determines that vacuum tower carries out the vacuum degree of deep vacuum distillation by the height of regulation decompression heater outlet temperature.
22. -15,18,20,21 described in any item anhydrous atmospheric and vacuum distillation techniques according to claim 1, in which: according to product
Production needs to select the action type of vacuum tower, using dry type or wet type；
When using lube type vacuum tower, using the steam stripped mode of water vapour；When using fuels-type vacuum tower, use is anhydrous
The mode of steam stripping.
23. anhydrous atmospheric and vacuum distillation technique according to claim 16, in which: needed to select vacuum tower according to production
Action type, using dry type or wet type；
When using lube type vacuum tower, using the steam stripped mode of water vapour；When using fuels-type vacuum tower, use is anhydrous
The mode of steam stripping.
24. anhydrous atmospheric and vacuum distillation technique according to claim 17, in which: needed to select vacuum tower according to production
Action type, using dry type or wet type；
When using lube type vacuum tower, using the steam stripped mode of water vapour；When using fuels-type vacuum tower, use is anhydrous
The mode of steam stripping.
25. anhydrous atmospheric and vacuum distillation technique according to claim 19, in which: needed to select vacuum tower according to production
Action type, using dry type or wet type；
When using lube type vacuum tower, using the steam stripped mode of water vapour；When using fuels-type vacuum tower, use is anhydrous
The mode of steam stripping.
26. a kind of anhydrous atmospheric and vacuum distillation system comprising: primary distillation tower, atmospheric pressure kiln, atmospheric tower, vacuum flasher, vacuum furnace,
Vacuum tower, condenser, caustic treater, reboiler；
Wherein, the tower reactor of the primary distillation tower is connected to the atmospheric pressure kiln；
The oil plant outlet of the atmospheric pressure kiln is connected to the bottom inlet of the atmospheric tower；
The bottom of the atmospheric tower is without stripping section, also, the atmospheric tower is equipped with several side lines；
The side line of the atmospheric tower is connected to reboiler respectively；
The top exit of the atmospheric tower is connected to the condenser, and the condenser is connected to the caustic treater；
The outlet at bottom of the atmospheric tower is connected to the entrance of the vacuum flasher, the re-injection of vacuum flasher outlet with
The re-injection entrance of the atmospheric tower is connected to；
The outlet at bottom of the vacuum flasher is connected to the vacuum furnace；
The vacuum furnace is connected to the bottom inlet of the vacuum tower, and the vacuum tower is equipped with several side lines.
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