CN107699273A - 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
- Publication number
- CN107699273A CN107699273A CN201711129325.XA CN201711129325A CN107699273A CN 107699273 A CN107699273 A CN 107699273A CN 201711129325 A CN201711129325 A CN 201711129325A CN 107699273 A CN107699273 A CN 107699273A
- Authority
- CN
- China
- Prior art keywords
- tower
- vacuum
- atmospheric
- flasher
- oil
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
-
- 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 invention provides a kind of anhydrous atmospheric and vacuum distillation technique and device.The technique includes：Atmospheric tower and vacuum tower are by the way of four vaporization feedings, crude oil is fed after normal pressure stove heat from atmospheric tower tower reactor, tower reactor is not passed through water vapour, and each sideline product is heated using reboiler, and the tower top dry gas after the condensed cooling of normal pressure column overhead carries out alkali cleaning；Vacuum flasher is set up between atmospheric tower and vacuum furnace, the atmospheric residue come out from atmospheric tower tower reactor enters vacuum flasher；Vacuum flasher sets some side lines to extract product out, and the product of the first lateral line withdrawal function is recycled into atmospheric tower, and tower reactor heavy oil enters after vacuum furnace further heats and enters vacuum tower；The Stress control of vacuum flasher is between atmospheric tower and the pressure of vacuum tower.Present invention also offers anhydrous atmospheric and vacuum distillation unit.The low-temperature dew point corrosion problem of Atmospheric Tower is can solve the problem that 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.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 device, belong to crude oil atmospheric vacuum distillation technical field.
Background technology
Crude(oil)unit be petroleum refining " tap " industry, be most crude oil enter refinery after by first
Procedure, the stability of its running 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 its atmospheric tower 3 strips provided with atmospheric tower
Section 7.Atmospheric and vacuum distillation unit processing capacity is very big, and the height of its energy consumption is directly connected to whole oil plant energy consumption level and economic benefit,
Modern crude distillation tower energy consumption in oil plant is huge, accounts for the 15%-20% of refinery's total energy consumption, single to be commented from energy consumption index
Valency, the distilling apparatus energy consumption in China are in more advanced level, oily for 9.2-9.5kg marks oil/ton, but this energy consumption index
Be product quality, light oil yield and total extracting rate it is relatively low in the case of obtain, the energy consumption of atmospheric and vacuum distillation unit is surprising
Numeral, all there may be great economic benefit and social benefit for any technical progress.Often subtract it can be seen from more than
Press equipment investment, operational management, energy saving optimizing and the economic benefit of distillation technique operation stability and its energy consumption level to enterprise
Aspect is particularly important.
In recent years, oil refining enterprise of China is faced with the problem of crude oil heaviness, in poor quality, salt content, the acid of crude oil mostly
The more and more highers such as value, this also causes the desalination of crude electric desalter, dehydrating effect to turn into the great difficult problem that refinery faces.With
Heaviness, the in poor quality of crude oil, and the influence of the factor such as tertiary oil recovery hardening agent, electric desalting technology are difficult to meet primary distillation tower original
Oil charging salt content is not more than 3mg/L production Con trolling index, and the low-temperature dew point corrosion of atmospheric and vacuum distillation unit overhead system is increasingly tight
Weight.For the impurity in as far as possible more removing crude oil, refinery is typically using two level even three-level electric desalting technology, electric desalting apparatus
Maximization more highlight crude electric desalter production effect be deteriorated reality, not only increase cost of equipment and sewage
Discharge capacity, also differ and surely reach the production requirement of electro-desalting.
The impurity such as the inorganic villaumite that is not removed during electro-desalting, sulfide, are entered during following process with crude oil.
When these impurity with crude oil enter atmospheric and vacuum distillation unit in, can hydrolyze, easily be decomposed under high temperature at a certain temperature, particularly be passed through
After crossing atmospheric pressure kiln, Korrosionsmedium HCl and H are generated2S gases.Butter is mainly NaCl, CaCl2、MgCl2, it is common
Hydrolysis is as follows：
NaCl+H2O=NaOH+2HCl
MgCl2+2H2O=Mg (OH)2+2HCl
CaCl2+2H2O=Ca (OH)2+2HCl
In the case of 360 DEG C or so of normal pressure heater outlet temperature, there is nearly 90% MgCl2With nearly 16% CaCl2Generation water
Solution, generate HCl gases.Decomposition, the difficult target-seeking restriction of equipment green coke, reboiler thermal 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, bottom of towe.HCl and H2S
Gas non-corrosiveness under situation existing for no aqueous water, the operating characteristics of tower is safe from harm substantially, therefore do not interfered with
The operation of the bottom and center section of destilling tower.Normal pressure column overhead temperatures are generally 100-140 DEG C, and overhead reflux temperature is typically controlled
For system at 40-50 DEG C, water vapour easily condenses into aqueous water, HCl and H on this condition2S gases tower top be condensed water absorb, shape
Into HCl-H2S-H2O or HCl-H2O system, there is very strong corrosiveness, cause 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 nertralizer, note corrosion inhibiter in overhead condensation cooling system, the purpose is to reduce the salt in crude oil as far as possible
Content, suppress HCl generation, neutralize the acidic corrosive media generated, change the pH value of environment, and one is formed in equipment surface
Layer diaphragm, hinders corrosive medium to be contacted 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, it is difficult to control.Nertralizer typically notes inorganic ammonia at present, generates amine hydrochlorate and amine carbonic acid
Salt etc., anticaustic is easily caused, and can be accumulated in Atmospheric Tower, cause fouling corrosion etc., blocking pipeline." de- three notes " are very big
Ground adds production cost, and is readily incorporated not degradable and regeneration new pollutant, it is impossible to fundamentally solves 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, substantial amounts of oil refining sewerage can be also produced, not only contains petroleum-type, sulfide etc. in sewage, also containing a huge sum of money
The mankind and ecological environment can be caused serious harm by category.Substantial amounts of water is needed in refinery's production process, although part water can be with
Recycling, but still many oil refining sewerages can be produced, its quantity can even reach the 60%-70% of crude runs, wherein
Sewage caused by atmospheric and vacuum distillation accounts for greatly.Oil refining sewerage complicated component, organic matter particularly hydro carbons and its derivative
Content is high, serious containing various heavy, harm, it is necessary to could to discharge after treatment.In addition to organic matter, also grease, phenol
The materials such as class, sulfide, ammonia nitrogen, COD contents are higher, and hard-degraded substance is more, and regenerability is poor, processing high energy consumption, expensive.Refining
Oily water typically has three kinds of physical treatment, chemical treatment, biological treatment methods, removes oil slick, oil emulsion, suspension in waste water
Deng, reduction waste water COD, BOD, fat content, phenols, sulfide content etc., reach discharge standard.In the last few years, with
The adjustment of energy crisis and energy resource structure, environmental requirement are also increasingly strict, it is proposed that the items such as water saving, reduction quantity of wastewater effluent refer to
Mark, energy-saving and emission-reduction are also the problem of current atmospheric and vacuum distillation technique is 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 can increase fuel energy consumption in process, such as crude oil
Water content increase by 1%, it is negative equivalent to heating furnace heat due to extra 10 DEG C of heat-exchange temperature reductions for absorbing heat, crude oil being made more
Lotus adds 5% or so.When crude oil water containing exchanges heat through heat exchanger, temperature gradually rises, and water is easy to overheat, relative 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, increase system pressure drop and power consumption, cause oil flow to decline, the increase of heat-exchange system pressure, even meeting when serious
Heat exchanger is caused to suppress Lou.
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, it is very easy to produce excessive entrainment phenomenon, mainly for atmospheric residue and decompression residuum, has had a strong impact on each side line
Product quality, reduce the property of secondary operation crude oil, make troubles for follow-up oil product process.Once water steams in atmospheric tower
The control of vapour dosage is bad, and operating effect is bad, and excessive diesel oil distillate can be caused to be distillated from vacuum 1st side cut, vacuum tower excess mist folder
Band is serious, its operation, extracting rate is affected, product quality is deteriorated, especially lube type vacuum tower, its base oil colourity
It is heavier, cut 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 cut
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.The cutting temperature of deep vacuum distillation is typically more than 560 DEG C, and some external advanced technologies, it often subtracts
The true boiling-point (TBP) cutting of pressure device can even reach more than 600 DEG C, and the depth that China's decompression is extracted is substantially relatively low, typically 540
Under DEG C, this maturity with China's atmospheric and vacuum distillation technology, deep vacuum distillation operating condition severity height etc. have relation.Decompression
Deep drawing generally requires raising decompression heater outlet temperature, but heater outlet temperature is higher, the coking problem as caused by oil-cracking, condensation
It is more serious, the blocking of equipment is caused, influences the stability of production operation；It can also realize that decompression is deep by reducing decompression pressure tower
Pull 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 gentle deep vacuum distillation technology, and bottleneck that at present China atmospheric and vacuum distillation technology run into one of are realized.
Faucet device of the atmospheric and vacuum distillation unit as petroleum industry, its steady production are particularly important.Normal pressure column overhead
Low-temperature dew point corrosion, the operational stability of device can be made to be deteriorated, on-stream time greatly shortens.Oil refining sewerage largely produces, greatly
The energy consumption for adding device, also increase the workload and operating cost of follow-up sewage disposal process.Phase is born in tower simultaneously
Lotus skewness, causes the disposal ability of tower to reduce, and vaporization section excess entrainment is serious, especially vacuum tower, not only makes
Into oil distillation column bottom 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.
In summary, although traditional atmospheric and vacuum distillation flow technology maturation, industrial applicability is strong, but still in the presence of
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 difficult.
Although substantial amounts of research work, traditional Atmospheric vacuum flow base are carried out for Atmospheric vacuum technology both at home and abroad
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 Yu light et al. at entitled " dew point controlled corrosion proof device for ordinary decompression column top system "
(CN1864789A) proposed in, anticorrosion tank is set before atmospheric and vacuum tower and condenser, liquid is set in anticorrosion tank
Body distributor and non-metallic fillers, add water and corrosion inhibiter, the purpose is to by the sour gas corrosion medium in oil gas in anti-corrosion
Lose in tank and absorb, 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 relatively low, the condensation of part water vapour, can also inhale
Receive corrosive gas HCl and form acid solution, its etching problem does not obtain solution substantially.
Itd is proposed on Atmospheric vacuum process energy consumption problem, Arjmand et al. 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 epimere of destilling tower, made cold
Condenser load saves energy 12.6%.
On excessive entrainment problem, Yuan Yifu et al. in entitled " atmospheric and vacuum distillation unit vapour-liquid load transfer skill
The increase side line of the primary distillation tower before atmospheric pressure kiln is proposed in the patent (Application No. 98101068.7) of art ", sideline product is injected
Atmospheric tower appropriate location, and flash column is set up 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 follow-up heating furnace and tower.
But because flash process is arranged on oil product into before heating furnace, now oil product potential temperature is not high, evaporating capacity very little, so for drop
The gas-liquid phase load of low fractionating column (particularly vacuum tower) vaporization section, entrainment is reduced, improves the problem of product is overlapping and acts on
It is limited.
On deep vacuum distillation problem, Yuan Qing, Zhang Zhanzhu et al. in a kind of entitled " vacuum distillation for improving extracting rate
Itd is proposed in the patent application (CN102676211A) of method " after vacuum furnace, vaporization tower is set up before vacuum tower, reduced crude is through subtracting
Enter back into vacuum tower and be fractionated into progress part vaporization, vapo(u)rizing oil in vaporization tower after pressing stove heat, non-vaporization gasoline is straight
Connect and drawn as residual oil from device, the purpose is to reduce the energy loss caused by oil transfer line temperature drop and pressure drop, 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, is easily decomposed under high temperature, causes product quality to decline, while makes 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 that carry vacuum flasher "
Proposed in patent application (CN101376068A) and vacuum flasher is set up 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 similar in cut near certain sideline product outlet port, with up to
To treating capacity is improved, extracting rate is improved, reduces the purpose of energy consumption.But tower overhead gas is injected vacuum tower top, phase by the flash column
Vacuum tower sectional feeding after in flash distillation, the fractionation of vacuum tower, the raising effect to treating capacity are not being changed fundamentally
Unobvious.Vacuum flasher does not share a set of pumped vacuum systems with vacuum tower, considerably increases the expense of auxiliary 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 "
Increase three stages of flashing tank is proposed in patent application (CN103242885A), atmospheric tower base oil enters one-level gasification furnace, and heating is laggard
Enter the separation of primary flash tank, gas phase enters vacuum tower top distillation stage, and liquid phase enters two level gasification furnace；Enter two 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 bottom 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, bottom of towe extracts decompression residuum out, so as to improve the extracting rate in crude oil vacuum distillation process.This side
Method is additionally arranged three flash tanks, and oil product will pass through heating before each flash tank is entered, hence it is evident that adds device
Energy consumption and equipment investment cost, and the inlet temperature of third level flash tank reaches 420 DEG C, the easy coking of oil product, reduces
The operation stability of device.
The content of the invention
In order to solve the above technical problems, it is an object of the invention to provide a kind of anhydrous atmospheric and vacuum distillation technique and device,
By way of setting up vacuum flasher, the water vapour stripping of substitution atmospheric tower bottom of towe, mainly solves the low temperature dew of Atmospheric Tower
Spot corrosion phenomenon, improve the long period of device, safe and stable runnability；The consumption of fresh water in refinery is substantially reduced, is subtracted
The generation of few oil refining sewerage, reduces expense, the energy consumption needed for follow-up sewage disposal process, responds energy-saving and emission-reduction policy, realizes green
Color Atmospheric vacuum technique；Gas phase load in atmospheric tower is substantially reduced, reduces overhead condenser duty, reduces energy consumption, improves atmospheric tower
Disposal ability；The diesel oil extracting rate of atmospheric residue is improved, alleviates the serious entrainment of vacuum tower, reduces deep vacuum distillation vacuum
Degree.
In order to solve the above technical problems, the invention provides a kind of anhydrous atmospheric and vacuum distillation technique, it includes：
Atmospheric tower and vacuum tower are by the way of four vaporization feedings, and crude oil is by normal pressure stove heat afterwards from atmospheric tower tower
Kettle is fed, and atmospheric tower tower reactor is not passed through water vapour, and each sideline product is heated using reboiler, and normal pressure column overhead is condensed cold
But the tower top dry gas after carries out alkali cleaning；
Vacuum flasher is set up between atmospheric tower and vacuum furnace, the atmospheric residue come out from atmospheric tower tower reactor enters decompression
Flash column tower reactor；
Vacuum flasher sets some side lines to extract product out, wherein the product of the first lateral line withdrawal function is recycled into normal pressure
Tower, bottom of tower heavy oil is further heated into vacuum furnace, subsequently into vacuum tower；
The Stress control of vacuum flasher is 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 is heated into atmospheric pressure kiln.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, the re-injection flow of the side line of vacuum flasher first can be reduced.
2-8 block hydraulic barriers are provided with below the feedboard of atmospheric tower bottoms.Water vapour is no longer passed through in atmospheric tower and carries out vapour
Carry, improve the heater outlet temperature (preferably 340-400 DEG C, more preferably 360-380 DEG C) of atmospheric pressure kiln, atmospheric tower charging can be increased
Vaporization rate, the reduction of 350 DEG C of the front-end volatiles extracting rate caused by lacking water vapour stripping is partly made up, crude oil is in atmospheric tower
Inside carry out fractionation production dry gas, liquefied gas, perfectly straight gasoline fraction, light diesel fuel cut, heavy diesel fuel cut, kerosene distillate and normal pressure weight
Oil.
Each side stripper of atmospheric tower is no longer stripped using water vapour, but uses the stripping section with reboiler, i.e., boils again
Stripper.Boiling stripper again can avoid being mixed into moisture in product, reduce product quality, such as raise the freezing point of aviation kerosine
Deng.Stripped using reboiler, contrast water vapour stripping, without the volume flow of water vapour, reduce the gas phase load in tower, carry
The high disposal ability of tower.And the efficiency of reboiler is much larger than the steam stripped efficiency of water vapour.
Caustic treater is set up after the condenser system of Atmospheric Tower to absorb HCl, H in tower top dry gas2The corrosivity gas such as S
Body.Two caustic treaters in parallel can be included in caustic treater, it is few to set up 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, beneficial to alkali cleaning
The renewal of liquid, improve plant running stability.
Due to lacking water vapour stripping, contain more light component in the heavy oil at atmospheric tower bottom, set up 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 cut before 350 DEG C is vaporized and extracted, and
Re-injection enters in atmospheric tower to be fractionated again.Reduced crude is fed from vacuum flashing tower reactor, bottom of towe dry-steam stripping.Pass through regulation and control
The vacuum of vacuum flasher, the extracting rate of diesel oil distillate can be controlled, 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, gentle deep vacuum distillation can be realized.
Vacuum flasher is recommended to use packed tower, because small more of the pressure drop ratio plate column of packed tower, can reduce and take out very
Empty set system operational load.Filler need not use anticorrosion material, because belong to waterless operation in tower, and HCl, H2S corrosivity are situated between
Matter is completely drawn out substantially in atmospheric tower, will not produce etching problem.
Vacuum flasher can set 2-4 bar side lines, and the circulation of regulation and control stage casing takes heat to control the matter of lateral line withdrawal function oil
Amount reaches cut split requirement, and the cut before 350 DEG C is extracted in the control of the first side line out, and general re-injection enters in atmospheric tower to be divided again
Evaporate, 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
Go out.Second side line can extraction section second line of distillation cut, so as to further reduce vacuum tower load.
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 cut of the side line of vacuum flasher first is essentially diesel oil distillate, return
The position section that oil quality is similar in atmospheric tower is injected, can the relative consumption for reducing energy.
3-8 block theoretical plates, preferably 4-6 blocks can be provided with vacuum flasher, rough fractionation is carried out to oil plant, is being met
Under technological requirement, number of theoretical plate is the smaller the better, can reduce tower internal drop, reduces the operational load of pumped vacuum systems.Vacuum furnace
Outlet temperature control be 380-420 DEG C；Preferably, the technique includes improving the step that decompression heater outlet temperature realizes deep vacuum distillation
Suddenly.Vacuum flasher can use same pumped vacuum systems with vacuum tower, can reduce the cost of equipment of pumped vacuum systems.
Pressure in vacuum flasher takes heat with stage casing circulation, depending on the overall processing side of crude quality and product requirement
Depending on case.By regulating and controlling the pressure in vacuum flasher, light component extracting rate can be controlled, not only improves each side in atmospheric tower
The yield of line product, especially diesel product, and the thermic load of follow-up heating under reduced pressure stove can be lowered, lower in vacuum tower
Vapour phase load, its excessive entrainment situation is substantially improved, improve fractionating column bottom 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 that vacuum tower carries out deep drawing needs also may be used
To reduce, but depressurize that heater outlet temperature is too high can cause oil coke.Vacuum flasher tower reactor heavy oil enters through depressurizing stove heat
Enter vacuum tower, the heater outlet temperature of vacuum furnace typically between 380-420 DEG C, carries depending on vacuum tower sideline product extracting rate
Height decompression heater outlet temperature, it is possible to achieve deep vacuum distillation technology.Due to setting up for vacuum flasher, deep vacuum distillation goes out to vacuum furnace
The requirement of mouthful temperature substantially reduces, it is possible to reduce oil product because temperature is too high and caused by decompose, coking, cause under product yield
The problems such as drop, equipment coking.By the height for regulating and controlling decompression heater outlet temperature, it may be determined that vacuum tower carries out the true of deep vacuum distillation
Reciprocal of duty cycle.
Needed to select the action type of vacuum tower according to production, dry type or wet type can be used.Vacuum tower can be adopted
With fuels-type vacuum tower or lube type vacuum tower.Wherein, fuels-type vacuum tower can be stripped using water vapour, also can also be adopted
With waterless operation (the steam stripped mode of dry-steam), its main task is for catalytic cracking, is hydrocracked offer raw material, controlling
Extracting rate is improved as far as possible on 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 recommends water vapour stripping, and its separation accuracy is high compared with fuels-type vacuum tower, fractionating effect it is excellent
The bad quality for directly affecting following process process and lube product, require that boiling range is narrow to a certain extent, therefore use water vapour
The obtained product quality of stripping is preferable.
Present invention also offers a kind of anhydrous atmospheric and vacuum distillation unit, the device can be used for above-mentioned technique.The device
Including：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 connects with the atmospheric pressure kiln；
The oil plant outlet of the atmospheric pressure kiln connects with the bottom inlet of the atmospheric tower；
The bottom of the atmospheric tower is without stripping section, also, the atmospheric tower is provided with some side lines；
The side line of the atmospheric tower connects with reboiler respectively；
The top exit of the atmospheric tower connects with the condenser, and the condenser connects with the caustic treater；
The outlet at bottom of the atmospheric tower connects with the entrance of the vacuum flasher, and the re-injection of the vacuum flasher goes out
Mouth connects with the re-injection entrance of the atmospheric tower；
The outlet at bottom of the vacuum flasher connects with the vacuum furnace；
The vacuum furnace connects with the bottom inlet of the vacuum tower, and the vacuum tower is provided with some side lines.
According to specific embodiments of the present invention, it is preferable that above-mentioned anhydrous atmospheric and vacuum distillation unit includes：Primary distillation tower, often
Press stove, atmospheric tower, vacuum flasher, vacuum furnace, vacuum tower, condenser, caustic treater, reboiler；
Wherein, the primary distillation tower is provided with crude oil entrance, outlet at bottom and top exit；Crude oil entrance is used to input by electricity
The crude oil of desalting and dewatering processing, outlet at bottom are used to export treated oil plant, and top exit is used for the cut for discharging fore-running；
The atmospheric pressure kiln is provided with fuel inlet, oil product entrance, exhanst gas outlet and oil plant outlet, and the bottom of the primary distillation tower goes out
Mouth connects with the oil product entrance of the atmospheric pressure kiln；Atmospheric pressure kiln is used to heat the oil plant from primary distillation tower, its 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 used to discharge heating process
In caused flue gas, oil plant export for atmospheric tower input by heating oil plant；
The atmospheric tower is provided 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 connects with 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 the 3rd 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 its bottom inlet is used to input pending oil plant, and bottom goes out
Mouth is used to export the caused heavy oil in fractional distillation process, and the outlet of the first side line, the outlet of the second side line, the 3rd side line are exported and used respectively
In heavy diesel fuel cut, light diesel fuel cut, kerosene distillate that output fractionation obtains, re-injection entrance, which is used to inject, comes from vacuum flasher
Cut, top exit be used for condenser input oil gas；
The condenser is provided with entrance, fuel dispensing outlet and dry gas outlet；The top exit of the atmospheric tower and the condensation
The entrance connection of device；Condenser is used to condense oil gas, isolates gasoline and dry gas, dry gas is handled into caustic treater
After be discharged among air；
The dry gas outlet of the caustic treater and the condenser, caustic treater are used to handle dry gas, absorbed
HCl、H2The corrosive gas such as S；
The vacuum flasher is provided 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 connects with the entrance of the vacuum flasher, re-injection outlet and the normal pressure of the vacuum flasher
The re-injection entrance connection of tower；For being further fractionated, its outlet at bottom is used to obtain after discharging fractionation vacuum flasher
The heavy oil arrived, entrance are used to input the heavy oil from atmospheric tower, and side line exports the oil product obtained for exporting fractionation, top exit
For vacuumizing, re-injection is exported for needing to participate in the cut of fractionation again to atmospheric tower input or output meets product requirement
Oil product；
The vacuum furnace is provided with fuel inlet, oil product entrance, exhanst gas outlet and oil plant outlet；The bottom of the vacuum flasher
Portion outlet connects with the oil product entrance of the vacuum furnace；Vacuum furnace is used to heat the heavy oil from vacuum flasher, its
Fuel inlet is used for the oil plant for inputting heating, and oil product entrance is used to input the heavy oil for needing to heat, and exhanst gas outlet is used to discharge
Caused flue gas in heating process, oil plant are exported for inputting the heavy oil by heating to vacuum tower；
The vacuum tower is provided with bottom inlet, steam entry, outlet at bottom, top exit, vacuum 1st side cut outlet, second line of distillation
Export, subtracting three, line exports, subtracting four, line exports；The oil plant outlet of the vacuum furnace connects with the bottom inlet of the vacuum tower；Subtract
Pressure tower is used to be stripped, and to obtain corresponding oil product, its bottom inlet is used to input the heavy oil by heating, steam entry
The water vapour required for inputting water vapour stripping, outlet at bottom are used to discharge caused decompression residuum, and top exit is used
In vacuumizing, vacuum 1st side cut outlet, second line of distillation outlet, subtracting three, line exports, 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 advantage of the invention is that：
(1) atmospheric tower heats substitution water vapour stripping by reboiler, realizes the waterless operation condition in atmospheric tower, utilizes corruption
Corrosion gas not can ensure that the feelings of desalting effect corrosivity is small under the conditions of anhydrous the characteristics of in electro-desalting and demulsifier technology
Under condition, can thoroughly solve the problems, such as Atmospheric Tower low-temperature dew point corrosion, improve the long period of device, safe and stable runnability；
Separating effect that atmospheric tower thereby results in reduces can be by setting up the side of vacuum flasher after atmospheric tower, before vacuum furnace
Method is made up, and can not only increase the diesel oil extracting rate of atmospheric residue, and can reduce vacuum tower entrance because of gas phase load
Excessive entrainment, realizes load transfer technology caused by excessive, 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 entered with dry gas
In tower top condensing system (condenser), caustic treater is set up after tower top condensing system, absorbs corrosive gas in dry gas, will not
Environment is polluted；
(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 Distallation systm is pressed, reduces expense, the energy consumption needed for follow-up sewage disposal process, active response country
Energy-saving and emission-reduction policy, realize the atmospheric and vacuum distillation operation of green；
(4) dry-steam is stripped in atmospheric tower, and sideline product is stripped using reboiler, improves vapour in atmospheric tower well
The problem of liquid phase load is larger, gas phase load in tower, especially stripping section are substantially reduced, increase the disposal ability 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,
The quality of stable sideline product；
(5) atmospheric tower bottom crude oil feeding plate lower end can set up hydraulic barrier, be the structure for aiding in vapour-liquid contact, increase tower
The contact area of interior liquid phase, improve vapour-liquid distribution, be advantageous to the progress of mass transfer, the light fraction for making to carry secretly in bottom of tower heavy oil to the greatest extent may be used
Separation more than energy, improve extracting rate；
(6) atmospheric residue carries out decompression prefractionation in vacuum flasher, and light before the first 350 DEG C of lateral line withdrawal function evaporates
Point, the extracting rate of diesel oil is improved, by the regulation and control of vacuum flasher operating pressure, the cutting accuracy of diesel oil can be controlled, realized
Ideal segmentation, improves the problem of excessive entrainment is serious in oil distillation column, especially vacuum tower, further solves fractionating column
The problems such as bottom sideline product overlapping, gum level are high, product colour is poor, product quality is difficult up to standard, reduce secondary add
Expenses of labour is used, and improves product quality, while improve the operational stability of device；
(7) for the bar such as fuels-type vacuum tower, operating pressure, decompression heater outlet temperature by changing vacuum flasher
Part, improves the cutting accuracy of product, and controls development 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, fixed gas content is reduced, the efficiency of pumped vacuum systems is improved, can subtract
Deep vacuum distillation is realized in the case that pressure heater outlet temperature is relatively low, reduces the energy consumption of vacuum furnace, improves vacuum tower internal cause oil plant temperature
Spend high and caused cracking, be condensed green coke so as to cause the situation that equipment blocks, under mild conditions, deep vacuum distillation technology
The true boiling point of crude oil cutting can reach 560 DEG C of even more highs；
(8) vacuum flasher is set up, in the case where cost of equipment increase is few, has reached the corruption of elimination tower top low temperature dew point
Erosion, energy-saving and emission-reduction, increase atmospheric and vacuum distillation unit disposal ability, improve excessive entrainment serious situation, realize the clear of diesel oil
Cut, realize gentle deep vacuum distillation technical equivalences fruit, be the bottleneck of atmospheric and vacuum distillation technology of breaking traditions, realize green Atmospheric vacuum
The innovative technique of technique.
Brief description of the drawings
Fig. 1 is the schematic flow sheet of conventional atmospheric vacuum distillation process.
Fig. 2 is the structure and schematic flow sheet for the anhydrous atmospheric and vacuum distillation unit that embodiment 1 provides.
Fig. 3 is the bottom of towe baffle arrangement schematic diagram of the atmospheric tower in embodiment 1.
Fig. 4 is the graph of a relation of vacuum flashing pressure tower and light ends content in the discharging of bottom of towe tower.
Main Reference label declaration：
1- primary distillation tower 2- atmospheric pressure kiln 3- atmospheric tower 4- condenser 5- vacuum furnace 6- vacuum towers 7-
Atmospheric tower stripping section 8- caustic treater 9- vacuum flasher 10- normal pressure deflection plate sections
Embodiment
In order to which technical characteristic, purpose and the beneficial effect of the present invention is more clearly understood, now to the skill of the present invention
Art scheme carry out it is described further below, but it is not intended that to the present invention can practical range restriction.
Embodiment 1
A kind of anhydrous atmospheric and vacuum distillation unit is present embodiments provided, its structure is as shown in Figure 2.The anhydrous atmospheric and vacuum distillation
Device includes：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 provided with crude oil entrance, outlet at bottom and top exit；
Atmospheric pressure kiln 2 be provided with fuel inlet, oil product entrance, exhanst gas outlet and oil plant outlet, the outlet at bottom of primary distillation tower 1 with often
Press the oil product entrance connection of stove 2；
Atmospheric tower 3 is provided with bottom inlet, outlet at bottom, the outlet of the first side line, the outlet of re-injection entrance, the second side line, the 3rd
Side line outlet, top exit；The oil plant outlet of atmospheric pressure kiln 2 connects with the bottom inlet of atmospheric tower 3；The bottom of atmospheric tower 3 is without vapour
Section is put forward, also, the outlet of the first side line, the outlet of the second side line, the outlet of the 3rd side line of atmospheric tower 3 are connected to reboiler；Return
The position of inlet is exported between the outlet of the second side line in the first side line；The bottom of atmospheric tower 3 is provided with normal pressure deflection plate section 10, interior
Provided with 4 pieces of hydraulic barriers, as shown in Figure 3；
Condenser 4 is provided with entrance, fuel dispensing outlet and dry gas outlet；The top exit of atmospheric tower 3 connects with the entrance of condenser 4
It is logical；
The dry gas outlet of caustic treater 8 and condenser 4；
Vacuum flasher 9 is provided 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 connects with the entrance of vacuum flasher 9, re-injection outlet and the atmospheric tower 3 of vacuum flasher 9
Re-injection entrance connection；
Vacuum furnace 5 is provided with fuel inlet, oil product entrance, exhanst gas outlet and oil plant outlet；The outlet at bottom of vacuum flasher 9
Connected with the oil product entrance of vacuum furnace 5；
Vacuum tower 6 goes out provided 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 connects with the bottom inlet of vacuum tower 6.
Embodiment 2
A kind of anhydrous atmospheric and vacuum distillation new technology is present embodiments provided, it is carried out using the device of embodiment 1, its
Flow is as shown in Figure 2.The technique comprises the following steps：
Crude oil exchanges heat to 230 DEG C or so, into primary distillation tower 1 after electric desalting and dewatering；
The bottom of towe oil plant of primary distillation tower 1 enters atmospheric pressure kiln 2, is fractionated after being heated to 360-370 DEG C into atmospheric tower 3, respectively
Individual side line is stripped by reboiler, obtains naphtha, heavy diesel fuel, light diesel fuel, kerosene, and dry gas caused by fractionation passes through tower top
Condenser 4 after enter caustic treater 8, by HCl, H therein2S gases are sloughed, and the gasoline that condenser 4 obtains is defeated as product
Go out；
Also the front-end volatiles containing 350 DEG C of part are not cut totally in the heavy oil of the tower reactor of atmospheric tower 3, are heated being passed through vacuum furnace 5
Before, vacuum flasher 9 is introduced into, the pressure tower is controlled in 0.1-0.5kg/cm2Between, before in atmospheric residue 350 DEG C
Cut further separate, improve decompression before extracting rate, 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, the tower reactor of vacuum flasher 9
Heavy oil be heated to 390-420 DEG C into vacuum furnace, 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 contrast is shown in Table 1.
Simulated by the softwares of PRO/II 9.2, the effect of conventional Atmospheric vacuum technology and anhydrous Atmospheric vacuum new technology can be obtained
Contrast, is shown in Table 2 and table 3.
In the anhydrous Atmospheric vacuum flow it can be seen from the data in table 2 and table 3, no water vapour is passed through in atmospheric tower,
Therefore water recovery is not had in Atmospheric Tower, Korrosionsmedium HCl can not 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 flow, each side line production of atmospheric tower
Product, which are done, slightly to be raised, and naphtha makes improve 2.20%, and the output increased 0.88% of aviation kerosine, the total output of diesel oil drops
Low 0.49%, diesel oil flow broadens.Set up 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.The more conventional flow of decompression residuum yield reduces 4.17% in anhydrous flow, total extracting rate of crude oil
Improve.Side line substantially saves energy 5.60Mkcal/h after boiling substitution side line water vapour stripping again.1 year uptime of device
For 8450 hours, it was 47360.63Mkcal/a that year, which saves heat,.
Embodiment 4
Other operating conditions are constant, change the normal pressure heater outlet temperature of anhydrous Atmospheric vacuum flow, the results are shown in Table 4-6.By table
Data in 4-6 can be seen that with the rise of normal pressure furnace temperature, the gas phase fraction increase of charging, the sideline product of atmospheric tower
In, naphtha, aviation kerosine, the yield of light diesel fuel are improved, the yield relative reduction of heavy diesel fuel, the increase of overflash oil mass.
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), it is 40623.7kg/h.
After temperature rise, light component vaporizes more in charging, and the fractionating effect of atmospheric tower makes moderate progress, and some are in temperature
The light component being dissolved in when spending relatively low in heavy diesel fuel cut is pulled out, and is entered in side line above, therefore naphtha, aviation coal
Oil, the yield of light diesel fuel respectively increased.
The Atmospheric vacuum common process of table 1 contrasts with anhydrous new technology operating parameter
The Atmospheric vacuum common process of table 2 and anhydrous new technology 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% |
| Enter 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 contrasts in the two schemes of table 3
The vacuum tower extracting rate of table 4 is with the change DEG C for depressurizing heater outlet temperature
The energy of stripped vapor and reboiler contrasts in the atmospheric tower of table 5
Note：The conversion relation of water vapour and energy is 0.01155Mkcal/kg
The influence of the normal pressure heater outlet temperature of table 6 change
Embodiment 5
The influence of light ends content during vacuum flashing pressure tower discharges to its bottom of towe tower is studied, controls vacuum flashing column overhead
Pressure is in 0.1-0.4kg/cm2Between, light component (cut before 350 DEG C) content in bottom of tower heavy oil is contrasted, such as Fig. 4 institutes
Show.As can be seen that with the rise of vacuum flasher tower top pressure, the content increase of 350 DEG C of front-end volatiles in bottom of tower heavy oil, when
Stress control is in 0.4kg/cm2When following, ends content is controllable before 350 DEG C in the heavy oil of vacuum flasher tower reactor in this flow
System is under 5%.
Claims (10)
1. a kind of anhydrous atmospheric and vacuum distillation technique, it includes：
Atmospheric tower and vacuum tower are by the way of four vaporization feedings, and crude oil after normal pressure stove heat from atmospheric tower tower reactor by entering
Material, atmospheric tower tower reactor are not passed through water vapour, and each sideline product is heated using reboiler, the condensed cooling of normal pressure column overhead
Tower top dry gas afterwards carries out alkali cleaning；
Vacuum flasher is set up between atmospheric tower and vacuum furnace, the atmospheric residue come out from atmospheric tower tower reactor enters vacuum flashing
Tower tower reactor；
Vacuum flasher sets some side lines to extract product out, wherein the product of the first lateral line withdrawal function is recycled into atmospheric tower, tower
Bottom heavy oil is further heated into vacuum furnace, subsequently into vacuum tower；
The Stress control of vacuum flasher is 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, preferably
360-380℃；
It is highly preferred that the technique includes the outlet temperature for improving atmospheric pressure kiln, the re-injection flow of the side line of vacuum flasher first is reduced
The step of.
3. technique according to claim 1, wherein, 2-8 blocks baffling is provided with below the feedboard of the atmospheric tower bottoms and is kept off
Plate.
4. technique according to claim 1, wherein, the Stress control of the vacuum flasher is 0.1-1.0kg/cm2, it is excellent
Elect 0.1-0.5kg/cm as2；It is highly preferred that the step of pressure that the technique includes regulation and control vacuum flasher realizes deep vacuum distillation.
5. the technique according to claim 1 or 4, wherein, the vacuum flasher sets 2-4 bar side lines；
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,
Re-injection position is preferably between light diesel fuel and the extraction plate of heavy diesel fuel.
6. according to the technique described in claim 1,4 or 5, wherein, it is provided with 3-8 block theoretical plates in the vacuum flasher.
7. according to the technique any one of claim 1,4,5 and 6, wherein, the outlet temperature control of the vacuum furnace is
380-420℃；Preferably, the technique includes improving the step of decompression heater outlet temperature realizes deep vacuum distillation.
8. according to the technique any one of claim 1 and 4-7, wherein, the vacuum flasher is adopted with the vacuum tower
With same pumped vacuum systems, the height by regulating and controlling to depressurize heater outlet temperature determines that vacuum tower carries out the vacuum of deep vacuum distillation.
9. the anhydrous atmospheric and vacuum distillation technology according to claim any one of 1-8, wherein：Need to select according to production
The action type of vacuum tower, it is preferred to use 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.
10. a kind of anhydrous atmospheric and vacuum distillation system, it includes：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 connects with the atmospheric pressure kiln；
The oil plant outlet of the atmospheric pressure kiln connects with the bottom inlet of the atmospheric tower；
The bottom of the atmospheric tower is without stripping section, also, the atmospheric tower is provided with some side lines；
The side line of the atmospheric tower connects with reboiler respectively；
The top exit of the atmospheric tower connects with the condenser, and the condenser connects with the caustic treater；
The outlet at bottom of the atmospheric tower connects with the entrance of the vacuum flasher, the re-injection of vacuum flasher outlet with
The re-injection entrance connection of the atmospheric tower；
The outlet at bottom of the vacuum flasher connects with the vacuum furnace；
The vacuum furnace connects with the bottom inlet of the vacuum tower, and the vacuum tower is provided with some side lines.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711129325.XA CN107699273B (en) | 2017-11-15 | 2017-11-15 | A kind of anhydrous atmospheric and vacuum distillation technique and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711129325.XA CN107699273B (en) | 2017-11-15 | 2017-11-15 | A kind of anhydrous atmospheric and vacuum distillation technique and device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107699273A true CN107699273A (en) | 2018-02-16 |
| CN107699273B CN107699273B (en) | 2019-09-06 |
Family
ID=61178580
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711129325.XA Active CN107699273B (en) | 2017-11-15 | 2017-11-15 | A kind of anhydrous atmospheric and vacuum distillation technique and device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107699273B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112048331A (en) * | 2020-08-21 | 2020-12-08 | 马金山 | Raw oil primary distillation processing device and production process |
| CN113975839A (en) * | 2021-10-21 | 2022-01-28 | 山东昌邑石化有限公司 | Novel grading flash evaporation equipment and process |
| CN114292659A (en) * | 2022-01-25 | 2022-04-08 | 枣庄杰富意振兴化工有限公司 | Coal tar deep processing method |
| CN114853591A (en) * | 2022-06-13 | 2022-08-05 | 扬州大学 | Resource utilization method of acetone and carbon dioxide in sodium phenolate carboxylation reaction |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4261814A (en) * | 1977-11-30 | 1981-04-14 | Exxon Research And Engineering Co. | Vacuum pipestill operation |
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| 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 |
| CN103242896A (en) * | 2012-02-06 | 2013-08-14 | 中国石油化工股份有限公司 | Reduced pressure distillation method with low energy consumption and deep total distillation rate |
| CN104053751A (en) * | 2012-01-17 | 2014-09-17 | 国际壳牌研究有限公司 | Process For Vacuum Distillation Of A Crude Hydrocarbon Stream |
| CN106318435A (en) * | 2015-06-18 | 2017-01-11 | 中石化洛阳工程有限公司 | Normal pressure distillation method |
| CN107057747A (en) * | 2016-11-07 | 2017-08-18 | 中国石油大学(华东) | It is a kind of based on the energy-efficient deep drawing technique of Atmospheric vacuum clearly cut |
-
2017
- 2017-11-15 CN CN201711129325.XA patent/CN107699273B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4261814A (en) * | 1977-11-30 | 1981-04-14 | Exxon Research And Engineering Co. | Vacuum pipestill operation |
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| 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 |
| CN104053751A (en) * | 2012-01-17 | 2014-09-17 | 国际壳牌研究有限公司 | Process For Vacuum Distillation Of A Crude Hydrocarbon Stream |
| CN103242896A (en) * | 2012-02-06 | 2013-08-14 | 中国石油化工股份有限公司 | Reduced pressure distillation method with low energy consumption and deep total distillation rate |
| CN106318435A (en) * | 2015-06-18 | 2017-01-11 | 中石化洛阳工程有限公司 | Normal pressure distillation method |
| CN107057747A (en) * | 2016-11-07 | 2017-08-18 | 中国石油大学(华东) | It is a kind of based on the energy-efficient deep drawing technique of Atmospheric vacuum clearly cut |
Non-Patent Citations (1)
| Title |
|---|
| 王丽云: "原油的常减压蒸馏过程的模拟与优化", 《中国优秀硕士学位论文全文数据库（电子期刊）》 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112048331A (en) * | 2020-08-21 | 2020-12-08 | 马金山 | Raw oil primary distillation processing device and production process |
| CN113975839A (en) * | 2021-10-21 | 2022-01-28 | 山东昌邑石化有限公司 | Novel grading flash evaporation equipment and process |
| CN113975839B (en) * | 2021-10-21 | 2023-01-10 | 山东昌邑石化有限公司 | Grading flash evaporation equipment and process |
| CN114292659A (en) * | 2022-01-25 | 2022-04-08 | 枣庄杰富意振兴化工有限公司 | Coal tar deep processing method |
| CN114292659B (en) * | 2022-01-25 | 2023-09-01 | 枣庄杰富意振兴化工有限公司 | Deep processing method of coal tar |
| CN114853591A (en) * | 2022-06-13 | 2022-08-05 | 扬州大学 | Resource utilization method of acetone and carbon dioxide in sodium phenolate carboxylation reaction |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107699273B (en) | 2019-09-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107699273B (en) | A kind of anhydrous atmospheric and vacuum distillation technique and device | |
| US3625881A (en) | Crank case oil refining | |
| CN104419444B (en) | A kind of method utilizing the moisture sump oil of delayed coking unit freshening | |
| CN102153449B (en) | Continuous refining separation device and method for coal gasification crude phenol | |
| CN102951762B (en) | Method and system for preventing scales and improving recycling water quality of saliferous and oily wastewater thermal desalination | |
| CN106336939A (en) | Refining technique of base oil regenerated from used lubrication oil | |
| CN100486920C (en) | Gas field methanol sewage disposal process | |
| US9969944B2 (en) | Dissolved oil removal from quench water of gas cracker ethylene plants | |
| CN106477792A (en) | A kind of method and device for stripping process petrochemical industry sour water nothing side line single column negative pressure | |
| CN103964631A (en) | Efficient coal-water slurrygasification ash water treatment method | |
| CN102491578B (en) | Method for stripping emptying tower top sewage by utilizing coke tower waste heat | |
| CN101602641B (en) | Double-effect rectification method and system thereof for finely separating hybrid pentane isomer | |
| CN108485790A (en) | A method of improving regenerating waste oil treating capacity | |
| CN204151297U (en) | A kind of chlorion extracting corrosion-resisting device | |
| RU2544994C1 (en) | Method and unit for oil preliminary distillation | |
| RU2372379C1 (en) | Cleaning method of hydrogen sulfide- and mercaptan bearing oil | |
| CN106830605A (en) | A kind of sludge combination treatment method and device | |
| CN110642314A (en) | Process unit for comprehensively utilizing crude oil electric desalting sewage by delayed coking device | |
| CN210462963U (en) | Dilute steam generator capable of controlling steam/hydrocarbon ratio for light hydrocarbon thermal cracking | |
| CN201952379U (en) | Continuous refining and separating device of gasified crude phenol | |
| CN106318435A (en) | Normal pressure distillation method | |
| CN1009304B (en) | Atmospheric-type thermodynamic deoxidizing method without using water vapour | |
| CN107267202A (en) | A kind of hydrogenated diesel oil refinery gas stripping fractionation and negative pressure desorption method and its device | |
| CN111825258B (en) | Coking residual ammonia water treatment device and method | |
| CN210915945U (en) | Equipment for preparing regenerated base oil from waste mineral oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |