CN104498076B

CN104498076B - A kind of method that light oil is produced in the hydrocarbon stream of self-contained heavy oil

Info

Publication number: CN104498076B
Application number: CN201410645835.2A
Authority: CN
Inventors: 何巨堂
Original assignee: Individual
Current assignee: Luoyang Rui Hua New Energy Technology Development Co Ltd
Priority date: 2014-11-06
Filing date: 2014-11-06
Publication date: 2017-08-22
Anticipated expiration: 2034-11-06
Also published as: CN104498076A

Abstract

A kind of method that light oil is produced in hydrocarbon stream of self-contained heavy oil, is suitable for the processing of middle coalite tar, using indirect heating manner realize the depth of residue fraction vaporize and reduce its heating process maximum temperature suppress thermal condensation reaction：Separate section is vaporized first, the hydrocarbon feed F01 of the ZYC containing residue fraction comprising liquid and vapor capacity is separated into vapour phase V1 and liquid phase L1；At least a portion vapour phase V1 obtains high-temperature gas V2 as vapor phase stream V11 to be heated after vapour phase heating part heat temperature raising；Separate section is vaporized second, at least a portion liquid phase L1 and at least a portion high temperature gas phase V2 completion mixing contact and are separated into the depth vaporization that at least a portion residue fraction gasification in gas phase V3 and liquid phase L3, liquid phase L1 enters completion liquid phase L1 in gas phase V3；Clear gusoline can be made by hydrogenation process by condensing oil product obtained by gas phase V3.

Description

A kind of method that light oil is produced in the hydrocarbon stream of self-contained heavy oil

Technical field

The present invention relates to a kind of method that light oil is produced in hydrocarbon stream of self-contained heavy oil；Particularly the present invention relates to one The method that light oil is produced in the low hydrogen content miscella for planting self-contained heavy oil component；More particularly the present invention relates to one kind is self-contained The method that light oil is produced in the coal base oil of heavy oil component, is suitable for the processing of middle coalite tar, using indirect heating manner The maximum temperature realized the depth vaporization (reducing coal tar asphalt yield) of residue fraction and reduce its heating process suppresses heat Condensation reaction, the cold oil of depth vaporization gained steam can produce clear gusoline by hydro-upgrading.

Background technology

In order to describe the problem, the present invention is (such as conventional to boil by conventional middle coalite tar heavy oil or residual oil or coal tar pitch Point is higher than 500 DEG C of coal tar fraction) be divided into light residue fraction and heavy resid component is treated, such as by normal boiling point be 500~ 540 DEG C of coal tar oil ingredient is referred to as the light residue fraction of coal tar, normal boiling point is higher than to 540 DEG C of coal tar oil ingredient referred to as coal tar Oily heavy resid component.Therefore, it is exactly by conventional coal tar on middle coalite tar depth vaporization question essence of the present invention The problem of light residue fraction vaporization separation of coal tar is deviate from, while namely improving coal tar heavy duty residue fraction purity or improving it The problem of softening point.

Coalite tar product in the dry distillation of coal process such as coal semi-coke process of coalite tar, gained in producing at present Containing a number of coal tar residual oil (such as normal boiling point is higher than 500 DEG C of coal tar fraction).Coal tar residual oil possesses Boiling point is high, resin and asphalt content is high, the characteristics of being easily condensed coking of being heated, in conventional fractional distillation process, in order to avoid height The heating upper limit value that anneal crack solution is present, even with comprehensive technical measure such as using charging heating furnace, to heating furnace A variety of hands such as injection stripped vapor, vacuum distillation reduction operating pressure, vacuum tower charging aperture throttled steam used below in boiler tube Section, can not realize that (such as normal boiling point is 500~540 DEG C of coal tar from the light residue oil fraction of deep drawing in coal-tar residue oil distillate Dregs of fat oil distillate) target, when coal tar heavy oil remaining carbon it is relatively low (i.e. it is therein it is potential hydrogenation material component such as normal boiling point be 500~540 DEG C of coal tar fraction is more) it is forced such as to enter the hot-working such as delayed coking as coal-tar residue oil processing During process, the in poor quality for foring resource is utilized.For the coal tar heavy oil of low residual carbon content, above mentioned problem forms great Economic loss.And the distillation separation method for solving the problem is there is no at present.

By taking coalite tar processing in 500,000 tons/year of semi-coke device productions as an example, coalite tar can in 500,000 tons/year of fractionation To obtain the coal tar heavy oil that about 10~15% 5.0~7.5 ten thousand tons/year of normal boiling point is higher than 500 DEG C, the coal tar heavy oil It is 500~540 DEG C of coal tar fractions containing 50~70% normal boiling point, even if even if isolate half calculates its number by 50% Amount also has 2.5~3.75 ten thousand tons/year, if separating successfully, benefit is also huge.

In order to improve the extracting rate of the light residue fraction of coal tar, if only consideration distillation principle without considering coal-tar residue The thermal condensation coking of oil, realizes that (such as normal boiling point is 500~540 DEG C of coal tar to deep drawing lighter fraction in coal tar heavy fractioning Oil distillate) target be possible, table 1 lists the lower boiling point data for analytical of hydro carbons decompression and used.

The hydro carbons atmospheric boiling point of table 1 and decompression boiling point conversion, unit DEG C

Because the residual oil of middle coalite tar has the temperature-sensitive feature of easy coking, ensureing the precondition in long running cycle Under, the heating separation method of the conventional coal tar for directly heating the heavy oil comprising middle coalite tar or residual oil is difficult to can not be real The depth vaporization target of existing middle coalite tar of the present invention.

The charging heating furnace of coalite tar fractionating column in existing full cut is described below, the low temperature coal tar in full cut The fractionating column system of oil, coal tar is separated into the light fraction of bottom of towe coal tar pitch and removing coal tar pitch.

Tested, under normal pressure, about existed according to the hot-working of northern Shensi Shenmu County, Fugu one with coalite tar in typical full cut 425~440 DEG C, middle coalite tar occurs first fast pyrolysis and produces condensation product while discharging a large amount of gases, partial condensates Thing adheres to the inwall of container, it is therefore necessary to which the heating furnace tube highest inner wall temperature TH of coalite tar is less than certain in strict control Such as 425 DEG C of one setting, generally regulation heating furnace tube highest inner wall temperature TH is less than 410 DEG C to protect in commercial plant operation Stay 15 DEG C of safety temperature away from, so middle maximum temperature of the coalite tar in the heating furnace tube of non-coking by heated stove stove The thermal conductivity factor that the thickness and oil film composition of inside pipe wall oil film retention layer have is determined.Such as, fractionating column requires coil outlet Ambient condition is that absolute pressure is that 0.10MPa, temperature are 360 DEG C, and the temperature difference of such boiler tube inwall oil film retention layer can only be less than 50 DEG C, that is to say, that boiler tube inwall oil film retention layer is uniform or thinner and the temperature difference of oil film everywhere is both less than 50 DEG C and could meet peace Produce entirely without coking.Can only be by reducing operation pressure if the temperature difference of boiler tube inwall oil film retention layer is more than 50 DEG C Power reduces operation temperature to compensate, because industrial reduction operating pressure has lower limit, so it is by reduction to be typically only capable to Operation temperature causes the reduction of the rise of coal tar pitch yield and light fraction yield to compensate.

For the charging heating furnace of coalite tar fractionating column in full cut, the medium in boiler tube has two major features：The One is, comprising a large amount of easily condensations or easy coking component such as alkene, phenols, condensed-nuclei aromatics, gum asphalt, temperature to be limited more than safety A large amount of condensation products can be produced after degree and boiler tube inner surface is attached to；Second be coalite tar in full cut boiling range is wide and boiling point The pyrocondensation sum velocity of higher component is faster, the temperature-rise period of middle coalite tar be both low viscosity light component evaporation process and The concentration process of liquid phase glue pitch shape component, also just says that the liquid phase in the process fluid of the outlet section of boiler tube is high viscosity Easily it is condensed the high concentration liquid phase of gum asphalt.The charging heating of coalite tar fractionating column in existing industrialized full cut Stove, it is most of to there is the easy coking of boiler tube, the problem of the operation cycle is short, it is accomplished by coke cleaning and burns within about 3~4 months, or uses The method for changing coking boiler tube shortens the coke cleaning time, therefore, delays coking, extension operation cycle to have significant industrial value.

Light vaporization rate of residual oil this purpose is improved in order to realize, the present invention proposes a kind of slag for avoiding centering coalite tar The direct-fired method of oil, direct-fired component is that the component i.e. distillate that coking is relatively difficult in middle coalite tar steams Vapour, then completes heating vaporization by contact heat-exchanging, i.e., the relative component i.e. residual oil for being easiest to coking in centering coalite tar The method that component is vaporized using indirectly heat suppresses thermal condensation reaction, its work to reduce the maximum temperature of residue fraction heating process Skill is contemplated：

Separate section STEP1 is vaporized first, by F01 points of the hydrocarbon feed of the ZYC containing residue fraction comprising liquid and vapor capacity From for gas V1 and liquid phase L1, the first vaporization separate section STEP1 operation temperatures are T1；At least a portion gas V1 is as to be added Hot vapor phase stream V11, it is understood that there may be remaining gas V1 be used as bypass vapor phase stream V12；

In vapour phase heating part STEP2, vapor phase stream V11 to be heated, which is heated to after second temperature T2, is used as High Temperature Gas Body V2；

It is completed in the second vaporization separate section STEP3, at least a portion liquid phase L1 and at least a portion high-temperature gas V2 Few mixed once contacts and is separated into gas phase V3 and liquid phase L3, and the gasification of at least a portion residue fraction enters gas phase V3 in liquid phase L1 In, liquid phase L3 weight flow WL3 is less than liquid phase L1 weight flow WL1.

Because the vaporized component gas phase V3 of middle coalite tar cold oil is adapted as hydro-upgrading process raw material, because This, this method can be with coal tar fraction hydro-upgrading process formation group technology, in this group technology, the light residual oil of coal tar Component hydrogenating materials can be converted into hydrogenation wax oil component through deep hydrofinishing process, and hydrogenation wax oil component is hydrogenated cracked Journey can be converted into diesel oil and its more light component.This is the second object of the present invention.

Because residual oil L3 is lower compared with the light contents of components in oil residue in residual oil L1 and heavy resid constituent content is higher, residual oil L3 compared with Residual oil L1 softening point is higher.Simultaneously as residual oil L1 and/or L3 that coalite tar is obtained viscosity are generally larger in separation, It is more conducive to use as visbreaking residue after visbreaking step used as fuel oil then by reducing viscosity, and the second of the present invention Separate section STEP3 is vaporized, certain visbreaking effect can be provided simultaneously with.This is the third object of the present invention, i.e., with raising The effect of coal tar pitch softening point and the effect of a certain degree of visbreaking.

The method of the invention, is applicable not only to the processing of middle coalite tar, is equally applicable to the coal base oil containing heavy oil Such as high temperature coal-tar, the processing of coal direct liquefaction oil, the oil shale oil containing more solid particle such as ash content is also suitable for Processing.In the same way, the method for the invention applies also for the processing of the low hydrogen content miscella containing heavy oil, is also applied for containing weight The processing of the petroleum base crude oil of oil.Substantially, the present invention proposes the side that light oil is produced in a kind of hydrocarbon stream of self-contained heavy oil Method.

The method of the present invention, different from conventional petroleum base decompression residuum (higher than 540 DEG C hydrocarbon groups of major oil normal boiling point Into) visbreaking processing method, first point be raw material mode of heating it is different, second point is that the raw material boiling range of processing is different, the 3rd Point be the raw material of processing by thermal condensation coking property very different, the 4th point be process operating condition difference it is very big. In order to be advantageously implemented visbreaking reaction, petroleum base decompression residuum (major oil normal boiling point higher than 540 DEG C hydrocarbon composition) subtracts Viscous reaction is generally operated under an increased pressure, is unfavorable for deep vacuum distillation and is improved feedstock oil vaporization rate.

The method of the present invention, also different from conventional petroleum base reduced crude (higher than 360 DEG C hydrocarbon groups of major oil normal boiling point Into) raising wax oil (major oil normal boiling point be 360~540 DEG C hydrocarbon composition) extracting rate deep vacuum distillation method, first point is The mode of heating of raw material is different, and second point is that the raw material boiling range of processing is different, be thirdly processing raw material by thermal condensation knot Burnt property difference is very big.In addition, the better heat stability in order to suppress heat scission reaction and petroleum base reduced crude, petroleum base is normal Visbreaking reaction does not occur generally for the deep vacuum distillation process of pressure residual oil.

The method of the present invention, the feedstock oil heating vaporization flow existed also different from conventional delayed coking unit, delay The feedstock oil vaporization flow that coking plant is present includes：Feedstock oil heat exchange heating, connect with coke drum top gas in coking fractional distillation column Touch heating evaporation, contact evaporation oil (comprising the oily heavy constituent of coking raw material and the dignified component of top of coke tower air cooling) and enter coking heater Heating, coking heater outlet oil gas occur heavy constituent by coke drum and are condensed green coke and cracking generation small molecule oil gas, coke Tower overhead gas enter coking fractional distillation column in coking raw material oil separate section heat exchange, separate section recuperated gas enter coking The overall process of the rectifying section on the top of the contact separation section in fractionating column.In process of the present invention, heavy resid component is without too high The Furnace Production Process of temperature section, the maximum temperature of heavy resid component experience is far below the pyrogenetic reaction temperature of residue fraction (i.e. Far below Outlet Temperature in Delayed Coking Furnace), operating pressure is also compared with heavy resid component does not generate solid product i.e. coke therefore need not Coke drum.Even only comparing from Process flow, step of the present invention is also concise more.

The method of the invention has no report.

Therefore, the first object of the present invention is a kind of method for proposing to produce light oil in hydrocarbon stream of self-contained heavy oil.

The second object of the present invention is the side for proposing to produce light oil in a kind of low hydrogen content miscella of self-contained heavy oil Method.

The third object of the present invention is a kind of method for proposing to produce light oil in coal base oil of self-contained heavy oil, Ke Yishi Existing coal tar is particularly the depth vaporization (reducing coal tar asphalt yield) of middle coalite tar, so as to improve the receipts of vapo(u)rizing oil Rate, the cold oil of steam can produce clear gusoline by hydro-upgrading obtained by vaporescence.

The content of the invention

The method that light oil is produced in a kind of hydrocarbon stream of self-contained heavy oil of the present invention, it is characterised in that comprise the steps of：

Generally condensation gas phase V3 and/or vapour phase V12 of the invention obtains cold oil：

In vaporised hydrocarbon recycling step STEP4, vapour phase V3 from the second vaporization separate section STEP3 is condensed and/or from the One vaporization separate section STEP1 bypass vapor phase stream V12 obtains hydrocarbon ils HPF.

The present invention can form group technology with the hydro-upgrading process of gas phase V3 and/or vapour phase V12 cold oil：

In hydrogenation step STEP5, at least a portion hydrocarbon ils HPF hydrogenation oil product, institute are converted into by hydro-upgrading process HP The unifining process HT that hydro-upgrading process HP includes hydrocarbon ils HPF is stated, can also adding comprising separation unifining process HT The main hydrogenation by normal boiling point higher than the hydrofinishing wax oil HTVGO that 350 DEG C of hydrocarbon components are constituted that hydrogen generation oil HTP is obtained splits Change process HC.

Hydrocarbon feed F01 of the present invention, one or more that can be in following materials：

1. the high hydrocarbon ils of gluey pitch shape constituent content；

2. the high hydrocarbon ils of content of ashes；

3. the high hydrocarbon ils of easy coking constituent content；

4. the high hydrocarbon ils of the easy reactant content of high temperature.

1. oil product obtained by coalite tar or its distillate or its hot procedure；

2. oil product obtained by medium temperature coal tar or its distillate or its hot procedure；

3. oil product obtained by high temperature coal-tar or its distillate or its hot procedure；

4. oil product obtained by liquefied coal coil obtained by coal liquefaction or its distillate or its hot procedure；；

5. oil product obtained by shale oil or its distillate or its hot procedure；

6. oil product obtained by tar sand base heavy oil or its hot procedure；

7. ethylene cracking tar；

8. petroleum base wax oil thermal cracking tars；

9. heavy oil fraction product obtained by petroleum based heavy fuel oils hot procedure；

10. gluey pitch shape composition weight content of other aromatic hydrocarbons weight contents higher than 50% is higher than 15% hydrocarbon ils；

The hot procedure includes coking, catalytic cracking process, catalytic pyrolysis process, visbreaking process, thermal cracking Process.

The invention is particularly suited to the processing of middle coalite tar, its operation target is usually：

Normal boiling point is higher than in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of 500 DEG C of components is higher than 70%；

Separate section STEP3 is vaporized second, liquid phase L3 weight flow WL3 is less than liquid phase L1 weight flow WL1 extremely Few 5%.

The invention is particularly suited to the processing of middle coalite tar, it operates target to be generally：

Normal boiling point is higher than in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of 500 DEG C of components is higher than 85%；

Separate section STEP3 is vaporized second, liquid phase L3 weight flow WL3 is less than liquid phase L1 weight flow WL1 extremely Few 30%.

The invention is particularly suited to the processing of middle coalite tar, its operation target is preferably：

Normal boiling point is higher than in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of 500 DEG C of components is higher than 90%；

Separate section STEP3 is vaporized second, liquid phase L3 weight flow WL3 is less than liquid phase L1 weight flow WL1 extremely Few 50%.

The invention is particularly suited to the processing of middle coalite tar, its operating condition is usually：

Normal boiling point is higher than in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of 500 DEG C of components is higher than 70%, and the first flash temperature T1 is 340~390 DEG C；

In vapour phase heating part STEP2, second temperature T2 is 340~450 DEG C, is advisable with high-temperature gas V2 noncokings；

At least 20% quilt of component of the normal boiling point less than 540 DEG C in the second vaporization separate section STEP3, liquid phase L1 Vaporization；Liquid phase L3 temperature T31 is 340~440 DEG C, is advisable with liquid phase L3 noncokings.

The invention is particularly suited to the processing of middle coalite tar, its operating condition is generally：

Normal boiling point is higher than in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of 500 DEG C of components is higher than 85%, and the first flash temperature T1 is 350~380 DEG C；

In vapour phase heating part STEP2, second temperature T2 is 360~440 DEG C, is advisable with high-temperature gas V2 noncokings；

At least 50% quilt of component of the normal boiling point less than 540 DEG C in the second vaporization separate section STEP3, liquid phase L1 Vaporization；Liquid phase L3 temperature T31 is 360~430 DEG C, is advisable with liquid phase L3 noncokings.

The invention is particularly suited to the processing of middle coalite tar, its operating condition is preferably：

Normal boiling point is higher than in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of 500 DEG C of components is higher than 90%, and the first flash temperature T1 is 360~375 DEG C；

In vapour phase heating part STEP2, second temperature T2 is 380~430 DEG C, is advisable with high-temperature gas V2 noncokings；

At least 80% quilt of component of the normal boiling point less than 540 DEG C in the second vaporization separate section STEP3, liquid phase L1 Vaporization；Liquid phase L3 temperature T31 is 370~420 DEG C, is advisable with liquid phase L3 noncokings.

The invention is particularly suited to the processing of middle coalite tar, its detailed operating condition is usually：

Normal boiling point is higher than in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of 500 DEG C of components is higher than 90%, and the first flash temperature T1 is 355~375 DEG C, and the first separation process operating pressure is low In 0.2MPaA；

In vapour phase heating part STEP2, second temperature T2 is 380~440 DEG C, is advisable with high-temperature gas V2 noncokings；

At least 80% quilt of component of the normal boiling point less than 540 DEG C in the second vaporization separate section STEP3, liquid phase L1 Vaporization；Liquid phase L3 temperature T31 is 380~420 DEG C, is advisable with liquid phase L3 noncokings；Second vaporization separate section STEP3 behaviour Make pressure less than 0.15MPaA.

The invention is particularly suited to the processing of middle coalite tar, its detailed operating condition is generally：

Normal boiling point is higher than in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of 500 DEG C of components is higher than 90%, and the first flash temperature T1 is 355~375 DEG C, the first vaporizing section, the first separation Process operation pressure is less than 0.17MPaA；

At least 80% quilt of component of the normal boiling point less than 540 DEG C in the second vaporization separate section STEP3, liquid phase L1 Vaporization；Liquid phase L3 temperature T31 is 380~420 DEG C, is advisable with liquid phase L3 noncokings；Second vaporization separate section STEP3 behaviour Make pressure less than 0.10MPaA.

The invention is particularly suited to the processing of middle coalite tar, its detailed operating condition is preferably：

Normal boiling point is higher than in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of 500 DEG C of components is higher than 90%, and the first flash temperature T1 is 355~375 DEG C, and the first separation process operating pressure is low In 0.15MPaA；

At least 80% quilt of component of the normal boiling point less than 540 DEG C in the second vaporization separate section STEP3, liquid phase L1 Vaporization；Liquid phase L3 temperature T31 is 380~420 DEG C, is advisable with liquid phase L3 noncokings；Second vaporization separate section STEP3 behaviour Make pressure less than 0.08MPaA.

The invention is particularly suited to the processing of middle coalite tar, its detailed operating condition preferably is：

Normal boiling point is higher than in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of 500 DEG C of components is higher than 90%, and the first flash temperature T1 is 355~375 DEG C, and the first separation process operating pressure is low In 0.10MPaA；

At least 80% quilt of component of the normal boiling point less than 540 DEG C in the second vaporization separate section STEP3, liquid phase L1 Vaporization；Liquid phase L3 temperature T31 is 380~420 DEG C, is advisable with liquid phase L3 noncokings；Second vaporization separate section STEP3 behaviour Make pressure less than 0.05MPaA.

When hydrocarbon feed F01 is middle coalite tar, according to the difference of operating condition, the second vaporization separate section STEP3 institutes Obtained liquid phase L3 softening point range is very wide, liquid phase L3 softening point usually above 90 DEG C, be generally greater than 100 DEG C, especially Higher than 110 DEG C.

Separate section STEP3 is vaporized second, the fractionating column T3 used the first working method is：

Vaporize separate section STEP3 second, using fractionating column T3, it is more than fractionating column T3 high-temperature gas V2 charging apertures and Tower section below liquid phase L1 charging apertures separate more than section T3S1 tower section as contact separation section T3S1, gas phase V3 entrance T3S2, which is condensed, obtains cold oil.

Separate section STEP3 is vaporized second, the fractionating column T3 used second of working method is：

Vaporize separate section STEP3 second, using fractionating column T3, it is more than fractionating column T3 high-temperature gas V2 charging apertures and Tower section below liquid phase L1 charging apertures separate more than section T3S1 rectifying section as contact separation section T3S1, gas phase V3 entrance It is separated and obtains 2 or multiple distillates.

Separate section STEP3 is vaporized second, the fractionating column T3 used the third working method is：

Vaporize separate section STEP3 second, using fractionating column T3, it is more than fractionating column T3 high-temperature gas V2 charging apertures and Tower section below liquid phase L1 charging apertures is used as contact separation section T3S1；

The liquid phase L3 for separateing section T3S1 is left, the vapor stripping section of section T3S1 bottoms is separate by being arranged in Light residue fraction is deviate from T3S3 vacuum flashings, and fractionating column T3 bottom of towe is passed through stripped vapor.

Separate section STEP3 is vaporized second, the fractionating column T3 used the 4th kind of working method is：

Vaporize separate section STEP3 second, using fractionating column T3, it is more than fractionating column T3 high-temperature gas V2 charging apertures and Tower section below liquid phase L1 charging apertures is as contact separation section T3S1, the tower section T3S2 quilts that gas phase V3 enters more than contact separation section Condensation obtains cold oil；

Bypass vapor phase stream V12 from the first vaporization separate section STEP1 enters the second vaporization separate section STEP3, Enter fractionating column T3 from fractionating column T3 contact separation section T3S1 top tower section T3S2, contact the material from gas phase V3 and carry out Combined recovery.

Separate section STEP3 is vaporized second, the fractionating column T3 used the 5th kind of working method is：

Separate section STEP3 is vaporized second, section T3S1, at least a portion liquid phase L1 and at least a portion is being separate High-temperature gas V2 completes at least mixed once and contacts and be separated into gas phase V3；Gas phase V3 passes through washing section T3SX and circulating cleaning solution Body BLR counter current contactings；L points of the liquid B of washing section T3SX bottoms outflow is two parts, and Part I is recycled into washing section T3SX Top turns into circulating cleaning solution body BLR, and Part II enters contact separation section T3SY as liquid B LP and contacted with high-temperature gas V2 And complete gas-liquid separation；Liquids in general BLP weight flow BLPW and circulating cleaning solution body BLR weight flow BLRW ratio For K, K is 0.0005 to 0.01.

Separate section STEP3 is vaporized second, the fractionating column T3 used the 6th kind of working method is：

Separate section STEP3 is vaporized second, section T3S1, at least a portion liquid phase L1 and at least a portion is being separate High-temperature gas V2 completes at least mixed once and contacts and be separated into gas phase V3；Gas phase V3 passes through washing section T3SX and circulating cleaning solution Body BLR counter current contactings；L points of the liquid B of washing section T3SX bottoms outflow is two parts, and Part I is recycled into washing section T3SX Top turns into circulating cleaning solution body BLR, and Part II enters as liquid B LP separate section T3S1 and high-temperature gas V2 and liquid Phase L1 is contacted and is completed gas-liquid separation；Liquids in general BLP weight flow BLPW and circulating cleaning solution body BLR weight flow BLRW ratio is K, and K is 0.0005 to 0.01.

Embodiment

The present invention described in detail below.

Pressure of the present invention, refers to absolute pressure.

Concentration of component of the present invention, is weight concentration i.e. mass concentration when not specializing.

Conventional gas hydrocarbon of the present invention is referred under normal condition in gaseous hydro carbons, including methane, ethane, third Alkane, butane；Conventional liq hydrocarbon of the present invention refers to the hydro carbons being in a liquid state under normal condition, including pentane and its boiling point are more High hydro carbons；Impurity composition of the present invention refers to hydro-conversion thing such as water, ammonia, the vulcanization of non-hydrocarbon component in feedstock oil Hydrogen, hydrogen chloride etc..

In order to describe the problem, the present invention is (such as conventional to boil by conventional middle coalite tar heavy oil or residual oil or coal tar pitch Point is higher than 500 DEG C of coal tar fraction) be divided into light residue fraction and heavy resid component is treated, such as by normal boiling point be 500~ 540 DEG C of coal tar oil ingredient is referred to as the light residue fraction of coal tar, normal boiling point is higher than to 540 DEG C of coal tar oil ingredient referred to as coal tar Oily heavy resid component.Light residue fraction of the present invention and heavy resid component, are a kind of concepts relatively.

Coal base oil of the present invention, refers to the coal hot-working such as the dry distillation of coal or coking of coal or coal generating gas or DCL/Direct coal liquefaction The hydrocarbon ils from coal charge that journey is produced, including low temperature tar, middle temperature tar, high temperature tar, liquefied coal coil and its miscella.

Coal base heavy oil of the present invention, is referred to mainly by normal boiling point higher than evaporating that 500 DEG C of coal base oil component is constituted Divide than the coal tar pitch from coal tar as generally described, usually contain a large amount of macromolecular substances such as polycyclic aromatic hydrocarbon, colloid, asphalitine Deng its hydrogen content is relatively low, content of ashes is higher.

Coal base heavy oil component of the present invention, refers to hydrocarbon ils component of the normal boiling point higher than 500 DEG C in coal base oil, generally Containing a large amount of macromolecular substances such as polycyclic aromatic hydrocarbon, colloid, asphalitine etc., its hydrogen content is relatively low.

Coal tar of the present invention, is referred to from pyrolysis of coal or coking of coal or the dry distillation of coal or the pyrolysis of coal generating gas process step The coal tar of process or its cut such as rapid, can be accessory substance coalite tar or its cut or the coal refining of coal generating gas Coking coal pyrolytic process (including semicoke, middle temperature coking, high-temperature coking process) accessory substance coal tar or its cut, institute of the present invention State the miscella that coal tar can also be above-mentioned coal tar.Coal tar of the present invention, including low temperature tar, middle temperature tar, height Miscella, the distillate of coal tar of temperature tar, different coal tar.

High-temperature coking belongs to coal high temperature pyrolysis process, and the final temperature of pyrolytic process is generally higher than 900 DEG C, generally 1000 Between~1400 DEG C.The high temperature coal-tar refers to that coal high temperature pyrolysis produces the pair of coke and/or the production of town gas process Product crude tar oil.High temperature coal-tar generally produces following product in primary distillation process：Light oil (topping tar), carbolic oil, naphthalene The product such as oil, lightweight washing oil, heavy wash oil, lightweight carbolineum, heavy carbolineum, pitch, carbolic oil can be further separated into crude phenols and de- Carbolic oil, naphtalene oil can be further separated into thick naphthalene and de- naphtalene oil.High temperature coal-tar light fraction of the present invention is referred to：Carbolineum, wash Oil, naphtalene oil, de- naphtalene oil, carbolic oil, dephenolize oil, light oil and its miscella.

Because raw coal property and coking or gas-making process condition change within the specific limits, the property of coal tar is also one Determine change in scope.The process conditions and product requirement of coal tar primary distillation process also change within the specific limits, therefore coal tar The property of oily light fraction also changes within the specific limits.The property of coal tar light fraction, proportion is usually 0.92~1.25, conventional It is usually 120~460 DEG C that boiling point, which is generally 60~500 DEG C, usual tenor be 5~80PPm, sulfur content be 0.4~ 0.8%th, nitrogen content is that 0.6~1.4%, oxygen content is 0.4~9.0%, and usual water content is 0.2~5.0%, and carbon residue content leads to It is often 0.5~13%.

The olefin(e) centent height of usual coal tar light fraction, phenol content are high and contain the more group easily reacted under the conditions of mitigation Point, therefore, the pre- hydrogenation process of coal tar light fraction of the present invention, usually using hydrogenation protecting agent, olefins hydrogenation The single dose of agent, hydrogenation deoxidation agent, hydrogen desulfurization agent etc. or double agent or the tandem compound or mixed loading combination of multi-agent.Coal tar heavy fractioning Particularly coal tar pitch cut, its tenor is high, gum level is high, asphalt content is high, therefore, coal tar of the present invention The pre- hydrogenation process of heavy distillat, usually using the single dose of hydrogenation protecting agent, HDM agent, hydrogen desulfurization agent etc. or double agent or The tandem compound or mixed loading combination of multi-agent

The process of light oil is produced in self-contained residue fraction ZYC of the present invention hydrocarbon feed F0, is the general of broad sense Read, including at least hydrocarbon feed F0 heating evaporation separation process, generally comprise hydrocarbon feed F0 separated process, can also wrap Unifining process HT containing the light fraction from hydrocarbon feed F0, can also include unifining process HT hydrogenated oils Hydrocracking process of the HTY normal boiling point higher than 350 DEG C of components.

First vaporization separate section STEP1 of the present invention, including at least a pervaporation step, as needed, can be wrapped Containing multiple pervaporation steps, while multiple heating stepses can be included, heater, flash tank, fractionating column can be used.Institute of the present invention The first vaporization separate section STEP1 is stated, as needed, can complete to be dehydrated, take off light fraction (such as carbolic oil, naphtalene oil, carbolineum) times The distillate that business production needs.

Vapour phase heating part STEP2 of the present invention, generally sets gas-phase feed heating furnace STEP2F, and gas phase passes through boiler tube It is the radiation chamber or convection cell of heating furnace in pipe, outside boiler tube, heating furnace is usually using fuel gas or fuel oil.

According to the present invention, in vapour phase heating part STEP2, as needed only to a part of vapour phase V1 (vapour phases i.e. to be heated Logistics V11) it is heated to after second temperature T2 and obtains high temperature gas phase V2, the purpose is to vaporize separate section meeting first The liquid phase L1 that STEP1 is produced under conditions of the heat energy that the second vaporization separate section STEP3 contact heat-exchanging evaporation process needs, If vapour phase V1 flows have affluence, it is to avoid consumed caused by the superheated of rich part vapour phase V1 (bypassing vapor phase stream V12) And can occur the unfavorable results such as heat scission reaction.

According to the present invention, at least mixed once is completed in the second vaporization separate section STEP3, liquid phase L1 and high temperature gas phase V2 Contact and be separated into gas phase V3 and liquid phase L3, the mixing separate process, can be 1 time or 2 times or multiple, generally can be Separate or the separation of 2 counter current contactings or repeatedly counter current contacting separation for 1 time, can in contact flash vessel or contact flash column or Completed in the contact flash zone of fractionating column.The step of condensed vapor phases V12 and/or vapour phase V3, can be complete in special condensation process Into the tower section being located at more than contact flash zone that can also be in the fractionating column comprising contact flash zone or system completion.

Second vaporization separate section STEP3 of the present invention, including at least a pervaporation step, as needed, can be wrapped Containing 2 or multiple pervaporation steps, while multiple heating stepses can be included, heater, flash tank, fractionating column can be used.

The process of light oil is produced in the hydrocarbon feed F0 of self-contained heavy oil of the present invention, separate section is vaporized second The liquid phase L3 that STEP3 is obtained, according to its composition and property, can be processed further into following processes：

1. after asphalt moulding process, obtained shaping pitch is stacked, sale；Asphalt moulding process, be typically into In being formed in type groove with chain-driving, cooled down with water and wind；

2. pitch coking process, including batch coking process or continuous coking process or Flexicoking process, product are passed through Coking oil can be used as hydrogenation material, and product coke can be stacked, sell；

3. it is outer after being stored in liquid fuel within oil tank to sell；

4. it is outer after being stored after being reconciled with other fuel oil in liquid fuel within oil tank to sell；

5. by depth visbreaking process production visbreaker tar, product coking oil can be used as hydrogenation material；

6. after asphalt moulding process, obtained molding massive pitch loads in mixture the coke oven in high-temperature coking with coking coal Interior coking, stacks to generate coke, tar and gas, sells；

7. used as high softening-point coal tar pitch；

8. it is used as the raw material for producing needle coke or asphalt-based carbon fiber；

9. it is used as producing the binding agent of carbon materials and the raw material of electrode coke；

10. when liquid phase L3 is as the high material of the aromatic carbon degree rich in hydrocarbon matter, coking yield about 80% during its coking, split Solution gas about 20, oil product yield are as little as almost equal to zero, close with low-volatile coal property, nearby without suitable liquid It during material purposes, can also be used as the admixture of solid coal fuel, solve the problems, such as that it stores accumulation.

1. the high hydrocarbon ils of gluey pitch shape constituent content；

2. the high hydrocarbon ils of content of ashes；

3. the high hydrocarbon ils of easy coking constituent content；

4. the high hydrocarbon ils of the easy reactant content of high temperature.

5. oil product obtained by shale oil or its distillate or its hot procedure；

6. oil product obtained by tar sand base heavy oil or its hot procedure；

7. ethylene cracking tar；

8. petroleum base wax oil thermal cracking tars；

Compared with the method for the existing middle coalite tar directly heated containing residual oil, the invention has the advantages that：

1. the method vaporized using indirectly heat, is avoiding coal-tar residue oil ingredient in high temperature section heating process in heating furnace Under the premise of the problem of quick coking occurs in boiler tube, realize coal tar and be particularly the depth vaporization of middle coalite tar and (subtract Few coal tar asphalt yield), so as to improve the yield of vapo(u)rizing oil, the light residual oil economic value of coal tar can be significantly improved；

2. cold oil can produce cleansing oil by hydro-upgrading process obtained by the vaporized components based on middle coalite tar Product, therefore, this method can be with coal tar fraction hydro-upgrading formation group technologies, in the process, the light residual oil group of coal tar Lease making deep hydrofinishing process can be converted into hydrogenation wax oil component, and the hydrogenation hydrogenated cracking process of wax oil component can be converted For diesel oil and its more light component, the light residual oil economic value of coal tar can be further improved；

3. because the viscosity of residual oil L1 and/or L3 that coalite tar is obtained in separation are generally larger, used as fuel oil Then it is more conducive to use as visbreaking residue after the visbreaking step by reducing viscosity, and the second vaporization separate section of the present invention STEP3, is provided simultaneously with certain visbreaking effect, can improve coal tar heavy duty residual oil economic value；

4. the purification of coal tar heavy duty residual oil is realized, the softening point of coal tar pitch is improved, up to more than 90~110 DEG C, The coal tar pitch of coalite tar, is to produce needle coke and asphalt-based carbon fiber in the main high softening-point being made up of coal tar heavy duty residual oil Potential material, be also the binding agent of carbon materials and the potential material of electrode coke；In other words, the present invention is improved often simultaneously Advise boiling point and be higher than 540 DEG C for the value (being used as hydrogenating materials) and normal boiling point of 500~540 DEG C of the light residue fraction of coal tar The value of coal tar heavy duty residue fraction (production low viscosity residual oil makees high softening point bitumen)；Say in a sense, the present invention Liquid and " solid " have been separated into equivalent to coalite tar in handle；

5. the present invention can apply to the processes such as distillation, the distillation of oil of shale oil, to enter as a kind of common method One step improves distillate vaporization rate and improves the initial boiling point temperature of heavy oil.

Embodiment one

The middle coalite tar that coal semi-coke process is produced is shown in Table 2,500,000 tons/year of year processing capacity, number 7920 when year goes into operation, Quantity is 63132kg/h.In order to isolate light residue fraction to greatest extent, at the same by the asphalitine in coal tar, ash content, Grain thing concentrates on the blue or green thing of coal that high softening-point is obtained in heavy coal tar pitch, and using the present invention, operating procedure is as follows：

1. separate section STEP1 is vaporized first, the condition after raw material F01 heating is：380 DEG C of temperature, pressure 0.15MPaA, carries out the first separation process and is separated into vapour phase V1 (47578kg/h, account for the 75.4% of raw material F01) and comprising residual oil Weight of the normal boiling point higher than 500 DEG C of components in the liquid phase L1 (15554kg/h, account for the 24.6% of raw material F01) of component, liquid phase L1 Content is 47.7%, and the first flash temperature T1 is 380 DEG C, and the first separation process operating pressure is 0.15MPaA；

Separate section STEP1 is vaporized first, makes 84.3% of component of the normal boiling point less than 500 DEG C in coal tar raw material Enter in vapour phase V1, normal boiling point is less than 500 DEG C, the light residual oil group of coal tar that normal boiling point is 500~540 DEG C in vapour phase V1 Divide and the part by weight of coal tar heavy duty residue fraction of the normal boiling point higher than 540 DEG C is 98.62%, 0.98%, 0.04%；

2. in vapour phase heating part STEP2, vapour phase V1 is all heated to second temperature as first via vapour phase V11 High temperature gas phase V2 is obtained after T2；High temperature gas phase V2 operation temperature T2 is 430 DEG C, operating pressure is 0.10MPaA；In this condition Under, the basic noncokings of high temperature gas phase V2, the heating furnace continuous cycle of operation can ensure more than 1 year；Heating furnace is to first via vapour phase V11 The thermic load that temperature-rise period is provided is 1601KW；

3. separate section STEP3 is vaporized second, whole liquid phase L1 and whole high temperature gas phase V2 mixing is contacted and is separated For gas phase V3 and liquid phase L3, liquid phase L1 about 69.1% component (the mainly light residue fraction of coal tar) gasification enters gas phase V3 In, liquid phase L3 weight is 4799kg/h, accounts for about the 30.9% of liquid phase L1 weight 15554kg/h；Liquid phase L3 temperature T31 is 399 DEG C, at this temperature liquid phase L3 noncokings；Second vaporizing section operating pressure is 0.07MPaA；

Above-mentioned second vaporization separate section STEP3 is the Contact Evaporating section more than fractionating column T3 gas phase V2 charging apertures What T3S1 was carried out；Contact Evaporating section T3S1 sets 5~8 pieces of tower trays, or it is highly 2.5~3.0 meters to set effect identical Random packing layer；

Vapor stripping section T3S3 of the fluid body of flash zone by the setting of gas phase V2 charging apertures bottom is left further to subtract Oil L3SD, the stripped vapor operating condition that fractionating column T3 bottom of towe is passed through after being stripped after the light residue fraction of pressure flash distillation abjection For：410 DEG C of temperature, pressure 0.1MPaA, flow 486kg/h；Show vapor stripping section T3S3, liquid phase in stripping simulation calculating L3 16.9% component completes vaporization.Oil L3SD flow is 3986kg/h after stripping, accounts for coal tar raw material F01's 6.3%；

Space after the stripping of fractionating column T3 bottoms between oil L3SD storage areas DL1 and vapor stripping section T3S1, It is disposed with oil L3SD after cold scarce Posterior circle liquid phase L3SDC refluxing opening L3SDC-N, stripping and mixes reduction with circulation liquid phase L3SDC Turn into liquid phase L3SDCP after temperature, liquid phase L3SDCP discharges fractionating column T3 bottoms are cooled after pump pressurizes by heat exchanger Turn into cold logistics L3SDCP1 to about 180~200 DEG C, the cold logistics L3SDCP1 in part passes through reflux line, passes through refluxing opening L3SDC-N is mixed into liquid phase L3SDCP in fractionating column T3 bottoms as liquid phase L3SDCP and liquid phase L3SD and arranged from fractionating column T3 bottoms Go out, the cold logistics L3SDCP1 in part is used as liquid phase L3SDCP2 deasphalting forming steps；Liquid phase L3SDCP temperature control is 280 ~300 DEG C；

4. liquid phase L3SDCP2 enters asphalt moulding process, and obtained shaping pitch is stacked, sale；Asphalt moulding process, be In being formed in forming tank with chain-driving, cooled down with water and wind.

In this example, coal tar raw material F01 heavy bitumen yield is 6.3%, and coal tar raw material F01 total vaporization rate is 93.7%, remove 4.2% water vapour, coal tar raw material F01 vaporised fraction oil yield is 89.5%；According to anhydrous butt Coal tar is converted, and coal tar raw material F01 vaporised fraction oil yield is 93.4%, and remaining is it is obvious that realize the mesh of the present invention Mark.

Embodiment two

Based on embodiment one, in vaporised hydrocarbon recycling step STEP4, the vapour from the second vaporization separate section STEP3 is condensed Phase V3 obtains hydrocarbon ils HPF.

In hydrogenation step STEP5, hydrocarbon ils HPF hydrogenation oil product, the hydro-upgrading are converted into by hydro-upgrading process HP Process HP includes hydrocarbon ils HPF unifining process HT, and the hydrogenated oil HTP also comprising separation unifining process HT is obtained The main hydrofinishing wax oil HTVGO being made up of normal boiling point higher than 350 DEG C of hydrocarbon components hydrocracking process HC.

This example forms the group technology of middle coalite tar deep drawing and vapo(u)rizing oil hydro-upgrading process.

The coal tar property analysis data of table 2

Claims

1. the method for light oil is produced in a kind of hydrocarbon stream of self-contained heavy oil, it is characterised in that comprise the steps of：

Separate section STEP1 is vaporized first, the hydrocarbon feed F01 of the ZYC containing residue fraction comprising liquid and vapor capacity is separated into Gas V1 and liquid phase L1, the first vaporization separate section STEP1 operation temperatures are T1；At least a portion gas V1 is used as hot vapour to be added Phase logistics V11, it is understood that there may be remaining gas V1 be used as bypass vapor phase stream V12；

In vapour phase heating part STEP2, vapor phase stream V11 to be heated, which is heated to after second temperature T2, is used as high-temperature gas V2；

At least one is completed in the second vaporization separate section STEP3, at least a portion liquid phase L1 and at least a portion high-temperature gas V2 Secondary mixing, which contacts and is separated at least a portion residue fraction gasification in gas phase V3 and liquid phase L3, liquid phase L1, to be entered in gas phase V3, Liquid phase L3 weight flow WL3 is less than liquid phase L1 weight flow WL1.

2. according to the method described in claim 1, it is characterised in that：

In vaporised hydrocarbon recycling step STEP4, condense from the second vapour phase V3 for vaporizing separate section STEP3 and/or from the first vapour The bypass vapor phase stream V12 for changing separate section STEP1 obtains hydrocarbon ils HPF.

3. method according to claim 2, it is characterised in that：

In hydrogenation step STEP5, at least a portion hydrocarbon ils HPF is converted into hydrogenation oil product by hydro-upgrading process HP, described to add Hydrogen upgrading processes HP includes hydrocarbon ils HPF unifining process HT.

4. method according to claim 2, it is characterised in that：

In hydrogenation step STEP5, at least a portion hydrocarbon ils HPF is converted into hydrogenation oil product by hydro-upgrading process HP, described to add Hydrogen upgrading processes HP includes hydrocarbon ils HPF unifining process HT, also includes separation unifining process HT hydrogenated oil The main hydrocracking process by normal boiling point higher than the hydrofinishing wax oil HTVGO that 350 DEG C of hydrocarbon components are constituted that HTP is obtained HC。

5. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Hydrocarbon feed F01, the one or more in following materials：

1. the high hydrocarbon ils of gluey pitch shape constituent content；

2. the high hydrocarbon ils of content of ashes；

3. the high hydrocarbon ils of easy coking constituent content；

4. the high hydrocarbon ils of the easy reactant content of high temperature.

6. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Hydrocarbon feed F01, the one or more in following materials：

4. oil product obtained by liquefied coal coil obtained by coal liquefaction or its distillate or its hot procedure；

5. oil product obtained by shale oil or its distillate or its hot procedure；

6. oil product obtained by tar sand base heavy oil or its hot procedure；

7. ethylene cracking tar；

8. petroleum base wax oil thermal cracking tars；

7. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Normal boiling point is higher than 500 DEG C in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of component is higher than 70%；

Separate section STEP3 is vaporized second, liquid phase L3 weight flow WL3 is less than liquid phase L1 weight flow WL1 at least 5%.

8. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Normal boiling point is higher than 500 DEG C in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of component is higher than 85%；

Separate section STEP3 is vaporized second, liquid phase L3 weight flow WL3 is less than liquid phase L1 weight flow WL1 at least 30%.

9. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Normal boiling point is higher than 500 DEG C in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of component is higher than 90%；

Separate section STEP3 is vaporized second, liquid phase L3 weight flow WL3 is less than liquid phase L1 weight flow WL1 at least 50%.

10. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Normal boiling point is higher than 500 DEG C in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of component is higher than 70%, and the first flash temperature T1 is 340~390 DEG C；

In vapour phase heating part STEP2, second temperature T2 is 340~450 DEG C；

Vaporize separate section STEP3 second, component of the normal boiling point in liquid phase L1 less than 540 DEG C at least 20% by vapour Change；Liquid phase L3 temperature T31 is 340~440 DEG C.

11. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Normal boiling point is higher than 500 DEG C in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of component is higher than 85%, and the first flash temperature T1 is 350~380 DEG C；

In vapour phase heating part STEP2, second temperature T2 is 360~440 DEG C；

Vaporize separate section STEP3 second, component of the normal boiling point in liquid phase L1 less than 540 DEG C at least 50% by vapour Change；Liquid phase L3 temperature T31 is 360~430 DEG C.

12. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Normal boiling point is higher than 500 DEG C in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of component is higher than 90%, and the first flash temperature T1 is 360~375 DEG C；

In vapour phase heating part STEP2, second temperature T2 is 380~430 DEG C；

Vaporize separate section STEP3 second, component of the normal boiling point in liquid phase L1 less than 540 DEG C at least 80% by vapour Change；Liquid phase L3 temperature T31 is 370~420 DEG C.

13. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Normal boiling point is higher than 500 DEG C in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of component is higher than 90%, and the first flash temperature T1 is 355~375 DEG C, and the first separation process operating pressure is less than 0.2MPaA；

In vapour phase heating part STEP2, second temperature T2 is 380~440 DEG C；

Vaporize separate section STEP3 second, component of the normal boiling point in liquid phase L1 less than 540 DEG C at least 80% by vapour Change；Liquid phase L3 temperature T31 is 380~420 DEG C；Second vaporization separate section STEP3 operating pressure is less than 0.15MPaA.

14. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Normal boiling point is higher than 500 DEG C in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of component is higher than 90%, and the first flash temperature T1 is 355~375 DEG C, the first vaporizing section, the first separation process behaviour Make pressure less than 0.17MPaA；

In vapour phase heating part STEP2, second temperature T2 is 380~440 DEG C；

Vaporize separate section STEP3 second, component of the normal boiling point in liquid phase L1 less than 540 DEG C at least 80% by vapour Change；Liquid phase L3 temperature T31 is 380~420 DEG C；Second vaporization separate section STEP3 operating pressure is less than 0.10MPaA.

15. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Normal boiling point is higher than 500 DEG C in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of component is higher than 90%, and the first flash temperature T1 is 355~375 DEG C, and the first separation process operating pressure is less than 0.15MPaA；

In vapour phase heating part STEP2, second temperature T2 is 380~440 DEG C；

Vaporize separate section STEP3 second, component of the normal boiling point in liquid phase L1 less than 540 DEG C at least 80% by vapour Change；Liquid phase L3 temperature T31 is 380~420 DEG C；Second vaporization separate section STEP3 operating pressure is less than 0.08MPaA.

16. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Normal boiling point is higher than 500 DEG C in the first vaporization separate section STEP1, hydrocarbon feed F01 is middle coalite tar, liquid phase L1 The weight content of component is higher than 90%, and the first flash temperature T1 is 355~375 DEG C, and the first separation process operating pressure is less than 0.10MPaA；

In vapour phase heating part STEP2, second temperature T2 is 380~440 DEG C；

Vaporize separate section STEP3 second, component of the normal boiling point in liquid phase L1 less than 540 DEG C at least 80% by vapour Change；Liquid phase L3 temperature T31 is 380~420 DEG C；Second vaporization separate section STEP3 operating pressure is less than 0.05MPaA.

17. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

The softening point that hydrocarbon feed F01 is the liquid phase L3 obtained by middle coalite tar, the second vaporization separate section STEP3 is higher than 90 ℃。

18. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

The softening point that hydrocarbon feed F01 is the liquid phase L3 obtained by middle coalite tar, the second vaporization separate section STEP3 is higher than 100℃。

19. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

The softening point that hydrocarbon feed F01 is the liquid phase L3 obtained by middle coalite tar, the second vaporization separate section STEP3 is higher than 110℃。

20. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Separate section STEP3 is vaporized second, using fractionating column T3, more than fractionating column T3 high-temperature gas V2 charging apertures and liquid phase Tower section below L1 charging apertures separate more than section T3S1 tower section T3S2 quilts as contact separation section T3S1, gas phase V3 entrance Condensation obtains cold oil.

21. method according to claim 20, it is characterised in that：

Separate section STEP3 is vaporized second, using fractionating column T3, more than fractionating column T3 high-temperature gas V2 charging apertures and liquid phase Tower section below L1 charging apertures is divided as section T3S1, the rectifying section that gas phase V3 enters contact separation more than section T3S1 is separate From obtaining 2 or multiple distillates.

22. method according to claim 20, it is characterised in that：

The liquid phase L3 for separateing section T3S1 is left, the vapor stripping section T3S3 of section T3S1 bottoms is separate by being arranged in Light residue fraction is deviate from vacuum flashing, and fractionating column T3 bottom of towe is passed through stripped vapor.

23. the method according to claim 1 or 2 or 3 or 4, it is characterised in that：

Separate section STEP3 is vaporized second, using fractionating column T3, more than fractionating column T3 high-temperature gas V2 charging apertures and liquid phase Tower section below L1 charging apertures enters the tower section T3S2 separateing more than section and is condensed as section T3S1, gas phase V3 is separate Obtain cold oil；

Bypass vapor phase stream V12 from the first vaporization separate section STEP1 enters the second vaporization separate section STEP3, divides certainly The top tower section T3S2 for evaporating tower T3 contact separation section T3S1 enters fractionating column T3, and material of the contact from gas phase V3 is combined Reclaim.

24. method according to claim 20, it is characterised in that：

Separate section STEP3 is vaporized second, section T3S1, at least a portion liquid phase L1 and at least a portion high temperature is being separate Gas V2 completes at least mixed once and contacts and be separated into gas phase V3；Gas phase V3 passes through washing section T3SX and circulating cleaning solution body BLR counter current contactings；L points of the liquid B of washing section T3SX bottoms outflow is two parts, and Part I is recycled on washing section T3SX Portion turns into circulating cleaning solution body BLR, and Part II enters contact separation section T3SY as liquid B LP and contacted simultaneously with high-temperature gas V2 Complete gas-liquid separation.

25. method according to claim 20, it is characterised in that：

Separate section STEP3 is vaporized second, section T3S1, at least a portion liquid phase L1 and at least a portion high temperature is being separate Gas V2 completes at least mixed once and contacts and be separated into gas phase V3；Gas phase V3 passes through washing section T3SX and circulating cleaning solution body BLR counter current contactings；L points of the liquid B of washing section T3SX bottoms outflow is two parts, and Part I is recycled on washing section T3SX Portion turns into circulating cleaning solution body BLR, and Part II enters as liquid B LP separate section T3S1 and high-temperature gas V2 and liquid phase L1 is contacted and is completed gas-liquid separation.

26. method according to claim 25, it is characterised in that：

Separate section STEP3 is vaporized second, in washing section T3SX, liquid B LP weight flow BLPW and circulating cleaning solution body BLR weight flow BLRW ratio is K, and K is 0.0005 to 0.01.