CN104498076A

CN104498076A - Method for preparing light oil from heavy oil-containing hydrocarbon material flow

Info

Publication number: CN104498076A
Application number: CN201410645835.2A
Authority: CN
Inventors: 何巨堂
Original assignee: 何巨堂
Current assignee: Luoyang Rui Hua new energy technology development Co., Ltd.
Priority date: 2014-11-06
Filing date: 2014-11-06
Publication date: 2015-04-08
Anticipated expiration: 2034-11-06
Also published as: CN104498076B

Abstract

The invention relates to a method for preparing light oil from heavy oil-containing hydrocarbon material flow, and is suitable for processing medium and low temperature coal tar, deep vaporization of residue fraction can be realized by employing an indirect heating mode, the highest temperature during a heating process is reduced for inhibiting a thermal condensation reaction; in a first vaporization separation part, a hydrocarbon raw material F01 containing vapor phase, liquid phase and residue fraction ZYC is separated to a vapor phase V1 and a liquid phase L1; at least a part of vapor phase V1 taken as a vapor phase material flow V11 to be heated for heating the vapor phase heating part to obtain high temperature gas V2; in a second vaporization separation part, at least a part of liquid phase L1 and at least a part of high temperature gas phase V2 are mixed and contacted, and then separated to gas phase V3 and liquid phase L3, at least a part of residue fraction in the liquid phase L1 is introduced in the gas phase V3 for completing deep vaporization of the liquid phase L1; and the gas phase V3 is condensed to obtain oil product, and then the oil product can pass through a hydrogenation process to prepare clean oil products.

Description

The method of lightweight oil is produced in a kind of hydrocarbon stream of self-contained heavy oil

Technical field

The present invention relates to a kind of method producing lightweight oil in hydrocarbon stream of self-contained heavy oil; Particularly the present invention relates to a kind of method producing lightweight oil in low hydrogen content mixing oil of self-contained heavy oil component; More particularly the present invention relates to a kind of method producing lightweight oil in coal-based oil of self-contained heavy oil component, be suitable for the processing of middle coalite tar, adopt indirect heating manner to realize degree of depth vaporization (namely reduce coal-tar pitch yield) of residue fraction and the top temperature reducing its heat-processed suppresses thermal condensation reaction, the cold oil of degree of depth vaporization gained steam can produce clear gusoline through hydro-upgrading.

Background technology

In order to describe the problem, coalite tar heavy oil in routine or residual oil or the coal-tar pitch coal tar fraction of 500 DEG C (the such as normal boiling point higher than) are divided into light residue fraction and heavy resid component to treat by the present invention, are such as that the coal tar component of 500 ~ 540 DEG C is called the light residue fraction of coal tar, normal boiling point is called coal tar heavy duty residue fraction higher than the coal tar component of 540 DEG C by normal boiling point.Therefore, middle coalite tar degree of depth vaporization question essence of the present invention is exactly light for coal tar in conventional coal tar residue fraction vaporization is separated the problem of deviating from, namely improves coal tar heavy duty residue fraction purity simultaneously or improve the problem of its softening temperature.

The blue charcoal process of the dry distillation of coal process of coalite tar such as coal system in current generation, the coal tar residual oil of coalite tar product all containing some amount in the gained coal tar fraction of 500 DEG C (the such as normal boiling point higher than).It is high that coal tar residual oil possesses boiling point, resin and asphalt content is high, to be heated the feature of very easily condensation coking, at the fractionation process of routine, in order to avoid the heating upper limit value that Pintsch process exists, even adopt comprehensive technical measure such as to adopt charging process furnace, stripped vapor is injected in heating furnace tube, underpressure distillation reduces working pressure, the multiple means such as reduced steam are used below vacuum distillation tower opening for feed, the target of the light residue oil fraction of deep drawing (such as normal boiling point is the coal-tar residue oil distillate of 500 ~ 540 DEG C) in coal-tar residue oil distillate can not be realized, when coal tar heavy oil remaining carbon lower (namely potential hydrogenation material ratio of component wherein such as normal boiling point is that the coal tar fraction of 500 ~ 540 DEG C is more) is forced to such as enter the hot procedures such as delayed coking process as coal-tar residue oil treatment, the in poor quality defining resource utilizes.For the coal tar heavy oil of low residual carbon content, the problems referred to above form great financial loss.And there is no the distillation separation method solving this problem at present.

In producing with 500,000 tons/year of blue charcoal devices, coalite tar is processed as example, the normal boiling point that in fractionation 500,000 tons/year, coalite tar can obtain about 10 ~ 15% 5.0 ~ 7.5 ten thousand tons/year is higher than the coal tar heavy oil of 500 DEG C, the normal boiling point that this coal tar heavy oil contains 50 ~ 70% is 500 ~ 540 DEG C of coal tar fractions, even if even if isolate half also have 2.5 ~ 3.75 ten thousand tons/year by 50% its quantity of calculating, if be separated successfully, benefit is also huge.

In order to improve the extracting rate of the light residue fraction of coal tar, the thermal condensation coking of coal tar residual oil is not considered iff considering distillation principle, the target realizing deep drawing lighter fraction in coal tar heavy fractioning (such as normal boiling point is the coal tar fraction of 500 ~ 540 DEG C) is possible, and table 1 lists the lower boiling point data for analytical of hydro carbons decompression and uses.

Table 1 hydro carbons atmospheric boiling point and decompression boiling point convert, unit DEG C

Residual oil due to middle coalite tar has the temperature-sensitive feature of easy coking, under the precondition ensureing the long running cycle, the heating and separating method that conventional direct heating comprises the heavy oil of middle coalite tar or the coal tar of residual oil is difficult to realize the degree of depth vaporization target of middle coalite tar of the present invention.

Below describe the charging process furnace of coalite tar separation column in existing full cut, the fractionating column system of coalite tar in full cut, coal tar is separated into tower ground coal pitch and removes the lighting end of coal-tar pitch.

According to northern Shensi Shenmu County, the hot-work experiment of Fugu one with coalite tar in the full cut of typical case, under normal pressure, large about 425 ~ 440 DEG C, there is first fast pyrolysis generation condenses and discharge a large amount of gas simultaneously in middle coalite tar, the inwall of partial condensate attachment container, therefore in must strictly controlling, the heating furnace tube the highest inner wall temperature TH of coalite tar is lower than a certain prescribed value such as 425 DEG C, in full scale plant operation usually the highest inner wall temperature TH of regulation heating furnace tube lower than 410 DEG C with the safety temperature distance retaining 15 DEG C, like this top temperature of coalite tar in the heating furnace tube of non-coking by the thermal conductivity had by the thickness of heating-furnace inside pipe wall oil film retention layer and oil film composition determine.Such as, it is 0.10MPa that separation column requires coil outlet ambient condition to be absolute pressure, temperature is 360 DEG C, the temperature difference of such boiler tube inwall oil film retention layer can only be less than 50 DEG C, and that is even or the thinner and temperature difference that is oil film everywhere of boiler tube inwall oil film retention layer is all less than 50 DEG C of ability and meets safety in production and can not coking.If the temperature difference of boiler tube inwall oil film retention layer is greater than 50 DEG C, can only be then compensate by reducing working pressure or reducing service temperature, because industrial reduction working pressure exists lower limit, but so can only be compensate cause the rising of coal-tar pitch productive rate and the reduction of lighting end yield by reducing service temperature usually.

For the charging process furnace of coalite tar separation column in full cut, medium in boiler tube has two major features: first be comprise a large amount of easily condensation or easily coking component as alkene, phenols, condensed-nuclei aromatics, gum asphalt, a large amount of condenses can be produced after exceeding safe limiting temperature and be attached to boiler tube internal surface; Second is that the boiling range of coalite tar in full cut is wide and thermal condensation speed that the is higher component of boiling point is faster, the concentration process of the temperature-rise period of middle coalite tar to be the evaporative process of low viscosity light constituent be also liquid phase gluey pitch shape component, the liquid phase also just saying in the process fluid of the outlet section of close boiler tube is the high density liquid phase of the easy condensation gum asphalt of high viscosity.The charging process furnace of coalite tar separation column in existing industrialized full cut, there is the easy coking of boiler tube, operational cycle short problem in great majority, within about 3 ~ 4 months, coke cleaning is just needed namely to burn, or adopt the method changing coking boiler tube to shorten the coke cleaning time, therefore, delay coking, prolong operation cycle has significant industrial value.

In order to realize improving light vaporization rate of residual oil this purpose, the present invention proposes a kind ofly to avoid the direct-fired method of the residual oil of centering coalite tar, direct-fired component is the component and the distillate steam that are relatively difficult to coking in middle coalite tar, then completed heat vaporized by contact heat-exchanging, namely the component of the easiest relative coking in centering coalite tar and the method for residue fraction employing indirect heating vaporization reduce the top temperature suppression thermal condensation reaction of residue fraction heat-processed, and its process imagine is:

At the first vaporization separate part STEP1, the hydrocarbon feed F01 containing residue fraction ZYC comprising liquid and vapor capacity is separated into gas V1 and liquid phase L1, the first vaporization separate part STEP1 service temperature is T1; Gas V1 is as vapor phase stream V11 to be heated at least partially, and the residue gas V1 that may exist is as bypass vapor phase stream V12;

High-temperature gas V2 is used as after vapour phase hot spots STEP2, vapor phase stream V11 to be heated are heated to the second temperature T2;

At the second vaporization separate part STEP3, liquid phase L1 and high-temperature gas V2 at least partially complete mixing at least one times and contact and be separated into gas phase V3 and liquid phase L3 at least partially, in liquid phase L1, residue fraction gasification enters in gas phase V3 at least partially, and the weight rate WL3 of liquid phase L3 is less than the weight rate WL1 of liquid phase L1.

Cold oil due to the vaporized component gas phase V3 of middle coalite tar is suitable for as hydro-upgrading process raw material, therefore, present method can form combination process with coal tar fraction hydro-upgrading process, in this combination process, the light residue fraction hydrogenating materials of coal tar can be converted into hydrogenation wax oil component through deep hydrofinishing process, and hydrogenation wax oil component can be converted into diesel oil and more light constituent thereof through hydrocracking process.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, heavy resid component concentration is higher, and residual oil L3 is higher compared with the softening temperature of residual oil L1.Simultaneously, due to the residual oil L1 that obtains of coalite tar in being separated and or the viscosity of L3 usually larger, if be used as oil fuel, be more conducive to use by becoming visbreaking residue after falling low viscous visbreaking step, and the second vaporization separate part STEP3 of the present invention, certain visbreaking effect can be possessed simultaneously.This is the third object of the present invention, namely has the effect and visbreaking effect to a certain degree that improve coal tar pitch soften point.

The method of the invention, is not only applicable to the processing of middle coalite tar, is equally applicable to coal-based oil containing heavy oil as the processing of coal-tar heavy oil, coal direct liquefaction oil, is suitable for containing the processing of more solid particulate as the oil shale oil of ash content yet.In the same way, the method for the invention is also applicable to the processing of the low hydrogen content mixing oil containing heavy oil, is also applicable to the processing of the petroleum base crude oil containing heavy oil.In fact, the present invention proposes a kind of method producing lightweight oil in hydrocarbon stream of self-contained heavy oil.

Method of the present invention, be different from the visbreaking working method of conventional petroleum base vacuum residuum (major oil normal boiling point forms higher than 540 DEG C of hydrocarbon), first is that the type of heating of raw material is different, second point is that the raw material boiling range of processing is different, be thirdly the raw material of processing by thermal condensation coking property very different, the 4th be the operational condition difference of the course of processing greatly.In order to be conducive to realizing viscosity breaking reaction, the visbreaking reaction of petroleum base vacuum residuum (major oil normal boiling point forms higher than 540 DEG C of hydrocarbon) operates usually under an increased pressure, is unfavorable for that deep vacuum distillation improves stock oil vaporization rate.

Method of the present invention, also the deep vacuum distillation method of raising wax oil (major oil normal boiling point is 360 ~ 540 DEG C of hydrocarbon compositions) extracting rate of conventional petroleum base long residuum (major oil normal boiling point forms higher than 360 DEG C of hydrocarbon) is different from, first is that the type of heating of raw material is different, second point is that the raw material boiling range of processing is different, be thirdly the raw material of processing by thermal condensation coking property very different.In addition, in order to suppress the better heat stability of heat scission reaction and petroleum base long residuum, there is not visbreaking reaction in the deep vacuum distillation process of petroleum base long residuum usually.

Method of the present invention, also the stock oil intensification vaporization flow process that conventional delayed coking unit exists is different from, the stock oil vaporization flow process that delayed coking unit exists comprises: stock oil heat exchange heats up, contact to heat up with coke drum top gas in coking fractional distillation column and evaporate, contact evaporation oil (comprising coking raw material oil heavy constituent and the dignified component of top of coke tower air cooling) enters coking heater heating, coking heater outlet oil gas generates small molecules oil gas by coke drum generation heavy constituent condensation green coke and cracking, coke drum top gas enters in coking fractional distillation column and is separateing section heat exchange with coking raw material oil, separate the overall process that section recuperated gas enters the rectifying section on the top of the contact separation section in coking fractional distillation column.In process of the present invention, heavy resid component is without the Furnace Production Process of high temperature section, the top temperature that heavy resid component experiences is far below the pyrogenic reaction temperature (namely far below Outlet Temperature in Delayed Coking Furnace) of residue fraction, comparatively, heavy resid component does not generate solid phase prod and coke therefore does not need coke drum working pressure yet.Even only compare from Process flow, step of the present invention is also simple and clear many.

The method of the invention has no report.

Therefore, the first object of the present invention is to propose a kind of method producing lightweight oil in hydrocarbon stream of self-contained heavy oil.

The second object of the present invention is to propose a kind of method producing lightweight oil in low hydrogen content mixing oil of self-contained heavy oil.

The third object of the present invention is to propose a kind of method producing lightweight oil in coal-based oil of self-contained heavy oil, can realize coal tar particularly in degree of depth vaporization (namely reduce coal-tar pitch yield) of coalite tar, thus improving the yield of vaporizing oil, the cold oil of vaporescence gained steam can produce clear gusoline through hydro-upgrading.

Summary of the invention

Produce the method for lightweight oil in the hydrocarbon stream of a kind of self-contained heavy oil of the present invention, it is characterized in that comprising following steps:

The usual condensation gas phase V3 of the present invention and or vapour phase V12 obtain cold oil:

At vaporised hydrocarbon recycling step STEP4, condensation from the second vaporization separate part STEP3 vapour phase V3 and or bypass vapor phase stream V12 from the first vaporization separate part STEP1 obtain hydrocarbon ils HPF.

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

At hydrogenation step STEP5, hydrocarbon ils HPF is converted into hydrogenation oil product through hydro-upgrading process HP at least partially, described hydro-upgrading process HP comprises the unifining process HT of hydrocarbon ils HPF, the hydrocracking process HC of the hydrofining wax oil HTVGO formed higher than 350 DEG C of hydrocarbon components primarily of normal boiling point that can also comprise that the hydrogenated oil HTP that is separated unifining process HT obtains.

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

1. the hydrocarbon ils that gluey pitch shape component concentration is high;

2. the hydrocarbon ils that ash oontent is high;

3. the hydrocarbon ils that easily coking component concentration is high;

4. the hydrocarbon ils that high temperature easy reactant content is high.

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

2. coal-tar middle oil or its distillate or its hot procedure gained oil product;

3. coal-tar heavy oil or its distillate or its hot procedure gained oil product;

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

5. shale oil or its distillate or its hot procedure gained oil product;

6. tar sand basic weight oil or its hot procedure gained oil product;

7. ethylene cracking tar;

8. petroleum base wax oil thermal cracking tars;

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

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

Described hot procedure comprises coking, catalytic cracking process, catalytic pyrolysis process, visbreaking process, thermal cracking process.

The present invention is particularly suitable for the processing of middle coalite tar, and its Action Target is generally:

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

At the second vaporization separate part STEP3, the weight rate WL3 of liquid phase L3 is less than the weight rate WL1 at least 5% of liquid phase L1.

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

At the second vaporization separate part STEP3, the weight rate WL3 of liquid phase L3 is less than the weight rate WL1 at least 30% of liquid phase L1.

The present invention is particularly suitable for the processing of middle coalite tar, and its Action Target is preferably:

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

At the second vaporization separate part STEP3, the weight rate WL3 of liquid phase L3 is less than the weight rate WL1 at least 50% of liquid phase L1.

The present invention is particularly suitable for the processing of middle coalite tar, and its operational condition is generally:

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

Be 340 ~ 450 DEG C at vapour phase hot spots STEP2, the second temperature T2, be advisable with high-temperature gas V2 noncoking;

At the second vaporization separate part STEP3, the normal boiling point in liquid phase L1 is vaporized lower than at least 20% of the component of 540 DEG C; The temperature T31 of liquid phase L3 is 340 ~ 440 DEG C, is advisable with liquid phase L3 noncoking.

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

Be 360 ~ 440 DEG C at vapour phase hot spots STEP2, the second temperature T2, be advisable with high-temperature gas V2 noncoking;

At the second vaporization separate part STEP3, the normal boiling point in liquid phase L1 is vaporized lower than at least 50% of the component of 540 DEG C; The temperature T31 of liquid phase L3 is 360 ~ 430 DEG C, is advisable with liquid phase L3 noncoking.

The present invention is particularly suitable for the processing of middle coalite tar, and its operational condition is preferably:

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

Be 380 ~ 430 DEG C at vapour phase hot spots STEP2, the second temperature T2, be advisable with high-temperature gas V2 noncoking;

At the second vaporization separate part STEP3, the normal boiling point in liquid phase L1 is vaporized lower than at least 80% of the component of 540 DEG C; The temperature T31 of liquid phase L3 is 370 ~ 420 DEG C, is advisable with liquid phase L3 noncoking.

The present invention is particularly suitable for the processing of middle coalite tar, and its detailed operational condition is generally:

At the first vaporization separate part STEP1, hydrocarbon feed F01 is middle coalite tar, and in liquid phase L1, normal boiling point is higher than the weight content of 500 DEG C of components higher than 90%, and the first flash vaporization point T1 is 355 ~ 375 DEG C, and the first sepn process working pressure is lower than 0.2MPaA;

Be 380 ~ 440 DEG C at vapour phase hot spots STEP2, the second temperature T2, be advisable with high-temperature gas V2 noncoking;

At the second vaporization separate part STEP3, the normal boiling point in liquid phase L1 is vaporized lower than at least 80% of the component of 540 DEG C; The temperature T31 of liquid phase L3 is 380 ~ 420 DEG C, is advisable with liquid phase L3 noncoking; The working pressure of the second vaporization separate part STEP3 is lower than 0.15MPaA.

At the first vaporization separate part STEP1, hydrocarbon feed F01 is middle coalite tar, and in liquid phase L1, normal boiling point is higher than the weight content of 500 DEG C of components higher than 90%, and the first flash vaporization point T1 is 355 ~ 375 DEG C, first vaporizing section, the first sepn process working pressure is lower than 0.17MPaA;

At the second vaporization separate part STEP3, the normal boiling point in liquid phase L1 is vaporized lower than at least 80% of the component of 540 DEG C; The temperature T31 of liquid phase L3 is 380 ~ 420 DEG C, is advisable with liquid phase L3 noncoking; The working pressure of the second vaporization separate part STEP3 is lower than 0.10MPaA.

The present invention is particularly suitable for the processing of middle coalite tar, and its detailed operational condition is preferably:

At the first vaporization separate part STEP1, hydrocarbon feed F01 is middle coalite tar, and in liquid phase L1, normal boiling point is higher than the weight content of 500 DEG C of components higher than 90%, and the first flash vaporization point T1 is 355 ~ 375 DEG C, and the first sepn process working pressure is lower than 0.15MPaA;

At the second vaporization separate part STEP3, the normal boiling point in liquid phase L1 is vaporized lower than at least 80% of the component of 540 DEG C; The temperature T31 of liquid phase L3 is 380 ~ 420 DEG C, is advisable with liquid phase L3 noncoking; The working pressure of the second vaporization separate part STEP3 is lower than 0.08MPaA.

The present invention is particularly suitable for the processing of middle coalite tar, and its detailed operational condition preferably is:

At the first vaporization separate part STEP1, hydrocarbon feed F01 is middle coalite tar, and in liquid phase L1, normal boiling point is higher than the weight content of 500 DEG C of components higher than 90%, and the first flash vaporization point T1 is 355 ~ 375 DEG C, and the first sepn process working pressure is lower than 0.10MPaA;

At the second vaporization separate part STEP3, the normal boiling point in liquid phase L1 is vaporized lower than at least 80% of the component of 540 DEG C; The temperature T31 of liquid phase L3 is 380 ~ 420 DEG C, is advisable with liquid phase L3 noncoking; The working pressure of the second vaporization separate part STEP3 is lower than 0.05MPaA.

When hydrocarbon feed F01 is middle coalite tar, according to the difference of operational condition, the softening point range of the liquid phase L3 that the second vaporization separate part STEP3 obtains is very wide, the softening temperature of liquid phase L3 usually above 90 DEG C, generally higher than 100 DEG C, especially higher than 110 DEG C.

At the second vaporization separate part STEP3, the first mode of operation of the separation column T3 of use is:

At the second vaporization separate part STEP3, use separation column T3, tower section more than the high-temperature gas V2 opening for feed of separation column T3 and below liquid phase L1 opening for feed enters and separate the tower section T3S2 of more than section T3S1 as separateing section T3S1, gas phase V3 and be condensed and obtain cold oil.

At the second vaporization separate part STEP3, the second mode of operation of the separation column T3 of use is:

At the second vaporization separate part STEP3, use separation column T3, tower section more than the high-temperature gas V2 opening for feed of separation column T3 and below liquid phase L1 opening for feed enters separate that the rectifying section of more than section T3S1 is separated obtains 2 or multiple distillate as separateing section T3S1, gas phase V3.

At the second vaporization separate part STEP3, the third mode of operation of the separation column T3 of use is:

At the second vaporization separate part STEP3, use separation column T3, the tower section more than the high-temperature gas V2 opening for feed of separation column T3 and below liquid phase L1 opening for feed is as contact separation section T3S1;

Leave the liquid phase L3 separateing section T3S1, deviating from light residue fraction through being arranged in the water vapour stripping stage T3S3 vacuum flashing separateing section T3S1 bottom, at the bottom of separation column T3 tower, passing into stripped vapor.

At the second vaporization separate part STEP3, the 4th kind of mode of operation of the separation column T3 of use is:

At the second vaporization separate part STEP3, use separation column T3, tower section more than the high-temperature gas V2 opening for feed of separation column T3 and below liquid phase L1 opening for feed enters the tower section T3S2 separate more than section and is condensed as separateing section T3S1, gas phase V3 and obtains cold oil;

Bypass vapor phase stream V12 from the first vaporization separate part STEP1 enters the second vaporization separate part STEP3, and enter separation column T3 from the upper column section T3S2 of the contact separation section T3S1 of separation column T3, the material contacted from gas phase V3 carries out combined recovery.

At the second vaporization separate part STEP3, the 5th kind of mode of operation of the separation column T3 of use is:

At the second vaporization separate part STEP3, at contact separation section T3S1, at least partially liquid phase L1 and at least partially high-temperature gas V2 complete to mix at least one times and contact and be separated into gas phase V3; Gas phase V3 is by washing section T3SX and circulation cleaning liquid BLR counter current contact; The liquid B L that washing section T3SX bottom is flowed out is divided into two portions, and first part's circulation enters washing section T3SX top and becomes circulation cleaning liquid BLR, and second section enters as liquid B LP and separate section T3SY and to contact with high-temperature gas V2 and to complete gas-liquid separation; The ratio of the weight rate BLPW of liquids in general BLP and the weight rate BLRW of circulation cleaning liquid BLR is K, K is 0.0005 to 0.01.

At the second vaporization separate part STEP3, the 6th kind of mode of operation of the separation column T3 of use is:

At the second vaporization separate part STEP3, at contact separation section T3S1, at least partially liquid phase L1 and at least partially high-temperature gas V2 complete to mix at least one times and contact and be separated into gas phase V3; Gas phase V3 is by washing section T3SX and circulation cleaning liquid BLR counter current contact; The liquid B L that washing section T3SX bottom is flowed out is divided into two portions, first part's circulation enters washing section T3SX top and becomes circulation cleaning liquid BLR, and second section enters as liquid B LP and separate section T3S1 and high-temperature gas V2 and to contact with liquid phase L1 and to complete gas-liquid separation; The ratio of the weight rate BLPW of liquids in general BLP and the weight rate BLRW of circulation cleaning liquid BLR is K, K is 0.0005 to 0.01.

Embodiment

Below describe the present invention in detail.

Pressure of the present invention, refers to absolute pressure.

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

Conventional gas hydrocarbon of the present invention is the hydro carbons of gaseous state under referring to normal condition, comprises methane, ethane, propane, butane; The hydro carbons be in a liquid state under conventional liq hydrocarbon of the present invention refers to normal condition, comprises pentane and the higher hydro carbons of boiling point thereof; Impurity composition of the present invention refers to the hydrocracking thing of non-hydrocarbon component in stock oil as water, ammonia, hydrogen sulfide, hydrogenchloride etc.

In order to describe the problem, coalite tar heavy oil in routine or residual oil or the coal-tar pitch coal tar fraction of 500 DEG C (the such as normal boiling point higher than) are divided into light residue fraction and heavy resid component to treat by the present invention, are such as that the coal tar component of 500 ~ 540 DEG C is called the light residue fraction of coal tar, normal boiling point is called coal tar heavy duty residue fraction higher than the coal tar component of 540 DEG C by normal boiling point.Light residue fraction of the present invention and heavy resid component are a kind of concepts relatively.

Coal-based oil of the present invention, refers to the hydrocarbon ils from coal charge that the dry distillation of coal or coking of coal or the coal such as coal generating gas or DCL/Direct coal liquefaction hot procedure produce, comprises semi coking tar, middle temperature tar, high temperature tar, liquefied coal coil and mixing oil thereof.

Coal-based heavy oil of the present invention, refer to and compare as generally described from the coal-tar pitch of coal tar primarily of the cut of normal boiling point higher than the coal-based oil ingredient composition of 500 DEG C, usually contain a large amount of macromolecular substance as polycyclic aromatic hydrocarbons, colloid, bituminous matter etc., its hydrogen richness is lower, ash oontent is higher.

Coal-based heavy oil component of the present invention, refers to normal boiling point in coal-based oil higher than the hydrocarbon ils component of 500 DEG C, usually containing a large amount of macromolecular substance as polycyclic aromatic hydrocarbons, colloid, bituminous matter etc., its hydrogen richness is lower.

Coal tar of the present invention, refer to the coal tar from the process such as pyrolysis step of pyrolysis of coal or coking of coal or the dry distillation of coal or coal generating gas process or its cut, can be by product coalite tar or its cut of coal generating gas, also can be coal coking pyrolysis of coal process (comprising semi-coking, middle temperature coking, high-temperature coking process) by product coal tar or its cut, coal tar of the present invention can also be the mixing oil of above-mentioned coal tar.Coal tar of the present invention, comprises semi coking tar, middle temperature tar, high temperature tar, the mixing oil of different coal tar, the distillate of coal tar.

High-temperature coking belongs to coal high temperature pyrolysis process, and the outlet temperature of pyrolytic process is generally greater than 900 DEG C, usually between 1000 ~ 1400 DEG C.Described coal-tar heavy oil refers to the by product crude tar oil that coal high temperature pyrolysis produces coke and/or the production of town gas process.Coal-tar heavy oil is in primary distillation process, the following product of usual production: the products such as light oil (topping tar), carbolic oil, naphtalene oil, lightweight washing oil, heavy wash oil, lightweight carbolineum, heavy carbolineum, pitch, carbolic oil can be separated into crude phenols and dephenolize oil further, and naphtalene oil can be separated into thick naphthalene and de-naphtalene oil further.Coal-tar heavy oil lighting end of the present invention refers to: carbolineum, washing oil, naphtalene oil, de-naphtalene oil, carbolic oil, dephenolize oil, light oil and mixing oil thereof.

Because raw coal character and coking or gas-making process condition change all within the specific limits, coal tar oil properties also changes within the specific limits.Processing condition and the product requirement of coal tar primary distillation process also change within the specific limits, therefore the character of coal tar lighting end also changes within the specific limits.The character of coal tar lighting end, proportion is generally 0.92 ~ 1.25, normal boiling point is generally 60 ~ 500 DEG C and is generally 120 ~ 460 DEG C, usual metal content is 5 ~ 80PPm, sulphur content is 0.4 ~ 0.8%, nitrogen content is 0.6 ~ 1.4%, oxygen level is 0.4 ~ 9.0%, usual water-content is 0.2 ~ 5.0%, and carbon residue content is generally 0.5 ~ 13%.

The olefin(e) centent of usual coal tar lighting end is high, the high component also containing more easily reaction under mitigation condition of phenol content; therefore; the pre-hydrogenation process of coal tar lighting end of the present invention, usually uses the single dose of hydrogenation protecting agent, olefins hydrogenation agent, hydrogenation deoxidation agent, hydrogen desulfurization agent etc. or the series combination of two agent or multi-agent or mixed loading combination.Coal tar heavy fractioning is coal-tar pitch cut particularly; its metal content is high, gum level is high, asphalt content is high; therefore; the pre-hydrogenation process of coal tar heavy fractioning of the present invention, usually uses the single dose of hydrogenation protecting agent, hydrodemetallation (HDM) agent, hydrogen desulfurization agent etc. or the series combination of two agent or multi-agent or mixed loading combination

The process of lightweight oil is produced in the hydrocarbon feed F0 of self-contained residue fraction ZYC of the present invention, it is the concept of a broad sense, at least comprise the heating evaporation sepn process of hydrocarbon feed F0, usually the fractionation by distillation process of hydrocarbon feed F0 is comprised, the unifining process HT of the light ends from hydrocarbon feed F0 can also be comprised, also can comprise the hydrocracking process of normal boiling point higher than 350 DEG C of components of unifining process HT hydrogenated oil HTY.

First vaporization separate part STEP1 of the present invention, at least comprises a pervaporation step, as required, can comprise multiple pervaporation step, can comprise multiple heating steps simultaneously, can use well heater, flash tank, separation column.First vaporization separate part STEP1 of the present invention, as required, can complete the distillate of dehydration, de-lighting end (such as carbolic oil, naphtalene oil, carbolineum) task need of production.

Vapour phase hot spots STEP2 of the present invention, arranges gas-phase feed process furnace STEP2F usually, and gas phase is by boiler tube pipe, and boiler tube outside is radiation chamber or the convection chamber of process furnace, and process furnace uses fuel gas or oil fuel usually.

According to the present invention, at vapour phase hot spots STEP2, high temperature gas phase V2 is obtained after only the second temperature T2 being heated to a part of vapour phase V1 (i.e. vapor phase stream V11 to be heated) as required, its objective is and meeting the liquid phase L1 of the first vaporization separate part STEP1 generation under the condition of the heat energy of the contact heat-exchanging evaporative process needs of the second vaporization separate part STEP3, if vapour phase V1 flow has affluence, the unfavorable results such as the power consumption avoiding the superheated of rich part vapour phase V1 (i.e. bypass vapor phase stream V12) to cause and generation heat scission reaction.

According to the present invention, at the second vaporization separate part STEP3, liquid phase L1 and high temperature gas phase V2 complete mixing at least one times and contact and be separated into gas phase V3 and liquid phase L3, this mixing separate process, can be 1 time or 2 times or repeatedly, usually can be that 1 contact separation or 2 counter current contact are separated or repeatedly counter current contact separation, can complete in the contact flash zone contacting flasher or contact flashing tower or separation column.Condensed vapor phases V12 and or the step of vapour phase V3, can complete in special condensation process, also can complete in the tower section being positioned at more than contact flash zone of separation column or system comprising contact flash zone.

Second vaporization separate part STEP3 of the present invention, at least comprises a pervaporation step, as required, can comprise 2 or multiple pervaporation step, can comprise multiple heating steps simultaneously, can use well heater, flash tank, separation column.

Produce the process of lightweight oil in the hydrocarbon feed F0 of self-contained heavy oil of the present invention, at the liquid phase L3 that the second vaporization separate part STEP3 obtains, according to its composition and character, following process can be entered and process further:

1., after asphalt moulding process, obtained shaping pitch is stacked, is sold; Asphalt moulding process, in normally being formed with chain-driving in forming tank, cools with water and wind;

2. through pitch coking process, comprise batch coking process or continuous coking process or Flexicoking process, product coking oil can use as hydrogenation material, and product coke can be stacked, sell;

3. sell outside after storing in liquid fuel within oil tank;

4. sell outside after storing in liquid fuel within oil tank after being in harmonious proportion with other oil fuel;

5. produce visbreaker tar through degree of depth visbreaking process, product coking oil can use as hydrogenation material;

6. after asphalt moulding process, obtained molding massive pitch, loads in mixture coking in the coke oven of high-temperature coking with coking coal, stacking, selling to generating coke, tar and gas;

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

8. as the starting material producing needle coke or asphalt-based carbon fiber;

9. as produce the binding agent of carbon materials and electrode coke starting material;

10. when liquid phase L3 is as the material that the aromatic carbon degree being rich in hydrocarbon matter is high, coking yield about 80% during its coking, cracked gas about 20, oil product yield are low to moderate is almost equal to zero, close with low-volatile coal character, when nearby without suitable liquid material purposes, also can use as the adulterant of solid coal fuel, solve it and store accumulation problem.

1. the hydrocarbon ils that gluey pitch shape component concentration is high;

2. the hydrocarbon ils that ash oontent is high;

3. the hydrocarbon ils that easily coking component concentration is high;

4. the hydrocarbon ils that high temperature easy reactant content is high.

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

5. shale oil or its distillate or its hot procedure gained oil product;

6. tar sand basic weight oil or its hot procedure gained oil product;

7. ethylene cracking tar;

8. petroleum base wax oil thermal cracking tars;

Compared with the method containing coalite tar in residual oil with existing direct heating, the invention has the advantages that:

1. the method for indirect heating vaporization is adopted, under the problem prerequisite avoiding coal-tar residue oil ingredient quick coking to occur in heating furnace tube in high temperature section heat-processed, achieve coal tar particularly in degree of depth vaporization (namely reduce coal-tar pitch yield) of coalite tar, thus improve the yield of vaporizing oil, the light residual oil economic worth of coal tar can be significantly improved;

2. the vaporized components gained cold oil based on middle coalite tar can produce clear gusoline through hydro-upgrading process, therefore, present method can form combination process with coal tar fraction hydro-upgrading, in the process, the light residue fraction of coal tar can be converted into hydrogenation wax oil component through deep hydrofinishing process, hydrogenation wax oil component can be converted into diesel oil and more light constituent thereof through hydrocracking process, can improve the light residual oil economic worth of coal tar further;

3. due to the residual oil L1 that obtains of coalite tar in being separated and or the viscosity of L3 usually larger, if be used as oil fuel, be more conducive to use by becoming visbreaking residue after falling low viscous visbreaking step, and the second vaporization separate part STEP3 of the present invention, possess certain visbreaking effect simultaneously, coal tar heavy duty residual oil economic worth can be improved;

4. the purification of coal tar heavy duty residual oil is achieved, improve the softening temperature of coal-tar pitch, can up to more than 90 ~ 110 DEG C, primarily of the coal-tar pitch of coalite tar in the high softening-point of coal tar heavy duty residual oil composition, being the potential material producing needle coke and asphalt-based carbon fiber, is also the binding agent of carbon materials and the potential material of electrode coke; In other words, the present invention improves value (as hydrogenating materials) that normal boiling point is the light residue fraction of coal tar of 500 ~ 540 DEG C and the normal boiling point value (production low viscosity residual oil or make high softening point bitumen) higher than the coal tar heavy duty residue fraction of 540 DEG C simultaneously; Say in a sense, the present invention is equivalent to coalite tar in handle and has been separated into liquid and " solid ";

5. the present invention is as a kind of common method, can be applied to the process such as the distillation of shale oil, the distillation of oil, to improve distillate vaporization rate further and to improve the initial boiling point temperature of heavy oil.

Embodiment one

The middle coalite tar that the blue charcoal process of coal system produces in table 2, year amount of finish 500,000 tons/year, number 7920 when year goes into operation, quantity is 63132kg/h.In order to isolate light residue fraction to greatest extent, the bituminous matter in coal tar, ash content, particulate matter are concentrated on the blue or green thing of the coal obtaining high softening-point in heavy coal-tar pitch, adopt the present invention, operation steps is as follows simultaneously:

1. at the first vaporization separate part STEP1, condition after raw material F01 heats is: temperature 380 DEG C, pressure 0.15MPaA, carry out the liquid phase L1 (15554kg/h, account for 24.6% of raw material F01) that the first sepn process is separated into vapour phase V1 (47578kg/h, account for 75.4% of raw material F01) and comprises residue fraction, in liquid phase L1, normal boiling point is 47.7% higher than the weight content of 500 DEG C of components, first flash vaporization point T1 is 380 DEG C, and the first sepn process working pressure is 0.15MPaA;

At the first vaporization separate part STEP1, make normal boiling point in coal tar raw material enter in vapour phase V1 lower than 84.3% of the component of 500 DEG C, in vapour phase V1 normal boiling point lower than 500 DEG C, normal boiling point be the light residue fraction of coal tar of 500 ~ 540 DEG C and normal boiling point higher than the part by weight of the coal tar heavy duty residue fraction of 540 DEG C is 98.62%, 0.98%, 0.04%;

2. at vapour phase hot spots STEP2, vapour phase V1 is all heated to after the second temperature T2 as first via vapour phase V11 and obtains high temperature gas phase V2; The service temperature T2 of high temperature gas phase V2 is 430 DEG C, working pressure is 0.10MPaA; With this understanding, the basic noncoking of high temperature gas phase V2, the process furnace continuous cycle of operation can ensure more than 1 year; Process furnace is 1601KW to the thermal load that first via vapour phase V11 temperature-rise period provides;

3. at the second vaporization separate part STEP3, whole liquid phase L1 is made to contact with whole high temperature gas phase V2 mixing and be separated into gas phase V3 and liquid phase L3, about 69.1% component (mainly the light residue fraction of the coal tar) gasification of liquid phase L1 enters in gas phase V3, the weight of liquid phase L3 is 4799kg/h, accounts for about 30.9% of the weight 15554kg/h of liquid phase L1; The temperature T31 of liquid phase L3 is 399 DEG C, liquid phase L3 noncoking at this temperature; Second vaporizing section working pressure is 0.07MPaA;

Above-mentioned second vaporization separate part STEP3 is that the Contact Evaporating section T3S1 more than the gas phase V2 opening for feed of separation column T3 carries out; Contact Evaporating section T3S1 arranges 5 ~ 8 pieces of tower trays, or arranges the random packing layer that the identical height of effect is 2.5 ~ 3.0 meters;

The stripped vapor operational condition passed at the bottom of oily L3SD, separation column T3 tower after the fluid body leaving flash zone obtains stripping after light residue fraction is deviate from the further vacuum flashing of water vapour stripping stage T3S3 that gas phase V2 opening for feed bottom is arranged is: temperature 410 DEG C, pressure 0.1MPaA, flow 486kg/h; Show water vapour stripping stage T3S3 in stripping analog calculation, liquid phase L3 16.9% component complete vaporization.After stripping, the flow of oily L3SD is 3986kg/h, accounts for 6.3% of coal tar raw material F01;

Space after stripping bottom separation column T3 between oily L3SD storage area DL1 and water vapour stripping stage T3S1, be furnished with the refluxing opening L3SDC-N of cold scarce Posterior circle liquid phase L3SDC, after stripping oily L3SD mix with circulation liquid phase L3SDC reduce temperature after become liquid phase L3SDCP, liquid phase L3SDCP to discharge bottom separation column T3 to be cooled to about 180 ~ 200 DEG C by interchanger after pump pressurization becomes cold logistics L3SDCP1, the cold logistics L3SDCP1 of part is through reflux line, bottom separation column T3, be mixed into liquid phase L3SDCP by refluxing opening L3SDC-N as liquid phase L3SDCP and liquid phase L3SD to discharge bottom separation column T3, the cold logistics L3SDCP1 of part is as liquid phase L3SDCP2 deasphalting forming step, the temperature of liquid phase L3SDCP controls as being 280 ~ 300 DEG C,

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

In this example, the heavy bitumen yield of coal tar raw material F01 be 6.3%, coal tar raw material F01 total vaporization rate be 93.7%, remove the water vapor of 4.2%, the vaporised fraction oil yield of coal tar raw material F01 is 89.5%; According to anhydrous butt coal tar conversion, the vaporised fraction oil yield of coal tar raw material F01 is 93.4%, and all the other clearly achieve target of the present invention.

Embodiment two

Based on embodiment one, at vaporised hydrocarbon recycling step STEP4, condensation obtains hydrocarbon ils HPF from the vapour phase V3 of the second vaporization separate part STEP3.

At hydrogenation step STEP5, hydrocarbon ils HPF is converted into hydrogenation oil product through hydro-upgrading process HP, described hydro-upgrading process HP comprises the unifining process HT of hydrocarbon ils HPF, the hydrocracking process HC of the hydrofining wax oil HTVGO formed higher than 350 DEG C of hydrocarbon components primarily of normal boiling point also comprising that the hydrogenated oil HTP that is separated unifining process HT obtains.

This example defines the combination process of middle coalite tar deep drawing and vaporizing oil hydro-upgrading process.

Table 2 coal tar property analysis data

Claims

1. produce a method for lightweight oil in the hydrocarbon stream of self-contained heavy oil, it is characterized in that comprising following steps:

2. method according to claim 1, is characterized in that:

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

At hydrogenation step STEP5, hydrocarbon ils HPF is converted into hydrogenation oil product through hydro-upgrading process HP at least partially, and described hydro-upgrading process HP comprises the unifining process HT of hydrocarbon ils HPF.

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

At hydrogenation step STEP5, hydrocarbon ils HPF is converted into hydrogenation oil product through hydro-upgrading process HP at least partially, described hydro-upgrading process HP comprises the unifining process HT of hydrocarbon ils HPF, the hydrocracking process HC of the hydrofining wax oil HTVGO formed higher than 350 DEG C of hydrocarbon components primarily of normal boiling point also comprising that the hydrogenated oil HTP that is separated unifining process HT obtains.

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

Hydrocarbon feed F01, is selected from one or more in following materials:

1. the hydrocarbon ils that gluey pitch shape component concentration is high;

2. the hydrocarbon ils that ash oontent is high;

3. the hydrocarbon ils that easily coking component concentration is high;

4. the hydrocarbon ils that high temperature easy reactant content is high.

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

Hydrocarbon feed F01, is selected from one or more in following materials:

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

5. shale oil or its distillate or its hot procedure gained oil product;

6. tar sand basic weight oil or its hot procedure gained oil product;

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, is characterized in that:

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

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

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

11. methods according to claim 1 or 2 or 3 or 4, is characterized in that:

12. methods according to claim 1 or 2 or 3 or 4, is characterized in that:

13. methods according to claim 1 or 2 or 3 or 4, is characterized in that:

14. methods according to claim 1 or 2 or 3 or 4, is characterized in that:

15. methods according to claim 1 or 2 or 3 or 4, is characterized in that:

16. methods according to claim 1 or 2 or 3 or 4, is characterized in that:

17. methods according to claim 1 or 2 or 3 or 4, is characterized in that:

Hydrocarbon feed F01 is middle coalite tar, and the softening temperature of the liquid phase L3 that the second vaporization separate part STEP3 obtains is higher than 90 DEG C.

18. methods according to claim 1 or 2 or 3 or 4, is characterized in that:

Hydrocarbon feed F01 is middle coalite tar, and the softening temperature of the liquid phase L3 that the second vaporization separate part STEP3 obtains is higher than 100 DEG C.

19. methods according to claim 1 or 2 or 3 or 4, is characterized in that:

Hydrocarbon feed F01 is middle coalite tar, and the softening temperature of the liquid phase L3 that the second vaporization separate part STEP3 obtains is higher than 110 DEG C.

20. methods according to claim 1 or 2 or 3 or 4, is characterized in that:

21. methods according to claim 20, is characterized in that:

22. methods according to claim 20, is characterized in that:

23. methods according to claim 1 or 2 or 3 or 4, is characterized in that:

24. methods according to claim 20, is characterized in that:

At the second vaporization separate part STEP3, at contact separation section T3S1, at least partially liquid phase L1 and at least partially high-temperature gas V2 complete to mix at least one times and contact and be separated into gas phase V3; Gas phase V3 is by washing section T3SX and circulation cleaning liquid BLR counter current contact; The liquid B L that washing section T3SX bottom is flowed out is divided into two portions, and first part's circulation enters washing section T3SX top and becomes circulation cleaning liquid BLR, and second section enters as liquid B LP and separate section T3SY and to contact with high-temperature gas V2 and to complete gas-liquid separation.

25. methods according to claim 20, is characterized in that:

At the second vaporization separate part STEP3, at contact separation section T3S1, at least partially liquid phase L1 and at least partially high-temperature gas V2 complete to mix at least one times and contact and be separated into gas phase V3; Gas phase V3 is by washing section T3SX and circulation cleaning liquid BLR counter current contact; The liquid B L that washing section T3SX bottom is flowed out is divided into two portions, first part's circulation enters washing section T3SX top and becomes circulation cleaning liquid BLR, and second section enters as liquid B LP and separate section T3S1 and high-temperature gas V2 and to contact with liquid phase L1 and to complete gas-liquid separation.

26. methods according to claim 25, is characterized in that:

At the second vaporization separate part STEP3, be K, K at the ratio of the weight rate BLPW of washing section T3SX, liquid B LP and the weight rate BLRW of circulation cleaning liquid BLR be 0.0005 to 0.01.