CN110180202A - The production system and production method of a kind of low coloration high boiling aromatic hydrocarbon solvent of width boiling range - Google Patents
The production system and production method of a kind of low coloration high boiling aromatic hydrocarbon solvent of width boiling range Download PDFInfo
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- CN110180202A CN110180202A CN201910604981.3A CN201910604981A CN110180202A CN 110180202 A CN110180202 A CN 110180202A CN 201910604981 A CN201910604981 A CN 201910604981A CN 110180202 A CN110180202 A CN 110180202A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4205—Reflux ratio control splitter
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/12—Controlling or regulating
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/18—Solvents
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/30—Aromatics
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- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of methods for producing the low coloration high boiling aromatic hydrocarbon solvent of wide boiling range.The production method of the low coloration high boiling aromatic hydrocarbon solvent of present invention width boiling range, rectifying removing light component is carried out by importing C9+ feedstock in first rectifying column, the first solvent product is separated with the second solvent crude product by Second distillation column again, the second solvent product is separated with coloured heavy constituent finally by third distillation column, simultaneously, accurately control the operating pressure of the rectifying of destilling towers at different levels, temperature and reflux ratio, the boiling range of the first aromatic solvent of gained can be substantially widened in this way, it can also effectively ensure the coloration of the second aromatic solvent, and each step carried out is rectification step, no waste mine discharge, it is environmental friendly pollution-free.
Description
Technical field
The invention belongs to technical field of petrochemical industry, and in particular to a kind of life of the low coloration high boiling aromatic hydrocarbon solvent of width boiling range
Production system and production method.
Background technique
In recent years, with the raising of the chemical industries ability such as oil refining, coal chemical industry, corresponding large-scale joint aromatic device production capacity
It is continuously increased, increases substantially domestic and international heavy aromatics yield.These heavy aromatics how are made full use of, high economic effect is created
Benefit, it has also become industry is paid high attention to and the hot spot of research and development.C9+ fraction generally refers to the heavy being made of C9 aromatic hydrocarbons and C9+ aromatic hydrocarbons
Aromatic fraction is mainly derived from oil plant catalytic reforming unit, ethylene cracker, hydrocracking unit and coal high-temperature coking
Device etc..Wherein, it reforms in C9+ fraction containing about 20% dimethylbenzene, 60% trimethylbenzene and 20% durene and other is few
The heavy aromatics of amount.These high boiling aromatic hydrocarbons mixed components are because its distinctive dissolving power is strong, toxicity is low, smell is small, boiling point is high, volatilization
Slowly, not aqueous and alkene, without chlorine and heavy metal, the advantages that Chemical Physics performance is stable and levelability has in solvent naphtha field
Very extensive application.The control of existing high boiling aromatic hydrocarbon solvent boiling range is more difficult, and coloration not can control, by raw material influenced compared with
Greatly.The boiling range of raw material directly affects product boiling range, and olefin(e) centent cannot be effectively controlled in raw material, easily leads to color number and does not conform to
Lattice.
Summary of the invention
In view of this, the technical problem to be solved in the present invention is that providing a kind of wide boiling range low coloration high boiling aromatic hydrocarbon solvent
Production system and production method, it is low using the available wide boiling range of the production system of high boiling aromatic hydrocarbon solvent provided by the invention
The aromatic solvent of coloration.
The present invention provides a kind of production systems of the low coloration high boiling aromatic hydrocarbon solvent of width boiling range, comprising:
First rectifying column, Second distillation column and the third distillation column being sequentially connected in series, the first rectifying column are provided with C9+ and evaporate
Divide feed(raw material)inlet.
Preferably, comprising:
First rectifying column, the first rectifying column tower middle part are provided with C9+ feedstock entrance, the first rectifying column tower
Top is provided with the first overhead outlet, and the first rectifying column tower bottom is provided with the first bottoms outlet；
Second distillation column, the after-fractionating tower tower middle part are provided with first the bottomsstream entrance, second rectifying
Column overhead is provided with the second overhead outlet, and the Second distillation column tower bottom is provided with the second bottoms outlet；
Third distillation column, the third destilling tower tower middle part are provided with second the bottomsstream entrance, the third rectifying
Column overhead is provided with third overhead outlet, and the third distillation column tower bottom is provided with third bottoms outlet.
Preferably, first overhead outlet is sequentially connected the first condenser and the first return tank, and described first
Return tank is provided with first material outlet, and the first material exit is provided with the first triple valve, first triple valve one
End is connected with the pipeline being connected with the first rectifying column, and the pipeline of high-octane rating tune oil ingredient is drawn in other end connection；
Second overhead outlet is sequentially connected the second condenser and the second return tank, and second return tank is set
It is equipped with second material outlet, the second material exit is provided with the second triple valve, and second triple valve one end is connected with
The pipeline of wide the first high boiling aromatic hydrocarbon solvent of boiling range is drawn in the pipeline being connected with the Second distillation column, other end connection；
The third overhead outlet is sequentially connected third condenser and third return tank, and the third return tank is set
It is equipped with third material outlet, third triple valve is provided at the third material outlet, third triple valve one end is connected with
The pipeline of low the second high boiling aromatic hydrocarbon solvent of coloration is drawn in the pipeline being connected with the third distillation column, other end connection.
Preferably, the third bottoms outlet connection catalytic cracking unit, catalytic diesel oil cracker, wax oil add
One of hydrogen production device or gasoline and diesel hydrogenation device.
Preferably, heavy aromatics or rich arene light wax oil entrance are additionally provided in the middle part of the after-fractionating tower tower.
Preferably, the first rectifying column, Second distillation column and third distillation column are packed tower.
The present invention also provides a kind of method that above-mentioned production system produces the low coloration high boiling aromatic hydrocarbon solvent of wide boiling range, packets
Include following steps:
C9+ feedstock is passed sequentially through into first rectifying column, Second distillation column and third rectifying from C9+ feedstock entrance
Tower, wherein
The absolute pressure of top of the tower of the first rectifying column is 30KPa~70KPa, and tower top operation temperature is 80 DEG C~110 DEG C,
Tower bottom operation temperature is 120~145 DEG C, and reflux ratio is (0.25~25): 1；
The absolute pressure of top of the tower of the Second distillation column is 20KPa~70KPa, and tower top operation temperature is 110 DEG C~140
DEG C, tower bottom operation temperature is 140~170 DEG C, and reflux ratio is (0.2~10): 1；
The absolute pressure of top of the tower of the third distillation column is 5KPa~40KPa, and tower top operation temperature is 100 DEG C~120 DEG C,
Tower bottom operation temperature is 140~170 DEG C, and reflux ratio is (0.1~20): 1.
Preferably, comprising the following steps:
A C9+ feedstock is fed from the C9+ feedstock entrance of first rectifying column), essence is carried out in first rectifying column
Fraction is from the first overhead and first the bottomsstream is obtained, and the first overhead passes through and the first rectifying column tower top phase
Enter the first return tank being connected with first condenser after the first condenser condensation of connection, leads to high-octane rating tune
Oil ingredient；
B) first the bottomsstream entrance that described first the bottomsstream is arranged from the middle part of the after-fractionating tower tower
Charging, in Second distillation column carry out rectifying separate the second overhead and second the bottomsstream, the second tower top distillate
Object enters after the second condenser condensation through being connected with the Second distillation column tower top and is connected with second condenser
Second return tank leads to wide the first high boiling aromatic hydrocarbon solvent of boiling range；
C) second the bottomsstream entrance that described second the bottomsstream is arranged from the middle part of the third destilling tower tower
Charging, in third distillation column carry out rectifying separate third overhead and third the bottomsstream, third tower top distillate
Object enters after the third condenser condensation through being connected with the third distillation column tower top and is connected with the third condenser
Third return tank, leads to low the second high boiling aromatic hydrocarbon solvent of coloration, and described third distillation column the bottomsstream is coloured recombination
Point.
Preferably, step B) are as follows:
By heavy aromatics or rich arene light wax oil and the mixed mixture of first the bottomsstream from described second
The first the bottomsstream entrance charging being arranged in the middle part of destilling tower tower, carries out rectifying in Second distillation column and separates to obtain the second tower top
Distillate and second the bottomsstream, the second overhead pass through the second condenser being connected with the Second distillation column tower top
Enter the second return tank being connected with second condenser after condensation, leads to wide the first high boiling aromatic hydrocarbon solvent of boiling range.
Preferably, the C9+ feedstock be oil plant catalytic reforming, cracking of ethylene, be hydrocracked and coal high temperature refining
The C9+ aromatic hydrocarbons that the devices such as coke obtain, the boiling range range of the C9+ feedstock are 140~220 DEG C, and the C9+ fraction is former
The platinum-cobalt color range of material is not less than 30.
Compared with prior art, the present invention provides a kind of method for producing the low coloration high boiling aromatic hydrocarbon solvent of wide boiling range,
The following steps are included: C9+ feedstock is passed sequentially through first rectifying column, Second distillation column and from C9+ feedstock entrance
Three rectifying columns, wherein the absolute pressure of top of the tower of the first rectifying column be 30KPa~70KPa, tower top operation temperature be 80 DEG C~
110 DEG C, tower bottom operation temperature is 120~145 DEG C, and reflux ratio is 1:4~25；The absolute pressure of top of the tower of the Second distillation column is
20KPa~70KPa, tower top operation temperature are 110 DEG C~140 DEG C, and tower bottom operation temperature is 140~170 DEG C, reflux ratio 1:5
~10；The absolute pressure of top of the tower of the third distillation column is 5KPa~40KPa, and tower top operation temperature is 100 DEG C~120 DEG C, tower
Bottom operation temperature is 140~170 DEG C, and reflux ratio is 1:10~20.The life of the low coloration high boiling aromatic hydrocarbon solvent of present invention width boiling range
Production method carries out rectifying removing light component by importing C9+ feedstock in first rectifying column, then will by Second distillation column
First solvent product is separated with the second solvent crude product, finally by third distillation column by the second solvent product with it is coloured heavy
Component is separated, meanwhile, the operating pressure, temperature and reflux ratio of the rectifying of destilling towers at different levels are accurately controlled, it in this way can be big
Width widens the boiling range of the first aromatic solvent of gained, moreover it is possible to effectively ensure the coloration of the second aromatic solvent, and each step carried out
It is rectification step, no waste mine discharge is environmental friendly pollution-free.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the production system of the low coloration high boiling aromatic hydrocarbon solvent of wide boiling range provided by the invention；
Fig. 2 is the structural schematic diagram of the production system for the high boiling aromatic hydrocarbon solvent that comparative example 1 provides.
Specific embodiment
The present invention provides a kind of production systems of the low coloration high boiling aromatic hydrocarbon solvent of width boiling range, comprising:
First rectifying column, Second distillation column and the third distillation column being sequentially connected in series, the first rectifying column are provided with C9+ and evaporate
Divide feed(raw material)inlet.
Referring to Fig. 1, Fig. 1 is that the structure of the production system of the low coloration high boiling aromatic hydrocarbon solvent of wide boiling range provided by the invention is shown
It is intended to.
In certain specific embodiments of the invention, the production system of the low coloration high boiling aromatic hydrocarbon solvent of the width boiling range
Include:
First rectifying column, the first rectifying column tower middle part are provided with C9+ feedstock entrance, the first rectifying column tower
Top is provided with the first overhead outlet, and the first rectifying column tower bottom is provided with the first bottoms outlet；
First overhead outlet is sequentially connected the first condenser and the first return tank, and first return tank is set
It is equipped with first material outlet, the first material exit is provided with the first triple valve, and first triple valve one end is connected with
The pipeline of high-octane rating tune oil ingredient is drawn in the pipeline being connected with the first rectifying column, other end connection.
Second distillation column, the after-fractionating tower tower middle part are provided with first the bottomsstream entrance, second rectifying
Column overhead is provided with the second overhead outlet, and the Second distillation column tower bottom is provided with the second bottoms outlet；
Second overhead outlet is sequentially connected the second condenser and the second return tank, and second return tank is set
It is equipped with second material outlet, the second material exit is provided with the second triple valve, and second triple valve one end is connected with
The pipeline of wide the first high boiling aromatic hydrocarbon solvent of boiling range is drawn in the pipeline being connected with the Second distillation column, other end connection.
Third distillation column, the third destilling tower tower middle part are provided with second the bottomsstream entrance, the third rectifying
Column overhead is provided with third overhead outlet, and the third distillation column tower bottom is provided with third bottoms outlet.
The third overhead outlet is sequentially connected third condenser and third return tank, and the third return tank is set
It is equipped with third material outlet, third triple valve is provided at the third material outlet, third triple valve one end is connected with
The pipeline of low the second high boiling aromatic hydrocarbon solvent of coloration is drawn in the pipeline being connected with the third distillation column, other end connection.
The third bottoms outlet connects catalytic cracking unit, catalytic diesel oil cracker, Wax Oil Hydrogenation Unit
Or one of gasoline and diesel hydrogenation device.
The tower bottom of the first rectifying column, Second distillation column and third distillation column be connected separately with the first tower bottom reboiler,
Second tower bottom reboiler and third tower bottom reboiler.
The first rectifying column, Second distillation column and third distillation column are packed tower, the filling kind in the packed tower
There is no particular/special requirement, the known filling kind of those skilled in the art.
First return tank, the second return tank and third return tank are connect with pumped vacuum systems, make entire production system
In decompression state, wherein the pumped vacuum systems is preferably vacuum pump, and the vacuum pump type uses dry vacuum pump.
The vacuum degree of the production system of the low coloration high boiling aromatic hydrocarbon solvent of the wide boiling range is 5~20KPa.
Heavy aromatics or rich arene light wax oil entrance are additionally provided in the middle part of the after-fractionating tower tower.Of the invention some
In specific embodiment, offered between first bottoms outlet and the connecting pipe of first the bottomsstream entrance
Threeway, one end of the threeway are connected with the first bottoms outlet, the other end of the threeway and first the bottomsstream
Entrance is connected, and the third end of the threeway is connected with heavy aromatics or rich arene light wax oil entrance.In this way distillate the first tower bottom
Object enters back into Second distillation column after mixing with heavy aromatics or rich arene light wax oil.At this point, heavy aromatics or rich arene light wax oil
Entrance and first the bottomsstream entrance are the same entrance.
The heavy aromatics or rich arene light wax oil are selected from reformer C10+ heavy aromatics, rich arene light wax oil plus hydrogen
The mixture of one or more materials such as heavy petrol.The quality index of the heavy aromatics is initial boiling point: 167.7；10% evaporation temperature
It spends (DEG C): 174.3；50% evaporating temperature (DEG C): 184.6；90% evaporating temperature (DEG C): 189.5；It does (DEG C): 196.1.
The raw material of the heavy aromatics or rich arene light wax oil as Second distillation column, effect are to increase high boiling aromatic hydrocarbons
The yield of solvent improves the value for the heavy aromatics that other devices come, and it is high boiling that another effect can exactly play adjustment first, second
The effect of point aromatic solvent boiling range.
In certain specific embodiments of the invention, heavy aromatics or Fu Fang are additionally provided in the middle part of the third destilling tower tower
Hydrocarbon lightweight wax oil entrance.In certain specific embodiments of the invention, in second bottoms outlet and the second tower
Threeway is offered between the connecting pipe of bottom distillate entrance, one end of the threeway is connected with the second bottoms outlet, institute
The other end for stating threeway is connected with second the bottomsstream entrance, third end and heavy aromatics or the rich arene light wax of the threeway
Oil-in is connected.Third rectifying is entered back into after mixing second the bottomsstream with heavy aromatics or rich arene light wax oil
Tower.At this point, heavy aromatics or rich arene light wax oil entrance and first the bottomsstream entrance are the same entrance.
The heavy aromatics or rich arene light wax oil are selected from reformer C10+ heavy aromatics, rich arene light wax oil plus hydrogen
The mixture of one or more materials such as heavy petrol.The quality index of the richness arene light wax oil is initial boiling point: 186.7；
10% evaporating temperature (DEG C): 188.6；50% evaporating temperature (DEG C): 189.6；90% evaporating temperature (DEG C): 190.2；It does
(DEG C): 195.4.
The raw material of the heavy aromatics or rich arene light wax oil as third distillation column, effect are to increase high boiling aromatic hydrocarbons
The yield of solvent improves the value for the heavy aromatics that other devices come, and it is high that another effect exactly can increase by second to a certain extent
The yield of boiling point aromatic solvent.
The present invention also provides a kind of sides that the low coloration high boiling aromatic hydrocarbon solvent of wide boiling range is produced using above-mentioned production system
Method, comprising the following steps:
C9+ feedstock is passed sequentially through into first rectifying column, Second distillation column and third rectifying from C9+ feedstock entrance
Tower, wherein
The absolute pressure of top of the tower of the first rectifying column is 30KPa~70KPa, and tower top operation temperature is 80 DEG C~110 DEG C,
Tower bottom operation temperature is 120~145 DEG C, and reflux ratio is (0.25~25): 1；
The absolute pressure of top of the tower of the Second distillation column is 20KPa~70KPa, and tower top operation temperature is 110 DEG C~140
DEG C, tower bottom operation temperature is 140~170 DEG C, and reflux ratio is (0.2~10): 1；
The absolute pressure of top of the tower of the third distillation column is 5KPa~40KPa, and tower top operation temperature is 100 DEG C~120 DEG C,
Tower bottom operation temperature is 140~170 DEG C, and reflux ratio is (0.1~20): 1.
In the present invention, the C9+ feedstock is oil plant catalytic reforming, cracking of ethylene, is hydrocracked and coal is high
The C9+ aromatic hydrocarbons that the devices such as warm coking obtain, the boiling range range of the C9+ feedstock are 140~220 DEG C, and the C9+ evaporates
The platinum-cobalt color range for dividing raw material is not less than 30.
C9+ feedstock is fed into the progress rectifying in first rectifying column from middle part and separates to obtain the first overhead, the
One overhead enters and first condensation after the first condenser condensation through being connected with the first rectifying column tower top
The first return tank that device is connected leads to high-octane rating tune oil ingredient；
The rectifying condition of the first rectifying column are as follows: absolute pressure of top of the tower be 30KPa~70KPa, preferably 40~
60KPa, tower top operation temperature are 80 DEG C~110 DEG C, and preferably 90~100 DEG C, tower bottom operation temperature is 120~145 DEG C, preferably
It is 130~140 DEG C, reflux ratio is 1:4~25, preferably 1:(10~17).
By described first the bottomsstream from middle part feed in Second distillation column carry out rectifying separate the second tower top evaporates
Object out, the second overhead enter and described the after the second condenser condensation through being connected with the Second distillation column tower top
The second return tank that two condensers are connected leads to wide the first high boiling aromatic hydrocarbon solvent of boiling range.
The rectifying condition of the Second distillation column are as follows: absolute pressure of top of the tower be 20KPa~70KPa, preferably 30~
60KPa, tower top operation temperature are 110 DEG C~140 DEG C, and preferably 120~130 DEG C, tower bottom operation temperature is 140~170 DEG C, excellent
It is selected as 150~160 DEG C, reflux ratio is 1:(5~10), preferably 1:(6~9).
In certain specific embodiments of the invention, heavy aromatics or rich arene light wax oil are evaporated with first tower bottom
First the bottomsstream entrance charging that the mixed mixture of object is arranged from the middle part of the after-fractionating tower tower out, in the second essence
It evaporates and carries out rectifying in tower and separate to obtain the second overhead and second the bottomsstream, the second overhead passes through and described second
Enter the second return tank being connected with second condenser after the second condenser condensation that the top of the distillation column is connected, draws
For wide the first high boiling aromatic hydrocarbon solvent of boiling range.
The source of the heavy aromatics or rich arene light wax oil is the C10+ heavy aromatics of reformer, rich arene light wax
The mixture of oily, hydrogenated heavy gasoline one or more materials.
By described second the bottomsstream from middle part feed in third distillation column carry out rectifying separate third tower top evaporates
Object out, third overhead enter and described the after the third condenser condensation through being connected with the third distillation column tower top
The third return tank that three condensers are connected leads to low the second high boiling aromatic hydrocarbon solvent of coloration.Third distillation column tower bottom distillates
Object is coloured heavy constituent, draws other device raw materials.
The rectifying condition of the third distillation column are as follows: absolute pressure of top of the tower be 5KPa~40KPa, preferably 15~30KPa,
Tower top operation temperature is 100 DEG C~120 DEG C, and preferably 105~115 DEG C, tower bottom operation temperature is 140~170 DEG C, preferably
150~160 DEG C, reflux ratio is 1:(10~20), preferably 1:(13~17).
The production method of the low coloration high boiling aromatic hydrocarbon solvent of present invention width boiling range, by the way that C9+ feedstock is imported first
Rectifying is carried out in rectifying column and removes light component, then is carried out the first solvent product and the second solvent crude product by Second distillation column
Separation, separates the second solvent product with coloured heavy constituent finally by third distillation column, meanwhile, accurately control steamings at different levels
The operating pressure, temperature and reflux ratio of the rectifying of tower are evaporated, can substantially widen the boiling range of the first aromatic solvent of gained in this way, moreover it is possible to
Effectively ensure the coloration of the second aromatic solvent, and each step carried out is rectification step, no waste mine discharge, environmental friendly nothing
Pollution.
In addition, production method provided by the invention also has the advantages that
(1) production method adaptability to raw material provided by the invention is strong, and it is very big to can be adapted for boiling range fluctuating change range
Raw material, production technology is flexible, and target product yield is high；
(2) for the raw material of wide process range, device technique process is adjusted fast and accurately；
(3) it is directed to high chroma raw material, feasible process and safe and reliable.
For a further understanding of the present invention, below with reference to embodiment to the low coloration higher boiling virtue of width boiling range provided by the invention
The production system and production method of hydrocarbon solvent are illustrated, and protection scope of the present invention is not limited by the following examples.
Embodiment 1
The production system of the low coloration high boiling aromatic hydrocarbon solvent of wide boiling range includes:
First rectifying column, the first rectifying column tower middle part are provided with C9+ feedstock entrance, the first rectifying column tower
Top is provided with the first overhead outlet, and the first rectifying column tower bottom is provided with the first bottoms outlet；
First overhead outlet is sequentially connected the first condenser and the first return tank, and first return tank is set
It is equipped with first material outlet, the first material exit is provided with the first triple valve, and first triple valve one end is connected with
The pipeline of high-octane rating tune oil ingredient is drawn in the pipeline being connected with the first rectifying column, other end connection.
Second distillation column, the after-fractionating tower tower middle part are provided with first the bottomsstream entrance, second rectifying
Column overhead is provided with the second overhead outlet, and the Second distillation column tower bottom is provided with the second bottoms outlet；
Second overhead outlet is sequentially connected the second condenser and the second return tank, and second return tank is set
It is equipped with second material outlet, the second material exit is provided with the second triple valve, and second triple valve one end is connected with
The pipeline of wide the first high boiling aromatic hydrocarbon solvent of boiling range is drawn in the pipeline being connected with the Second distillation column, other end connection.
Third distillation column, the third destilling tower tower middle part are provided with second the bottomsstream entrance, the third rectifying
Column overhead is provided with third overhead outlet, and the third distillation column tower bottom is provided with third bottoms outlet.
The third overhead outlet is sequentially connected third condenser and third return tank, and the third return tank is set
It is equipped with third material outlet, third triple valve is provided at the third material outlet, third triple valve one end is connected with
The pipeline of low the second high boiling aromatic hydrocarbon solvent of coloration is drawn in the pipeline being connected with the third distillation column, other end connection.
The third bottoms outlet connects catalytic cracking unit, catalytic diesel oil cracker, Wax Oil Hydrogenation Unit
Or one of gasoline and diesel hydrogenation device.
The tower bottom of the first rectifying column, Second distillation column and third distillation column be connected separately with the first tower bottom reboiler,
Second tower bottom reboiler and third tower bottom reboiler.
The first rectifying column, Second distillation column and third distillation column are packed tower, the filling kind in the packed tower
SP series structured packing.
First return tank, the second return tank and third return tank are connected with dry vacuum pump.
Embodiment 2
A kind of production method of the low coloration high boiling aromatic hydrocarbon solvent of width boiling range, is carried out using rectification process at reduced pressure conditions
Production.
The specific steps are that:
(1) C9+ feedstock is fed into the progress rectifying in first rectifying column from middle part and separates to obtain the first overhead,
It enters after first condenser condensation through being connected with the first rectifying column tower top and is connected with first condenser
First return tank leads to high-octane rating tune oil ingredient；
(2) the bottomsstream of the first rectifying column progress rectifying in Second distillation column is fed from middle part to separate
Second overhead enters and described second after the second condenser condensation through being connected with the Second distillation column tower top
The second return tank that condenser is connected leads to wide the first high boiling aromatic hydrocarbon solvent of boiling range；
(3) the bottomsstream of the Second distillation column progress rectifying in third distillation column is fed from middle part to separate
Third overhead enters and the third after the third condenser condensation through being connected with the third distillation column tower top
The third return tank that condenser is connected leads to low the second high boiling aromatic hydrocarbon solvent of coloration.Third distillation column the bottomsstream
For coloured heavy constituent, other device raw materials are drawn.
The rectifying tower internals are structured packing.
The rectifying condition of first rectifying column described in step (1) are as follows: absolute pressure of top of the tower is 35 ± 5KPa, tower top operation temperature
Degree is 100 ± 5 DEG C, and tower bottom operation temperature is 130 ± 5 DEG C, and reflux ratio is (10~12): 1
The rectifying condition of Second distillation column described in step (2) are as follows: absolute pressure of top of the tower is 30 ± 5KPa, tower top operation temperature
Degree is 120 ± 5 DEG C, and tower bottom operation temperature is 155 ± 5 DEG C, and reflux ratio is (0.5~3): 1.
The rectifying condition of third distillation column described in step (3) are as follows: absolute pressure of top of the tower is 10 ± 5KPa, tower top operation temperature
Degree is 110 ± 5 DEG C, and tower bottom operation temperature is 155 ± 5 DEG C, and reflux ratio is (1~6): 1.
Performance measurement is carried out to the product that above-mentioned steps obtain, the results are shown in Table 1
1 raw material of table and product property measurement result
Embodiment 3
A kind of production method of the low coloration high boiling aromatic hydrocarbon solvent of width boiling range, is carried out using rectification process at reduced pressure conditions
Production.
The specific steps are that:
(1) C9+ feedstock is fed into the progress rectifying in first rectifying column from middle part and separates to obtain the first overhead,
It enters after first condenser condensation through being connected with the first rectifying column tower top and is connected with first condenser
First return tank leads to high-octane rating tune oil ingredient；
It (2) will be after being sufficiently mixed of C10+ heavy aromatics that the bottomsstream of the first rectifying column and reformer unit come
Into the middle part of the Second distillation column, rectifying is carried out in Second distillation column and separates to obtain the second overhead, warp and institute
Enter the second reflux being connected with second condenser after stating the second condenser condensation that Second distillation column tower top is connected
Tank leads to wide the first high boiling aromatic hydrocarbon solvent of boiling range；
Wherein, in the production system of the low coloration high boiling aromatic hydrocarbon solvent of the wide boiling range, in described first the bottomsstream
Threeway, one end of the threeway and first the bottomsstream are offered between outlet and the connecting pipe of first the bottomsstream entrance
Outlet is connected, and the other end of the threeway is connected with first the bottomsstream entrance, the third end of the threeway and heavy aromatics or
Rich arene light wax oil entrance is connected.After in this way mixing first the bottomsstream and heavy aromatics or rich arene light wax oil again into
Enter Second distillation column.
(3) the bottomsstream of the Second distillation column progress rectifying in third distillation column is fed from middle part to separate
Third overhead enters and the third after the third condenser condensation through being connected with the third distillation column tower top
The third return tank that condenser is connected leads to low the second high boiling aromatic hydrocarbon solvent of coloration.Third distillation column the bottomsstream
For coloured heavy constituent, other device raw materials are drawn.
The rectifying tower internals are structured packing.
The rectifying condition of first rectifying column described in step (1) are as follows: absolute pressure of top of the tower is 30 ± 5KPa, tower top operation temperature
Degree is 98 ± 5 DEG C, and tower bottom operation temperature is 135 ± 5 DEG C, and reflux ratio is (15~17): 1.
The rectifying condition of Second distillation column described in step (2) are as follows: absolute pressure of top of the tower is 30 ± 5KPa, tower top operation temperature
Degree is 120 ± 5 DEG C, and tower bottom operation temperature is 155 ± 5 DEG C, and reflux ratio is (0.5~2.5): 1.
The rectifying condition of third distillation column described in step (3) are as follows: absolute pressure of top of the tower is 10 ± 5KPa, tower top operation temperature
Degree is 110 ± 5 DEG C, and tower bottom operation temperature is 155 ± 5 DEG C, and reflux ratio is (1~5): 1.
Performance measurement is carried out to the product that above-mentioned steps obtain, the results are shown in Table 2
2 raw material of table and product property measurement result
Embodiment 4
A kind of production method of the low coloration high boiling aromatic hydrocarbon solvent of width boiling range, is carried out using rectification process at reduced pressure conditions
Production.
The specific steps are that:
(1) C9+ feedstock is fed into the progress rectifying in first rectifying column from middle part and separates to obtain the first overhead,
It enters after first condenser condensation through being connected with the first rectifying column tower top and is connected with first condenser
First return tank leads to high-octane rating tune oil ingredient；
(2) the bottomsstream of the first rectifying column progress rectifying in Second distillation column is fed from middle part to separate
Second overhead enters and described second after the second condenser condensation through being connected with the Second distillation column tower top
The second return tank that condenser is connected leads to wide the first high boiling aromatic hydrocarbon solvent of boiling range；
(3) the bottomsstream of the Second distillation column is sufficiently mixed with the hydrogenated heavy gasoline come from gasoline hydrogenation device
It is fed afterwards from middle part, rectifying is carried out in third distillation column and separates to obtain third overhead, warp and the third distillation column
Enter the third return tank being connected with the third condenser after the third condenser condensation that tower top is connected, leads to low color
Spend the second high boiling aromatic hydrocarbon solvent.Third distillation column the bottomsstream is coloured heavy constituent, draws other devices.
Wherein, in the production system of the low coloration high boiling aromatic hydrocarbon solvent of the wide boiling range, in described second the bottomsstream
Threeway, one end of the threeway and second the bottomsstream are offered between outlet and the connecting pipe of second the bottomsstream entrance
Outlet is connected, and the other end of the threeway is connected with second the bottomsstream entrance, the third end of the threeway and plus hydrogen weight vapour
Oil-in is connected.Third distillation column is entered back into after mixing second the bottomsstream with hydrogenated heavy gasoline.
The rectifying tower internals are structured packing.
The rectifying condition of first rectifying column described in step (1) are as follows: absolute pressure of top of the tower is 30 ± 5KPa, tower top operation temperature
Degree is 98 ± 5 DEG C, and tower bottom operation temperature is 135 ± 5 DEG C, and reflux ratio is (10~20): 1.
The rectifying condition of Second distillation column described in step (2) are as follows: absolute pressure of top of the tower is 30 ± 5KPa, tower top operation temperature
Degree is 120 ± 5 DEG C, and tower bottom operation temperature is 155 ± 5 DEG C, and reflux ratio is (1~10): 1.
The rectifying condition of third distillation column described in step (3) are as follows: absolute pressure of top of the tower is 10 ± 5KPa, tower top operation temperature
Degree is 110 ± 5 DEG C, and tower bottom operation temperature is 155 ± 5 DEG C, and reflux ratio is (1~6): 1.
Performance measurement is carried out to the product that above-mentioned steps obtain, the results are shown in Table 3
3 raw material of table and product property measurement result
Comparative example 1
Referring to fig. 2, Fig. 2 is the structural representation of the production system for the high boiling aromatic hydrocarbon solvent that comparative example 1 provides to production system
Figure.It specifically includes:
First rectifying column, the first rectifying column tower middle part are provided with C9+ feedstock entrance, the first rectifying column tower
Top is provided with the first overhead outlet, and the first rectifying column tower bottom is provided with the first bottoms outlet；
First overhead outlet is sequentially connected the first condenser and the first return tank, and first return tank is set
It is equipped with first material outlet, the first material exit is provided with the first triple valve, and first triple valve one end is connected with
The pipeline of high-octane rating tune oil ingredient is drawn in the pipeline being connected with the first rectifying column, other end connection.
Second distillation column, the after-fractionating tower tower middle part are provided with first the bottomsstream entrance, second rectifying
Column overhead is provided with the second overhead outlet, and the Second distillation column tower bottom is provided with the second bottoms outlet；
Second overhead outlet is sequentially connected the second condenser and the second return tank, and second return tank is set
It is equipped with second material outlet, the second material exit is provided with the second triple valve, and second triple valve one end is connected with
The pipeline of the first high boiling aromatic hydrocarbon solvent is drawn in the pipeline being connected with the Second distillation column, other end connection.
The first rectifying column and the tower bottom of Second distillation column are connected separately with the first tower bottom reboiler and the second tower bottom again
Boil device.
The first rectifying column and Second distillation column are packed tower, and the filling kind SP series in the packed tower is regular to fill out
Material.
First return tank, the second return tank and third return tank are connected with dry vacuum pump.
Comparative example 2
The device for selecting comparative example 1 to provide
(1) C9+ feedstock is fed into the progress rectifying in first rectifying column from middle part and separates to obtain the first overhead,
It enters after first condenser condensation through being connected with the first rectifying column tower top and is connected with first condenser
First return tank leads to high-octane rating tune oil ingredient；
(2) the bottomsstream of the first rectifying column progress rectifying in Second distillation column is fed from middle part to separate
Second overhead enters and described second after the second condenser condensation through being connected with the Second distillation column tower top
The second return tank that condenser is connected, leads to the first high boiling aromatic hydrocarbon solvent, and Second distillation column the bottomsstream is second
High boiling aromatic hydrocarbon solvent.
The rectifying condition of first rectifying column described in step (1) are as follows: absolute pressure of top of the tower is 40 ± 1KPa, tower top operation temperature
Degree is 101 ± 1 DEG C, and tower bottom operation temperature is 128 ± 1 DEG C, reflux ratio 6:1.
The rectifying condition of Second distillation column described in step (2) are as follows: absolute pressure of top of the tower is 40 ± 1KPa, tower top operation temperature
Degree is 128 ± 1 DEG C, and tower bottom operation temperature is 172 ± 1 DEG C, reflux ratio 8:1.
Performance measurement is carried out to the product that above-mentioned steps obtain, the results are shown in Table 4
4 product property measurement result of table
Comparative example 3
A kind of production method of the low coloration high boiling aromatic hydrocarbon solvent of width boiling range, is carried out using rectification process at reduced pressure conditions
Production, the device for selecting embodiment 1 to provide are produced.
The specific steps are that:
(1) C9+ feedstock is fed into the progress rectifying in first rectifying column from middle part and separates to obtain the first overhead,
It enters after first condenser condensation through being connected with the first rectifying column tower top and is connected with first condenser
First return tank leads to high-octane rating tune oil ingredient；
(2) the bottomsstream of the first rectifying column progress rectifying in Second distillation column is fed from middle part to separate
Second overhead enters and described second after the second condenser condensation through being connected with the Second distillation column tower top
The second return tank that condenser is connected leads to wide the first high boiling aromatic hydrocarbon solvent of boiling range；
(3) by the bottomsstream of the Second distillation column and the heavy aromatics or rich arene light wax oil that come from other devices
Source be that the abundant of one or more materials such as reformer C10+ heavy aromatics, rich arene light wax oil, hydrogenated heavy gasoline mix
It is fed after conjunction from middle part, rectifying is carried out in third distillation column and separates to obtain third overhead, warp and the third rectifying
Enter the third return tank being connected with the third condenser after the third condenser condensation that column overhead is connected, leads to low
The second high boiling aromatic hydrocarbon solvent of coloration.Third distillation column the bottomsstream is coloured heavy constituent, draws other device raw materials.
The rectifying condition of first rectifying column described in step (1) are as follows: absolute pressure of top of the tower is 28 ± 1KPa, tower top operation temperature
Degree is 98 ± 1 DEG C, and tower bottom operation temperature is 127 ± 1 DEG C, reflux ratio 27:1.
The rectifying condition of Second distillation column described in step (2) are as follows: absolute pressure of top of the tower is 41 ± 1KPa, tower top operation temperature
Degree is 125 ± 1 DEG C, and tower bottom operation temperature is 151 ± 1 DEG C, reflux ratio 8:1.
The rectifying condition of third distillation column described in step (3) are as follows: absolute pressure of top of the tower is 45 ± 1KPa, tower top operation temperature
Degree is 136 ± 1 DEG C, and tower bottom operation temperature is 155 ± 1 DEG C, reflux ratio 2:1.
Performance measurement is carried out to the product that above-mentioned steps obtain, the results are shown in Table 5
5 product property measurement result of table
The above is only a preferred embodiment of the present invention, it is noted that for the ordinary skill people of the art
For member, various improvements and modifications may be made without departing from the principle of the present invention, these improvements and modifications are also answered
It is considered as protection scope of the present invention.
Claims (10)
1. a kind of production system of the low coloration high boiling aromatic hydrocarbon solvent of width boiling range characterized by comprising
First rectifying column, Second distillation column and the third distillation column being sequentially connected in series, it is former that the first rectifying column is provided with C9+ fraction
Expect entrance.
2. production system according to claim 1 characterized by comprising
First rectifying column, the first rectifying column tower middle part are provided with C9+ feedstock entrance, and the first rectifying column tower top is set
It is equipped with the first overhead outlet, the first rectifying column tower bottom is provided with the first bottoms outlet；
Second distillation column, the after-fractionating tower tower middle part are provided with first the bottomsstream entrance, the Second distillation column tower
Top is provided with the second overhead outlet, and the Second distillation column tower bottom is provided with the second bottoms outlet；
Third distillation column, the third destilling tower tower middle part are provided with second the bottomsstream entrance, the third distillation column tower
Top is provided with third overhead outlet, and the third distillation column tower bottom is provided with third bottoms outlet.
3. production system according to claim 2, which is characterized in that first overhead outlet is sequentially connected
One condenser and the first return tank, first return tank are provided with first material outlet, the first material exit setting
There is the first triple valve, first triple valve one end is connected with the pipeline being connected with the first rectifying column, and other end connection is drawn
The pipeline of high-octane rating tune oil ingredient out；
Second overhead outlet is sequentially connected the second condenser and the second return tank, and second return tank is provided with
Second material outlet, the second material exit are provided with the second triple valve, and second triple valve one end is connected with and institute
The connected pipeline of Second distillation column is stated, the pipeline of wide the first high boiling aromatic hydrocarbon solvent of boiling range is drawn in other end connection；
The third overhead outlet is sequentially connected third condenser and third return tank, and the third return tank is provided with
Third material outlet is provided with third triple valve at the third material outlet, and third triple valve one end is connected with and institute
The connected pipeline of third distillation column is stated, the pipeline of low the second high boiling aromatic hydrocarbon solvent of coloration is drawn in other end connection.
4. production system according to claim 1, which is characterized in that the third bottoms outlet connection catalysis is split
Makeup sets, one of catalytic diesel oil cracker, Wax Oil Hydrogenation Unit or gasoline and diesel hydrogenation device.
5. production system according to claim 1, which is characterized in that be additionally provided with weight virtue in the middle part of the after-fractionating tower tower
Hydrocarbon or rich arene light wax oil entrance.
6. production system according to claim 1, which is characterized in that the first rectifying column, Second distillation column and third
Rectifying column is packed tower.
7. a kind of molten using the low coloration high boiling aromatic hydrocarbons of the wide boiling range of the production of production system described in claim 1~6 any one
The method of agent, which comprises the following steps:
C9+ feedstock is passed sequentially through into first rectifying column, Second distillation column and third distillation column from C9+ feedstock entrance,
Wherein,
The absolute pressure of top of the tower of the first rectifying column is 30KPa~70KPa, and tower top operation temperature is 80 DEG C~110 DEG C, tower bottom
Operation temperature is 120~145 DEG C, and reflux ratio is (0.25~25): 1；
The absolute pressure of top of the tower of the Second distillation column is 20KPa~70KPa, and tower top operation temperature is 110 DEG C~140 DEG C, tower
Bottom operation temperature is 140~170 DEG C, and reflux ratio is (0.2~10): 1；
The absolute pressure of top of the tower of the third distillation column is 5KPa~40KPa, and tower top operation temperature is 100 DEG C~120 DEG C, tower bottom
Operation temperature is 140~170 DEG C, and reflux ratio is (0.1~20): 1.
8. the method according to the description of claim 7 is characterized in that the following steps are included:
A C9+ feedstock is fed from the C9+ feedstock entrance of first rectifying column), rectifying point is carried out in first rectifying column
From the first overhead and first the bottomsstream is obtained, the first overhead is connected with the first rectifying column tower top
The condensation of the first condenser after enter the first return tank for being connected with first condenser, lead to high-octane rating tune oil group
Point；
B) first the bottomsstream entrance that described first the bottomsstream is arranged from the middle part of the after-fractionating tower tower is fed,
Carry out rectifying in Second distillation column and separate to obtain the second overhead and second the bottomsstream, the second overhead pass through with
Enter second time to be connected with second condenser after the second condenser condensation that the Second distillation column tower top is connected
Tank is flowed, wide the first high boiling aromatic hydrocarbon solvent of boiling range is led to；
C) second the bottomsstream entrance that described second the bottomsstream is arranged from the middle part of the third destilling tower tower is fed,
Carry out rectifying in third distillation column and separate to obtain third overhead and third the bottomsstream, third overhead pass through with
Enter the third being connected with the third condenser after the third condenser condensation that the third distillation column tower top is connected to return
Tank is flowed, low the second high boiling aromatic hydrocarbon solvent of coloration is led to, described third distillation column the bottomsstream is coloured heavy constituent.
9. according to the method described in claim 8, it is characterized in that, step B) are as follows:
By heavy aromatics or rich arene light wax oil and the mixed mixture of first the bottomsstream from the after-fractionating
The first the bottomsstream entrance charging being arranged in the middle part of tower tower, carried out in Second distillation column rectifying separate the second tower top distillates
Object and second the bottomsstream, the second overhead pass through the second condenser condensation being connected with the Second distillation column tower top
Enter the second return tank being connected with second condenser afterwards, leads to wide the first high boiling aromatic hydrocarbon solvent of boiling range.
10. the method according to the description of claim 7 is characterized in that the C9+ feedstock is oil plant catalytic reforming, second
Alkene cracking is hydrocracked and C9+ aromatic hydrocarbons that the devices such as coal high-temperature coking obtain, the boiling range range of the C9+ feedstock
It is 140~220 DEG C, the platinum-cobalt color range of the C9+ feedstock is not less than 30.
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