CN106478379A - A kind of coal tar oil ingredient continuous separation technology and device - Google Patents
A kind of coal tar oil ingredient continuous separation technology and device Download PDFInfo
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- CN106478379A CN106478379A CN201610828429.9A CN201610828429A CN106478379A CN 106478379 A CN106478379 A CN 106478379A CN 201610828429 A CN201610828429 A CN 201610828429A CN 106478379 A CN106478379 A CN 106478379A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/005—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by obtaining phenols from products, waste products or side-products of processes, not directed to the production of phenols, by conversion or working-up
- C07C37/007—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by obtaining phenols from products, waste products or side-products of processes, not directed to the production of phenols, by conversion or working-up from the tar industry
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/18—Working-up tar by extraction with selective solvents
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C3/00—Working-up pitch, asphalt, bitumen
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- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Civil Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Structural Engineering (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Working-Up Tar And Pitch (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
A kind of coal tar oil ingredient continuous separation technology and device, are carried out mixing, are extracted, stir using solvent orange 2 A and coal tar in extractive reaction kettle, then in knockout drum, coal tar is separated with the mixture of solvent orange 2 A, obtain asphalt component；By the double adsorption tower of setting, achieve and adsorb and being carried out continuously of eluting, the solvent orange 2 A extract that removing asphalt component simultaneously can be made passes through adsorption tower, enters in neutral oil component knockout tower through the mixed liquor that adsorbing separation obtains and carries out rectification, obtains neutral oil ingredient and recycling design A；Adsorption tower solvent B being crossed after the pressurization of solvent B feed pump adsorption solvent A extract carries out eluting, and eluent enters crude phenols Component seperation tower, separates through rectification and obtains crude phenols component and recycling design B.The present invention is green separation technique, does not produce waste water, waste residue and waste gas, and the operating condition of technique is gentle, easy, technique and equipment manufacturing cost is low, less investment the advantages of.
Description
Technical field
The invention belongs to technical field of coal chemical industry, it is related to a kind of coal tar oil ingredient continuous separation technology and device.
Background technology
Coal tar is most valuable Organic Chemicals, and some products can not or can not be economically from petrochemical materials
In obtain, anthracene, acenaphthene and the pyrene that such as coking industry produces can meet more than the 90% of world's aggregate demand, industrial carbazole
Almost 100% ground is derived from coke chemicals with quinoline.Therefore, coai-tar product be seized of in world's industrial chemicals extremely important
Status.Coal tar can be divided into neutral compound, acid compound, oxygenatedchemicalss (content is very low) according to chemical composition and contain
Sulphur compound (content is very low).Neutral compound is commonly called as neutral oil, mainly includes aliphatic compound and arene
Compound.Aliphatic compound is the important component part of the fuel oil such as gasoline, diesel oil, is that hydrogenation produces high cetane number diesel oil
Good raw material；Compound fragrant hydrocarbon have petrochemical industry can not obtain or can not the economy naphthalene, anthracene, phenanthrene and the pyrene that obtain contour attached
Value added fine chemicals.Acid compound is primarily referred to as the phenolic compound in coal tar, and phenolic compound is important chemical industry
Raw material, has extensively at aspects such as synthetic fibers, engineering plastics, pesticide, medicine, preservative, plasticizer, spice and dyestuff intermediates
General purposes, belongs to high added value fine chemical product.More than being based on, isolate the higher neutral chemical combination of content from coal tar
Thing and acid compound tool have very important significance.
Traditional coal tar separation method has solvent extraction, the way of distillation and recrystallization method etc..But these traditional methods exist
Have during coal tar processing that course of processing energy consumption is big, multi-process handling and numerous and diverse, each Component seperation of product and utilization ratio
The problems such as relatively low, phenol wastewater amount is big, environmental pollution is serious.For example, carry " acid-base method " during phenol and put forward phenol method/work
Skill is complicated, and it mainly includes：The workshop sections such as the extraction of crude phenols, the purification of the purification of phenates, the decomposition of phenates and crude phenols, are related to equipment
Many, multi-process handling and numerous and diverse, energy consumption is big, and cost of investment is high, carries phenol efficiency is low, and phenol wastewater amount is big, environmental pollution is serious etc.
Problems.In addition to " acid-base method " carries phenol, industrialized also have Recovery by Solvent Extraction Methold phenol technique, but the method/technique is deposited
In solvent consumption greatly, the problems such as equipment corrosion is serious.
Chinese patent CN104845651A methods described is the component separation method of coal tar, is prepared using silica gel as filler
Chromatographic column, carries out eluting separation using four kinds of solvents to going up excellent chromatographic column, respectively obtains saturation light component, fragrant group
Point, light polar compound and weight polar compound.This invention is a kind of detached method of coal tar crude, and the boiling range of four kinds of fractions is wider,
It is unfavorable for the fine separation of coal tar and the identification of composition.
A kind of extraction phenols chemical combination from liquefied coal coil or coal tar is described in Chinese invention patent CN102219649A
The method of thing, distillation processes liquefied coal coil or coal tar, cuts<260 DEG C of fraction, extractant is mixed with this fraction, is layered,
Separate and collect the extraction oxidant layer containing phenolic compound；Multistage back extraction extraction is carried out to the phenolic compound in extraction oxidant layer,
Obtain back washing agent-phenol solution and extractant；Above-mentioned back washing agent-phenol solution is separated by rectification, reclaims back washing agent and recycle, and
Separate and obtain crude phenols；Carried using vapor and remove the neutral oil carried secretly in phenolic compound, finally give crude phenols product, and slightly
Phenol purity is relatively low, complex process.
Chinese invention patent CN102492451A methods described is the extraction separating method of high temperature coal-tar, and this invention is normal
Under the conditions of pressure, adopt No. 1 and No. 2 solvents carry out step extract and separate to remove the impurity in coal tar to coal tar, actually
Coal tar is not effectively separated in itself, simply eliminates the impurity in coal tar.
A kind of extraction separating method of high temperature coal-tar is described, using organic in Chinese invention patent CN102492451A
The method of solvent fractional extraction can achieve lightweight in coal tar, heavy ingredient dissolving and with raw coal tar in ash, coke powder with
And quinoline insolubles sharp separation comes.The above light components obtaining that separate are enriched whole high added values in raw coal tar
Polycyclic aromatic hydrocarbon and important hetero atom polycyclic organic compound, concentrated in heavy component in raw coal tar remove deash, coke powder
And the high-purity of quinoline insolubles refines asphalt component.
A kind of distillate dephenolizing process and its device is described, coal tar distillation evaporates in Chinese invention patent CN101475817A
Divide and be sufficiently mixed reaction with basic phenate salt, enter dephenolize tower, standing obtains mixing part and neutral phenol sodium；Mixing part and 10-12%
Diluted alkaline mixing after enter secondary dephenolize tower, mixture standing separation be basic phenate salt and washed mix part；Wash mixing part to enter
Enter dephenolize salt tower, enter basic phenate salt groove after dephenolize salt tower standing separation goes out the basic phenate salt of residual, obtain washes mixing
Part enters commercial naphthalene device and is processed further.
In sum, in current traditional coal Process of Tar Processing, energy consumption is big, multi-process handling and numerous and diverse, each component of product is divided
From, the problems such as phenol wastewater amount big, environmental pollution serious relatively low with utilization ratio, and it is detached new to be applied to coal tar
Or technology is that there is major defect, or being the main equipment development problem existing in commercial Application it is difficult to maximize industrial
Produce and cost of investment is high, laboratory stage can only be rested on.So, currently seek low energy consumption, low stain, high efficiency separation coal tar
The technology of oil has become as the task of top priority of Coal Chemical Industry low carbon development.
Content of the invention
For overcoming the problem in currently available technology, it is an object of the invention to provide a kind of coal tar oil ingredient is continuously separated work
Skill and device, this separating technology can achieve the efficiently separating of coal tar oil ingredient, energy saving technology is notable, operating condition is gentle, no useless
Water discharge, environmental protection, environmentally friendly, equipment investment is few, is easily enlarged production scale.
To achieve these goals, the technical solution used in the present invention is as follows：
A kind of coal tar oil ingredient continuous separation device, including coal tar storage tank, solvent orange 2 A storage tank, solvent B preheating storage
Tank, coal tar extractive reaction kettle, asphalt component separation storage tank, asphalt component storage tank, the first adsorption tower, the second adsorption tower, solvent orange 2 A
The remaining part storage tank of extraction absorption, neutral oil Component seperation tower, neutral oil column overhead return tank, neutral oil tank, solvent B elution fraction
Storage tank, crude phenols Component seperation tower, crude phenols column overhead return tank and crude phenols storage tank；
Described coal tar extractive reaction kettle top is connected with coal tar storage tank and solvent orange 2 A storage tank, and coal tar extraction is anti-
Answer bottom portion separate with asphalt component tank top be connected, asphalt component separation tank bottom respectively with the first adsorption tower and second
Absorption top of tower is connected；
The pre- hot tank of solvent B is connected with the first adsorption tower and the second absorption top of tower；
First adsorption tower and the second absorption tower bottom are respectively connected with the remaining part storage tank of solvent orange 2 A extraction absorption, solvent B elution fraction
Storage tank and absorption mix part storage tank with desorption；
The remaining part storage tank of solvent orange 2 A extraction absorption is connected with neutral oil Component seperation tower, neutral oil Component seperation top of tower and
Neutral oil column overhead backflow tank top be connected, neutral oil column overhead backflow pot bottom respectively with neutral oil Component seperation tower and solvent
A storage tank is connected；Neutral oil Component seperation tower bottom of towe is connected with neutral oil tank；
Solvent B elution fraction storage tank is connected with crude phenols Component seperation tower；Crude phenols Component seperation column overhead and crude phenols Component seperation
Column overhead return tank is connected；Crude phenols Component seperation tower bottom of towe is connected with crude phenols storage tank.
The present invention is further improved by, and also includes absorption and mixes part storage tank, mixing part knockout tower with desorption and mix
Close part column overhead return tank；
Absorption is connected with mixing part knockout tower with desorption mixing part storage tank；Mixing part separates column overhead and mixes part knockout tower
Overhead reflux tank top is connected；
Mixing part knockout tower overhead reflux pot bottom is divided into two-way, and a road separates column overhead with mixing part and is connected, Ling Yilu
Hot tank pre- with solvent B is connected；Mixing part knockout tower bottom of towe is entered with the first adsorption tower and the second absorption top of tower solvent orange 2 A extract
Tower tube road is connected.
The present invention is further improved by, described mixing part separate column overhead blended part knockout tower overhead condenser with
Mixing part knockout tower overhead reflux tank top is connected；Mixing part knockout tower bottom of towe is provided with mixing part knockout tower tower bottom reboiler,
And mix part knockout tower tower bottom reboiler gateway to be all connected with mixing part knockout tower bottom of towe.
The present invention is further improved by, and described crude phenols Component seperation column overhead backflow pot bottom is divided into two-way, a road
It is connected with crude phenols Component seperation column overhead；Another road hot tank pre- with solvent B is connected；Described asphalt component separation storage tank is also connected with
There is asphalt component storage tank.
The present invention is further improved by, and described neutral oil Component seperation tower bottom of towe is provided with neutral oil tower bottom of towe and boils
Device, and neutral oil tower tower bottom reboiler gateway is all connected with neutral oil Component seperation tower bottom of towe；Crude phenols Component seperation tower tower
Bottom is provided with crude phenols Component seperation tower tower bottom reboiler, and crude phenols Component seperation tower tower bottom reboiler gateway all with crude phenols group
Knockout tower bottom of towe is divided to be connected.
The present invention is further improved by, described neutral oil Component seperation top of tower through neutral oil column overhead condenser with
Neutral oil column overhead backflow tank top is connected；Neutral oil Component seperation tower bottom of towe is through neutral oil ingredient discharging condenser and neutral oil
Storage tank is connected；Crude phenols Component seperation column overhead is flowed back with crude phenols Component seperation column overhead through crude phenols Component seperation column overhead condenser
Tank is connected；Crude phenols Component seperation tower bottom of towe is connected with crude phenols storage tank through crude phenols component discharging condenser.
A kind of coal tar oil ingredient continuous separation technology, comprises the following steps：
1) solvent orange 2 A is mixed with coal tar and extraction：By coal tar and solvent orange 2 A in coal tar extractive reaction kettle extraction, continuous
Stirring, heating obtain mixture, and wherein, coal tar is 1 with the volume ratio of solvent orange 2 A：1～1：20；
2) in solvent orange 2 A mixture asphalt component separation：By step 1) mixture injection asphalt component separation storage tank, warp
Cross after separating, obtain asphalt component and the solvent orange 2 A extract removing asphalt component；
3) solvent orange 2 A extract adsorption tower adsorbing separation：By step 2) removing asphalt component solvent orange 2 A extract through solvent
After the pressurization of A extract feed pump, send in the first adsorption tower and carry out adsorbing separation, after absorption, mixed liquor is stored in solvent orange 2 A extraction
In the remaining part storage tank of absorption；
4) rectification of neutral oil ingredient separates：By step 3) mixed liquor that obtains of adsorbing separation extracts absorption through solvent orange 2 A
Remaining part feed pump pressurization enters neutral oil Component seperation tower, obtains neutral oil ingredient and solvent orange 2 A；Wherein, neutral oil ingredient divides
Collect neutral oil product from tower tower reactor and be stored in neutral oil tank, overhead collection solvent orange 2 A is back in solvent orange 2 A storage tank；
5) elution fraction of solvent B separates：When solvent orange 2 A extraction has been adsorbed, when switching to solvent B eluting, solvent B is first through solvent
After the preheating of B pre- hot tank, pressurizeing through solvent B feed pump to enter carries out eluting separation in the first adsorption tower, before eluting is stablized
To eluent be stored in absorption and mix in part storage tank with desorption, eluting stably after the eluent that obtains be stored in solvent B eluting
In part storage tank；
While the elution fraction of solvent B separates, by step 2) the solvent orange 2 A extract of removing asphalt component extract through solvent orange 2 A
After taking the pressurization of thing feed pump, send in the second adsorption tower and carry out adsorbing separation, after absorption, mixed liquor is stored in solvent orange 2 A extraction absorption
In remaining part storage tank；
6) rectification of solvent B elution fraction separates：The eluent of solvent B pressurizes through solvent B elution fraction feed pump and enters crude phenols
Component seperation tower, is isolated to solvent B and crude phenols, and wherein crude phenols Component seperation tower tower reactor is collected crude phenols product and is stored in crude phenols
Storage tank, overhead collection solvent B is back in the pre- hot tank of solvent B；
7) the mutual switching of the absorption of solvent orange 2 A extract and solvent B eluting：In the first adsorption tower or the second adsorption tower solvent orange 2 A
Before switching to solvent B eluting stable after the completion of extract absorbing process, or after the completion of elution processes, switch to solvent orange 2 A extract
Before absorption is stable, Ta Nei also nubbin solvent orange 2 A extract or solvent B eluent, in order to ensure the remaining part of solvent orange 2 A absorption with molten
The quality of agent B elution fraction, thus must absorption and elution processes stably before mix part and in addition produced collection, therefore this is mixed
Part is collected to be stored in adsorb and is mixed part storage tank with desorption；
8) rectification that absorption mixes part with eluting separates：It is mixed that absorption mixes the pressurization entrance of part blended part feed pump with eluting
Close part knockout tower, be isolated to solvent B and mix part except the residue of solvent B, wherein overhead collection solvent B reuse is to solvent
The pre- hot tank of B, tower reactor is collected mixing part and is removed the residue of solvent B through bottom of towe discharging pump pressurization entrance the first adsorption tower and the second suction
The solvent orange 2 A extract of receipts tower top enters tower tube road and carries out adsorbing separation together with solvent orange 2 A extract；
9) the first adsorption tower and the second adsorption tower mutually switch, and carry out absorption simultaneously and realize absorption and eluting with elution action
It is carried out continuously；
Step 1) to step 9) it is capable of being continuously separated of coal tar, obtain asphalt component, neutral oil ingredient and thick
Phenol component.
The present invention is further improved by, and described solvent orange 2 A is the mixture of one or more of the alkane of C5～C8；
Wherein, the alkane of C5～C8 includes n-alkane or branched paraffin；
Described coal tar is coalite tar, medium temperature coal tar or high temperature coal-tar；
The temperature range of described coal tar extractive reaction kettle heating is 60～100 DEG C；
Described solvent orange 2 A extract feed pump moulding pressure scope is 0.2MPa～10MPa；
All it is filled with silica gel in described first adsorption tower and the second adsorption tower.
The present invention is further improved by, and described solvent B is one of ethyl acetate, toluene, ethanol, methanol or several
The mixture planted；
The pre- hot tank preheating temperature scope of described solvent B is 20～60 DEG C.
The present invention is further improved by, and described solvent B feed pump moulding pressure scope is 0.2MPa～10MPa；
Described solvent orange 2 A extract is 0.2～0.5MPa through solvent orange 2 A extract feed pump moulding pressure scope, feeding temperature
Scope is 60～100 DEG C；
The remaining part feed pump moulding pressure scope of described solvent orange 2 A extraction absorption is 0.2MPa～10MPa, temperature be 60～
100℃；
Described solvent B elution fraction feed pump moulding pressure scope is 0.2～0.5MPa, and feed temperature range is 20-60 DEG C；
Described mixing part feed pump moulding pressure scope is 0.2～0.5MPa, and feed temperature range is 20-60 DEG C.
Compared with prior art, the device have the advantages that：The present invention pass through arrange coal tar extractive reaction kettle with
Asphalt component knockout drum, is carried out mixing, is extracted, separates using solvent orange 2 A and coal tar, can obtain asphalt component；By setting
Adsorption tower, makes the solvent orange 2 A extract of removing asphalt component pass through adsorption tower after the pressurization of solvent orange 2 A extract feed pump, through inhaling
Fufen enters in neutral oil tower from the mixed liquor obtaining and carries out rectification, obtains neutral oil ingredient；By absorption after solvent B is pressurizeed
Tower eluting solvent A extracts absorbed component, and the eluent after eluting enters crude phenols Component seperation tower, separates through rectification and obtains crude phenols
Component, completes the separation to coal tar oil ingredient.Mutual switching is entered by the double adsorption tower of setting, is adsorbed respectively simultaneously and wash
De- operation is realized absorption and is carried out continuously with eluting.This apparatus structure is simple, take up an area little it is easy to expanding production.
Further, neutral oil column overhead reflux pump is pre- with solvent B with solvent orange 2 A storage tank respectively with crude phenols column overhead reflux pump
Hot tank is connected so that the solvent in solvent tank can reuse.
Extractive reaction kettle is combined by the present invention with separated from bitumen tank, is carried out mixing, is extracted, stirs using solvent orange 2 A and coal tar
Mix, separate, asphalt component can be obtained；By arranging adsorption tower, the solvent orange 2 A extract making removing asphalt component is through solvent orange 2 A
Pass through adsorption tower after the pressurization of extract feed pump, enter in neutral oil tower through the mixed liquor that adsorbing separation obtains and carry out rectification, obtain
To neutral oil ingredient；Solvent B is extracted absorbed component by adsorption tower eluting solvent A after the pressurization of solvent B feed pump, through eluting
Eluent afterwards enters crude phenols Component seperation tower, separates through rectification and obtains crude phenols component, solves existing coal tar processing process
Present in energy consumption is big, multi-process handling and complicated, each Component seperation of product and utilization ratio is relatively low, serious the asking of environmental pollution
Topic.The present invention is green separation technique, does not produce waste water, waste residue and waste gas, and the operating condition of technique is gentle, easy, work
Skill and equipment manufacturing cost is low, less investment.
Brief description
Fig. 1 is the extraction absorption of coal tar Component seperation solvent orange 2 A and the solvent B elution processes flow process of the present invention；
Fig. 2 is the remaining part of coal tar Component seperation solvent orange 2 A extraction absorption and the solvent B elution fraction rectification process stream of the present invention
Journey；
Fig. 3 is that the coal tar Component seperation absorption of the present invention mixes part rectification process flow process with eluting；
Fig. 4 is the total ions chromatogram of neutral oil ingredient；
Fig. 5 is the total ions chromatogram of crude phenols component；
Fig. 6 is the hot weightless picture of asphalt component；
In figure, 1, coal tar storage tank, 2, solvent orange 2 A storage tank；3rd, the pre- hot tank of solvent B；4th, coal tar extractive reaction kettle；
5th, asphalt component separation storage tank；6th, solvent orange 2 A feed pump；7th, solvent orange 2 A extract feed pump；8th, solvent B feed pump；9th, asphalt component
Storage tank；10th, the first adsorption tower；11st, the second adsorption tower；12nd, the remaining part storage tank of solvent orange 2 A extraction absorption；13rd, solvent orange 2 A extraction absorption
Remaining part feed pump；14th, neutral oil Component seperation tower；15th, neutral oil column overhead condenser；16th, neutral oil column overhead return tank；
17th, neutral oil column overhead reflux pump；18th, neutral oil tower tower bottom reboiler；19th, neutral oil ingredient discharging condenser；20th, neutral oil
Component discharging pump；21st, neutral oil tank；22nd, solvent B elution fraction storage tank；23rd, solvent B elution fraction feed pump；24th, crude phenols component
Knockout tower；25th, crude phenols Component seperation column overhead condenser；26th, crude phenols column overhead return tank；27th, crude phenols column overhead reflux pump；
28th, crude phenols tower tower bottom reboiler；29th, crude phenols component discharging condenser；30th, crude phenols component discharging pump；31st, crude phenols storage tank；32nd, inhale
Attached with desorption mix part storage tank；33rd, mix part feed pump；34th, mix part knockout tower；35th, mix part column overhead condenser；36、
Mixing part column overhead return tank；37th, mix part column overhead reflux pump；38th, mix part tower tower bottom reboiler；39th, mix part tower tower
Bottom discharging pump.
Specific embodiment
The present invention is described in further detail by embodiment below in conjunction with accompanying drawing.
Heretofore described all raw materials all carry Liquid level with intermediate products and storage tank；Described coal tar extraction
Reactor band heating mantle and agitating device；Described solvent orange 2 A head tank carries heating mantle；Described adsorption tower bottom respectively with three
Pipeline is connected.
Referring to Fig. 1, Fig. 2 and Fig. 3, a kind of coal tar oil ingredient continuous separation device includes：Coal tar storage tank 1, solvent orange 2 A
Storage tank 2, the pre- hot tank of solvent B 3, coal tar extractive reaction kettle 4, asphalt component separation storage tank 5, solvent orange 2 A feed pump 6, solvent orange 2 A extraction
Thing feed pump 7, solvent B feed pump 8, asphalt component storage tank 9, the first adsorption tower 10, the second adsorption tower 11, solvent orange 2 A extraction is taken to inhale
Attached residue part storage tank 12, the remaining part feed pump 13 of solvent orange 2 A extraction absorption, neutral oil Component seperation tower 14, neutral oil column overhead are cold
Condenser 15, neutral oil column overhead return tank 16, neutral oil column overhead reflux pump 17, neutral oil tower tower bottom reboiler 18, neutral oil
Component discharging condenser 19, neutral oil ingredient discharging pump 20, neutral oil tank 21, solvent B elution fraction storage tank 22, solvent B eluting
Part feed pump 23, crude phenols Component seperation tower 24, crude phenols Component seperation column overhead condenser 25, crude phenols column overhead return tank 26, thick
Phenol column overhead reflux pump 27, crude phenols tower tower bottom reboiler 28, crude phenols component discharging condenser 29 are crude phenols component discharging pump 30, thick
Phenol storage tank 31；Absorption with desorption mix part storage tank 32, mixing part feed pump 33, mix part knockout tower 34, mix part column overhead cold
Condenser 35, mixing part column overhead return tank 36, mixing part column overhead reflux pump 37, mixing part tower tower bottom reboiler 38 and mixing
Part tower bottom of towe discharging pump 39.
Referring to Fig. 1, coal tar storage tank 1 bottom is connected with coal tar extractive reaction kettle 4 top side；Solvent orange 2 A storage tank 2
Bottom is connected with solvent orange 2 A feed pump 6 entrance, and solvent orange 2 A feed pump 6 is exported and is connected with coal tar extractive reaction kettle 4 top opposite side；
Coal tar extractive reaction kettle 4 bottom is separated storage tank 5 top and is connected with asphalt component；Asphalt component separation storage tank 5 one side bottom with
Asphalt component storage tank 9 is connected；Another side bottom of asphalt component separation storage tank 5 is connected with solvent orange 2 A extract feed pump 7 entrance, molten
Agent A extract feed pump 7 is exported and is connected with the first adsorption tower 10 and the second adsorption tower 11 top respectively；The pre- hot tank of solvent B 3 bottom
Portion is connected with solvent B feed pump 8 entrance, solvent B feed pump 8 export respectively with the first adsorption tower 10 and the second adsorption tower 11 top
It is connected；Remaining part storage tank 12, solvent B elution fraction storage tank 22 and the suction with solvent orange 2 A extraction absorption respectively of first adsorption tower 10 bottom
Attached with desorption mixing part storage tank 32 be connected；Second adsorption tower 11 bottom remaining part storage tank 12, solvent with solvent orange 2 A extraction absorption respectively
B elution fraction storage tank 22 and absorption are connected with desorption mixing part storage tank 32.
Referring to Fig. 2, the remaining part storage tank 12 of solvent orange 2 A extraction absorption remaining part feed pump 13 entrance phase with solvent orange 2 A extraction absorption
Even, the remaining part feed pump 13 of solvent orange 2 A extraction absorption is exported and is connected with neutral oil Component seperation tower 14；Neutral oil Component seperation tower 14
Top is connected with neutral oil column overhead condenser 15 top, is flowed back with neutral oil column overhead in neutral oil column overhead 15 condenser bottom
Tank 16 top is connected；Neutral oil column overhead return tank 16 bottom is connected with neutral oil column overhead reflux pump 17 entrance, neutral oil tower
Overhead reflux pump 17 outlet is divided into two-way, and a road is connected with neutral oil Component seperation tower 14 top；Neutral oil column overhead reflux pump
17 another roads of outlet are connected with solvent orange 2 A storage tank 2；Neutral oil tower tower bottom reboiler 18 gateway all with neutral oil Component seperation tower 14
Bottom of towe is connected；Neutral oil Component seperation tower 14 bottom of towe is connected with neutral oil ingredient discharging condenser 19 entrance；Neutral oil ingredient goes out
Material condenser 19 is exported and is connected with neutral oil ingredient discharging pump 20 entrance, and neutral oil ingredient discharging pump 20 exports and neutral oil tank
21 are connected；Solvent B elution fraction storage tank 22 is connected with solvent B elution fraction feed pump 23 entrance, and solvent B elution fraction feed pump 23 exports
It is connected with crude phenols Component seperation tower 24；Crude phenols Component seperation tower 24 tower top and crude phenols Component seperation column overhead condenser 25 top phase
Even, crude phenols Component seperation tower 25 overhead condenser bottom is connected with crude phenols Component seperation column overhead return tank 26 top；Crude phenols group
Knockout tower return tank of top of the tower 26 bottom is divided to be connected with crude phenols Component seperation column overhead reflux pump 27 entrance, crude phenols Component seperation tower tower
Top reflux pump 27 outlet is divided into two-way, and a road is connected with crude phenols Component seperation tower 24 tower top；Crude phenols Component seperation column overhead flows back
Pump 27 exports another road hot tank 3 pre- with solvent B and is connected；Crude phenols Component seperation tower tower bottom reboiler 28 gateway all with crude phenols group
Knockout tower 24 bottom of towe is divided to be connected；Crude phenols Component seperation tower 24 bottom of towe is connected with crude phenols component discharging condenser 29 entrance；Crude phenols group
Separate material condenser 29 and export and be connected with crude phenols component discharging pump 30 entrance, crude phenols component discharging pump 30 exports and crude phenols storage tank 31
It is connected；
Referring to Fig. 3, absorption is connected with mixing part feed pump 33 entrance with desorption mixing part storage tank 32, mixes part feed pump 33
Outlet is connected with mixing part knockout tower 34；Mix part knockout tower 34 tower top and mix part knockout tower overhead condenser 35 top phase
Even, mixing part knockout tower overhead condenser 35 bottom is connected with mixing part knockout tower return tank of top of the tower 36 top；Mixing part separates
Column overhead return tank 36 bottom is connected with mixing part knockout tower overhead reflux pump 37 entrance, mixes part knockout tower overhead reflux pump 37
Outlet is divided into two-way, and a road is connected with mixing part knockout tower 34 tower top；Mixing part knockout tower overhead reflux pump 37 exports another road
Hot tank 3 pre- with solvent B is connected；Mixing part knockout tower tower bottom reboiler 38 gateway all with mix part knockout tower 34 bottom of towe phase
Even；Mixing part knockout tower 34 bottom of towe is connected with mixing part tower bottom of towe discharging pump 39 entrance, and mixing part tower bottom of towe discharging pump 39 exports
Enter tower tube road and be connected with the first adsorption tower, the second adsorption tower solvent overhead A extract.
The coal tar Component seperation technique of the present invention comprises the following steps：
First, solvent orange 2 A extraction absorption and solvent B elution processes flow process
(1) solvent orange 2 A extraction and absorbing process flow process
Coal tar raw material seriality is stored up into coal tar storage tank 1 by certain flow, then coal tar raw material is injected coal
Tar extraction reactor 4.Solvent orange 2 A pumps into coal tar extractive reaction kettle 4 by solvent orange 2 A storage tank 2 through solvent orange 2 A feed pump 6 simultaneously.Open
Stirring makes solvent orange 2 A be mixed evenly with coal tar raw material, controls coal tar extractive reaction kettle 4 temperature to be 60～100 DEG C, extraction is certain
After time.Solvent orange 2 A and coal tar raw material mixed liquor are put into asphalt component knockout drum 5, asphalt component is through asphalt component knockout drum 5
Bottom produces, and enters asphalt component storage tank 9 and stores.Except the solvent orange 2 A extract of asphalt component is by asphalt component knockout drum 5 overhead stream
Go out, be forced into through solvent orange 2 A extract feed pump 7 that 0.2～10MPa pumps into the first adsorption tower 10 or the second adsorption tower 11 is inhaled
Attached, after after adsorbing separation, the remaining part of solvent orange 2 A extraction absorption is collected through the first adsorption tower 10 or the extraction of the second adsorption tower 11 bottom of towe, enter
Enter the remaining part storage tank 12 of solvent orange 2 A extraction absorption to store.First adsorption tower 10 and the second adsorption tower 11 rotation are adsorbed and eluting
Operation (when i.e. the first adsorption tower 10 is adsorbed, the second adsorption tower 11 carries out eluting, and vice versa), realizes continuous operation.
(2) solvent B elution processes flow process
After switching to solvent B eluting stable after the completion of the absorption of solvent orange 2 A extract, solvent B is pre- through solvent B pre- hot tank 3
Heat, to after 20～60 DEG C, is forced into 0.2MPa～10MPa through solvent B feed pump 8 pump and pumps into the first adsorption tower 10 or the second absorption
Tower 11 tower top, to tower internal solvent A absorption, surplus material carries out eluting, by solvent B elution fraction by the first adsorption tower 10 or the second absorption
After tower 11 bottom of towe is collected, enter solvent B elution fraction storage tank 22 and store.
(3) technological process when solvent orange 2 A/B absorption and eluting switching
Before switching to solvent B eluting stable after the completion of the first adsorption tower 10 or the second adsorption tower 11 solvent adsorption technique,
Or before switching to the absorption of solvent orange 2 A extract stable after the completion of elution processes, Ta Nei also nubbin solvent orange 2 A extraction absorption is remaining
Liquid or solvent B eluent, in order to ensure the quality of the remaining part of solvent orange 2 A extraction absorption and solvent B elution fraction, therefore must by absorption with
Before elution processes are stable, in addition mixing part is produced collection.Therefore in the first adsorption tower 10 or the extraction of the second adsorption tower 11 solvent orange 2 A
Solvent orange 2 A is switched to extract before switching to solvent B elution processes stable after the completion of thing absorbing process or after the completion of solvent B elution processes
Before taking thing absorption stable, before stablizing with eluting from the solvent orange 2 A/B absorption of the first adsorption tower 10 or the second adsorption tower 11 bottom of towe
Mixing part is collected in absorption and mixes part storage tank 32 and store with being desorbed.
2nd, the remaining part of solvent orange 2 A extraction absorption and solvent B elution fraction rectification process flow process
(1) remaining part rectification (neutral oil production) technique of solvent orange 2 A extraction absorption
When the solvent orange 2 A extract absorbing process normal table of adsorption tower runs, from the remaining part storage of solvent orange 2 A extraction absorption
Remaining part of solvent orange 2 A absorption of tank 12 pumps into neutral oil Component seperation tower 14 by remaining part feed pump 13 pressurization of solvent orange 2 A extraction absorption
Carry out rectification to separate.Neutral oil Component seperation tower 14 tower top output solvent orange 2 A steam, solvent orange 2 A steam is through neutral tower top complete condenser 15
All it is condensed into liquid phase, the solvent orange 2 A after entirely coagulating enters neutral oil column overhead return tank 16, then through neutral oil column overhead reflux pump
17 parts are back to neutral oil Component seperation tower 14 tower top by certain reflux ratio, and another part returns to solvent orange 2 A storage tank 2 times
With.
A neutral oil part for neutral oil 14 outputs of Component seperation tower is through neutral oil tower tower bottom reboiler 18 heating and gasifying
After be back in neutral oil Component seperation tower 14, another part is as tower reactor product output.The neutral oil ingredient of output is cold through discharging
Condenser 19 cools down, and the neutral oil after cooling pumps out through neutral oil ingredient discharging pump 20, enters neutral oil tank 21 as product and stores up
Deposit.
(2) solvent B elution fraction rectification (crude phenols production) technological process
When adsorption tower solvent B elution processes normal table runs, from the solvent B eluting of solvent B elution fraction storage tank 22
Part enters crude phenols Component seperation tower 24 by solvent B elution fraction feed pump 23 and carries out rectification separation.Crude phenols Component seperation tower 24 tower top
Output solvent B steam, solvent B steam is all condensed into liquid phase through crude phenols Component seperation column overhead condenser 25, molten after entirely coagulating
Agent B enters crude phenols column overhead return tank 26, then returns by certain reflux ratio through crude phenols knockout tower overhead reflux pump 27 part
It flow to crude phenols Component seperation tower 24 tower top, another part returns to the pre- hot tank of solvent B 3.
A crude phenols part for crude phenols 24 outputs of Component seperation tower is after crude phenols knockout tower tower bottom reboiler 28 heating and gasifying
It is back in crude phenols Component seperation tower 24, another part is as tower reactor product output.The crude phenols of output condense through crude phenols component discharging
Device 29 cools down, and the crude phenols after cooling enter crude phenols storage tank 31 through crude phenols component discharging pump 30 pump as product.
3rd, absorption mixes part rectification process with eluting
Before switching to solvent B eluting stable after the completion of the first adsorption tower 10 or the second adsorption tower 11 solvent adsorption technique,
Or before switching to the absorption of solvent orange 2 A extract stable after the completion of elution processes, during this period, mix with desorption when being collected in adsorb
Before the solvent orange 2 A/B absorb-elute of part storage tank 32 is stable mixing part to be achieved a certain amount of after, mixing is entered by mixing part feed pump 33
Part knockout tower 34 rectification separates.Mixing part knockout tower 34 tower top output solvent B steam, solvent B steam blended part column overhead is cold
Condenser 35 is all condensed into liquid phase, and the solvent B after entirely coagulating enters mixing part column overhead return tank 36, then blended part column overhead
By certain reflux ratio blowback to mixing part knockout tower 34 tower top, another part returns to solvent B preheating to reflux pump 37 part
Storage tank 3.
After mixing 34 output separation solvent B of part knockout tower, remaining a part of blended part tower tower bottom reboiler 38 heats
It is back to after gasification in mixing part knockout tower 34, another part is as tower reactor discharging.Tower reactor discharging blended part tower bottom of towe discharging pump
The solvent orange 2 A extract on 39 blowback the first adsorption towers 10 and second absorption tower 11 top enters tower tube road, in the first adsorption tower 10 or the second
When adsorption tower 11 solvent orange 2 A absorbing process normal table runs, separate storage tank 5 upper solvent A extract one with from asphalt component
Act the first adsorption tower 10 or the second adsorption tower 11 is adsorbed.
The mixture of the single alkane in the alkane for C5～C8 for the described solvent orange 2 A or several single alkane be (C5～C8's
Alkane includes n-alkane or branched paraffin).
Described solvent B is the mixture of one or more of ethyl acetate, toluene, ethanol, methanol.
It is filled with silica gel in the first described adsorption tower 10 and the second adsorption tower 11.
Described neutrality oil ingredient, crude phenols component and asphalt component are product.The solvent orange 2 A simultaneously obtaining and solvent B are permissible
Recycle.
In order to the effect of the present invention is described, following examples carry out middle low temperature coal tar using coal tar Component seperation new technology
Oil ingredient separation test, in order to accurate analytical separation product, using gas chromatograph-mass spectrometer (GC-MS) and thermal analyzer difference
Composition to product and thermal weight loss process are measured.It is now to take from the coal tar of semi-coke factory of northern Shensi Fugu County with experimental raw
(heavy oil) carries out separating as experimental subject, and heavy oil (tar depositing reservoir subsurface layer oil) is shown in Table 1 by the fundamental property that GB measures.
The fundamental property of table 1 coal tar heavy oil
Note：* minusing
Using coal tar oil ingredient continuous separation technology of the present invention, select solvent orange 2 A (the specially alkane of C7) and solvent B respectively
(specially polar solvent ethyl acetate) is eluant, and silica gel is adsorbent, the neutral oil ingredient in coal tar in separating, crude phenols
Component and asphalt component.
Take a certain amount of coal tar to be tested according to foregoing schemes, obtain after off-test and respectively to from products pot
Neutral oil ingredient and each 1mL of crude phenols component, then the acetone solution with 5mL, then carry out GC-MS analysis, analysis result is shown in figure
4th, Fig. 5 and table 2 and table 3.The asphalt component obtaining weighs 5mg and is analyzed with TG, and analysis result is shown in Fig. 6.
Coalite tar neutral oil composition in table 2
Coalite tar crude phenols composition in table 3
The present invention has carried out product analysis to the peak of peak 1-37 in Fig. 4, and the peak being 1-24 to peak number in Fig. 5 is carried out
Product analysis, the peak number of in figure can find in table.
From the experimental studies results of Fig. 4, Fig. 5 and Fig. 6, the coal tar oil ingredient using the present invention is continuously separated new work
Skill, can efficiently separate the neutral oil ingredient obtaining in coal tar, crude phenols component and asphalt component, compared with traditional method, this
Invention is a kind of method that green is continuously separated coal tar, does not produce waste water, waste residue and waste gas and relatively conventional separation of device fills
Put the little, small investment of occupation of land, be easily enlarged production.Simultaneously instant invention overcomes energy consumption present in existing coal tar processing process
Greatly, multi-process handling and numerous and diverse, product each component low separation efficiency, the problems such as phenol wastewater amount is big, environmental pollution is serious.
Claims (10)
1. a kind of coal tar oil ingredient continuous separation device is it is characterised in that include coal tar storage tank (1), solvent orange 2 A storage tank
(2), the pre- hot tank of solvent B (3), coal tar extractive reaction kettle (4), asphalt component separation storage tank (5), asphalt component storage tank (9),
First adsorption tower (10), the second adsorption tower (11), the remaining part storage tank (12) of solvent orange 2 A extraction absorption, neutral oil Component seperation tower
(14), neutral oil column overhead return tank (16), neutral oil tank (21), solvent B elution fraction storage tank (22), crude phenols Component seperation tower
(24), crude phenols column overhead return tank (26) and crude phenols storage tank (31)；
Described coal tar extractive reaction kettle (4) top is connected with coal tar storage tank (1) and solvent orange 2 A storage tank (2), and coal tar extracts
Take reactor (4) bottom to separate storage tank (5) top with asphalt component to be connected, asphalt component separation storage tank (5) bottom is respectively with the
One adsorption tower (10) is connected with the second adsorption tower (11) top；
The pre- hot tank of solvent B (3) is connected with the first adsorption tower (10) and the second adsorption tower (11) top；
First adsorption tower (10) and the second adsorption tower (11) bottom are respectively connected with the remaining part storage tank (12) of solvent orange 2 A extraction absorption, molten
Agent B elution fraction storage tank (22) and absorption mix part storage tank (32) with desorption；
The remaining part storage tank (12) of solvent orange 2 A extraction absorption is connected with neutral oil Component seperation tower (14), neutral oil Component seperation tower
(14) top is connected with neutral oil column overhead return tank (16) top, neutral oil column overhead return tank (16) bottom respectively with neutrality
Oil ingredient knockout tower (14) is connected with solvent orange 2 A storage tank (2)；Neutral oil Component seperation tower (14) bottom of towe and neutral oil tank (21) phase
Even；
Solvent B elution fraction storage tank (22) is connected with crude phenols Component seperation tower (24)；Crude phenols Component seperation tower (24) tower top and crude phenols
Component seperation column overhead return tank (26) is connected；Crude phenols Component seperation tower (24) bottom of towe is connected with crude phenols storage tank (31).
2. a kind of coal tar oil ingredient continuous separation device according to claim 1 is it is characterised in that also including absorption and taking off
Attached mixing part storage tank (32), mixing part knockout tower (34) and mixing part column overhead return tank (36)；
Absorption is connected with mixing part knockout tower (34) with desorption mixing part storage tank (32)；Mix part knockout tower (34) tower top and mix
Part knockout tower return tank of top of the tower (36) top is connected；
Mixing part knockout tower return tank of top of the tower (36) bottom is divided into two-way, and a road is connected with mixing part knockout tower (34) tower top, separately
One tunnel hot tank pre- with solvent B (3) is connected；Mixing part knockout tower (34) bottom of towe and the first adsorption tower (10) and the second adsorption tower
(11) solvent orange 2 A extract in top enters tower tube road and is connected.
3. a kind of coal tar oil ingredient continuous separation device according to claim 2 is it is characterised in that described mixing part separates
Tower (34) tower top blended part knockout tower overhead condenser (35) is connected with mixing part knockout tower return tank of top of the tower (36) top；Mixed
Close part knockout tower (34) bottom of towe and be provided with mixing part knockout tower tower bottom reboiler (38), and mix a part knockout tower tower bottom reboiler
(38) gateway is all connected with mixing part knockout tower (34) bottom of towe.
4. a kind of coal tar oil ingredient continuous separation device according to claim 1 is it is characterised in that described crude phenols component is divided
It is divided into two-way from column overhead return tank (26) bottom, a road is connected with crude phenols Component seperation tower (24) tower top；Another road and solvent B
Pre- hot tank (3) is connected；Described asphalt component separation storage tank (5) is also associated with asphalt component storage tank (9).
5. a kind of coal tar oil ingredient continuous separation device according to claim 1 it is characterised in that described neutrality oil ingredient
Knockout tower (14) bottom of towe is provided with neutral oil tower tower bottom reboiler (18), and neutral oil tower tower bottom reboiler (18) gateway is equal
It is connected with neutral oil Component seperation tower (14) bottom of towe；Crude phenols Component seperation tower (24) bottom of towe is provided with crude phenols Component seperation tower bottom of towe
Reboiler (28), and crude phenols Component seperation tower tower bottom reboiler (28) gateway all with crude phenols Component seperation tower (24) bottom of towe phase
Even.
6. a kind of coal tar oil ingredient continuous separation device according to claim 1 it is characterised in that described neutrality oil ingredient
Knockout tower (14) top is connected with neutral oil column overhead return tank (16) top through neutral oil column overhead condenser (15)；Neutral oil
Component seperation tower (14) bottom of towe is connected with neutral oil tank (21) through neutral oil ingredient discharging condenser (19)；Crude phenols Component seperation
Tower (24) tower top is connected with crude phenols Component seperation column overhead return tank (26) through crude phenols Component seperation column overhead condenser (25)；Slightly
Phenol Component seperation tower (24) bottom of towe is connected with crude phenols storage tank (31) through crude phenols component discharging condenser (29).
7. a kind of coal tar oil ingredient continuous separation technology is it is characterised in that comprise the following steps：
1) solvent orange 2 A is mixed with coal tar and extraction：Coal tar is extracted, continuously stirs in coal tar extractive reaction kettle (4) with solvent orange 2 A
Mix, heat and obtain mixture, wherein, coal tar is 1 with the volume ratio of solvent orange 2 A：1～1：20；
2) in solvent orange 2 A mixture asphalt component separation：By step 1) mixture injection asphalt component separation storage tank (5), warp
Cross after separating, obtain asphalt component and the solvent orange 2 A extract removing asphalt component；
3) solvent orange 2 A extract adsorption tower adsorbing separation：By step 2) removing asphalt component solvent orange 2 A extract through solvent orange 2 A extract
After taking thing feed pump (7) pressurization, send in the first adsorption tower (10) and carry out adsorbing separation, after absorption, mixed liquor is stored in solvent orange 2 A
In the remaining part storage tank (12) of extraction absorption；
4) rectification of neutral oil ingredient separates：By step 3) mixed liquor that obtains of adsorbing separation is remaining through solvent orange 2 A extraction absorption
Part feed pump (13) pressurization enters neutral oil Component seperation tower (14), obtains neutral oil ingredient and solvent orange 2 A；Wherein, neutral line of oils
Divide knockout tower (14) tower reactor to collect neutral oil product and be stored in neutral oil tank (21), overhead collection solvent orange 2 A is back to solvent orange 2 A and goes out
In storage tank (2)；
5) elution fraction of solvent B separates：When solvent orange 2 A extraction has been adsorbed, when switching to solvent B eluting, solvent B is first pre- through solvent B
After hot tank (3) preheating, pressurizeing through solvent B feed pump (8) to enter carries out eluting separation in the first adsorption tower (10), eluting is steady
The eluent obtaining before fixed is stored in absorption and mixes in part storage tank (32) with desorption, and the eluent obtaining after eluting is stable is stored in
In solvent B elution fraction storage tank (22)；
While the elution fraction of solvent B separates, by step 2) removing asphalt component solvent orange 2 A extract through solvent orange 2 A extract
After feed pump (7) pressurization, send in the second adsorption tower (11) and carry out adsorbing separation, after absorption, mixed liquor is stored in solvent orange 2 A extraction
In the remaining part storage tank (12) of absorption；
6) rectification of solvent B elution fraction separates：The eluent of solvent B pressurizes through solvent B elution fraction feed pump (23) and enters crude phenols
Component seperation tower (24), is isolated to solvent B and crude phenols, and wherein crude phenols Component seperation tower (24) tower reactor collects the storage of crude phenols product
It is stored in crude phenols storage tank (31), overhead collection solvent B is back in the pre- hot tank of solvent B (3)；
7) the mutual switching of the absorption of solvent orange 2 A extract and solvent B eluting：Molten in the first adsorption tower (10) or the second adsorption tower (11)
Before switching to solvent B eluting stable after the completion of agent A extract absorbing process, or solvent orange 2 A after the completion of elution processes, is switched to extract
Before taking thing absorption stable, Ta Nei also nubbin solvent orange 2 A extract or solvent B eluent, in order to ensure the remaining part of solvent orange 2 A absorption
With the quality of solvent B elution fraction, therefore must absorption and elution processes stably before mix part and in addition produced collection, therefore this
Mixing part is collected to be stored in adsorb and is mixed part storage tank (32) with desorption；
8) rectification that absorption mixes part with eluting separates：Absorption is mixed the pressurization of part blended part feed pump and enters mixing part with eluting
Knockout tower, is isolated to solvent B and mixes part except the residue of solvent B, wherein overhead collection solvent B reuse is pre- to solvent B
Hot tank (3), tower reactor is collected mixing part and is removed the residue of solvent B and pressurizes through bottom of towe discharging pump and enter the first adsorption tower (10) and the
The solvent orange 2 A extract that two absorption towers (11) are pushed up enters tower tube road and carries out adsorbing separation together with solvent orange 2 A extract；
9) the first adsorption tower and the second adsorption tower mutually switch, and carry out adsorbing continuous with eluting with elution action realization absorption simultaneously
Carry out；
Step 1) to step 9) it is capable of being continuously separated of coal tar, obtain asphalt component, neutral oil ingredient and crude phenols group
Point.
8. a kind of coal tar oil ingredient continuous separation technology according to claim 1 is it is characterised in that described solvent orange 2 A is C5
The mixture of one or more of the alkane of～C8；Wherein, the alkane of C5～C8 includes n-alkane or branched paraffin；
Described coal tar is coalite tar, medium temperature coal tar or high temperature coal-tar；
The temperature range of described coal tar extractive reaction kettle heating is 60～100 DEG C；
Described solvent orange 2 A extract feed pump (7) moulding pressure scope is 0.2MPa～10MPa；
All it is filled with silica gel in described first adsorption tower (10) and the second adsorption tower (11).
9. a kind of coal tar oil ingredient continuous separation technology according to claim 1 is it is characterised in that described solvent B is second
The mixture of one or more of acetoacetic ester, toluene, ethanol, methanol；
Described solvent B pre- hot tank (3) preheating temperature scope is 20～60 DEG C.
10. a kind of coal tar oil ingredient continuous separation technology according to claim 1 is it is characterised in that described solvent B feeds
Pump (8) moulding pressure scope is 0.2MPa～10MPa；
Described solvent orange 2 A extract is 0.2～0.5MPa through solvent orange 2 A extract feed pump (7) moulding pressure scope, feeding temperature model
Enclose for 60～100 DEG C；
Remaining part feed pump (13) the moulding pressure scope of described solvent orange 2 A extraction absorption is 0.2MPa～10MPa, temperature be 60～
100℃；
Described solvent B elution fraction feed pump (23) moulding pressure scope is 0.2～0.5MPa, and feed temperature range is 20-60 DEG C；
Described mixing part feed pump (33) moulding pressure scope is 0.2～0.5MPa, and feed temperature range is 20-60 DEG C.
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