CN106478379B - 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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- CN106478379B CN106478379B CN201610828429.9A CN201610828429A CN106478379B CN 106478379 B CN106478379 B CN 106478379B CN 201610828429 A CN201610828429 A CN 201610828429A CN 106478379 B CN106478379 B CN 106478379B
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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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- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Civil Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Structural Engineering (AREA)
- Working-Up Tar And Pitch (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
A kind of coal tar oil ingredient continuous separation technology and device are mixed with coal tar using solvent A in extraction reaction kettle, are extracted, are stirred, then separated to coal tar with the mixture of solvent A in knockout drum, obtain asphalt component；By the way that double adsorption towers are arranged, absorption is realized to be carried out continuously with what is eluted, it can make the solvent A extract for removing asphalt component by adsorption tower simultaneously, enter in neutral oil component knockout tower through the mixed liquor that adsorbing separation obtains and carry out rectifying, obtain neutral oil ingredient and recycling design A；The adsorption tower that solvent B is crossed to adsorption solvent A extract after the pressurization of solvent B feed pump elutes, and eluent enters crude phenols component knockout tower, through the isolated crude phenols component of rectifying and recycling design B.The present invention is green separation technique, does not generate waste water, waste residue and exhaust gas, and the operating condition of technique is mild, easy, technique and the advantages that equipment manufacturing cost is low, less investment.
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 technique
Coal tar is most valuable Organic Chemicals, some products cannot or cannot be economically from petrochemical materials
In obtain, anthracene, acenaphthene and the pyrene if coking industry produces can satisfy 90% or more of world's aggregate demand, industrial carbazole
Almost 100% ground comes from coke chemicals with quinoline.Therefore, coai-tar product is seized of extremely important in world's industrial chemicals
Status.Coal tar can be divided into neutral compound, acid compound, oxygenatedchemicals (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
Close object.Aliphatic compound is the important component of the fuel oil such as gasoline, diesel oil, is plus hydrogen produces high cetane number diesel oil
Good raw material；Compound fragrant hydrocarbon have petrochemical industry cannot obtain or cannot economy obtained naphthalene, anthracene, phenanthrene and pyrene it is 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, synthetic fibers, engineering plastics, pesticide, medicine, preservative, plasticizer, fragrance and in terms of have it is wide
General purposes belongs to high added value fine chemical product.Based on the above, isolating the higher neutral chemical combination of content from coal tar
Object 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 conventional methods exist
During coal tar processing there are process energy consumption is high, multi-process handling and many and diverse, product each component separation and utilization efficiency
The problems such as lower, phenol wastewater amount is greatly, environmental pollution is serious.For example, " acid-base method " during mentioning phenol proposes phenol method/work
Skill is complicated, specifically includes that the workshop sections such as the extraction of crude phenols, the purification of phenates, the decomposition of phenates and the purification of crude phenols, is related to equipment
It is more, multi-process handling and it is many and diverse, energy consumption is high, and cost of investment is high, proposes phenol low efficiency, and phenol wastewater amount is big, environmental pollution is serious
Problems.In addition to " acid-base method " mentions phenol, industrialized there are also Recovery by Solvent Extraction Methold phenol techniques, but this method/technique is deposited
It is big in solvent consumption, the problems such as equipment seriously corroded.
Chinese patent CN104845651A the method is the component separation method of coal tar, is prepared using silica gel as filler
Chromatographic column carries out elution separation to excellent chromatographic column has been gone up using four kinds of solvents, respectively obtains saturation light component, fragrant group
Point, light polar compound and weight polar compound.The invention is a kind of method of coal tar crude separation, and the boiling range of four kinds of fractions is wider,
It is unfavorable for the fine identification separated and form of coal tar.
One kind is described in Chinese invention patent CN102219649A, and phenols chemical combination is extracted from liquefied coal coil or coal tar
The method of object, distillation processing liquefied coal coil or coal tar, cut < 260 DEG C of fraction, extractant are mixed with the fraction, is layered,
It separates and collects the extraction oxidant layer containing phenolic compound；Multistage back extraction is carried out to the phenolic compound in extraction oxidant layer to extract,
Obtain stripping agent-phenol solution and extractant；Above-mentioned stripping agent-phenol solution is separated by rectifying, recycling stripping agent recycles, and
Isolated crude phenols；The neutral oil for removing and carrying secretly in phenolic compound is mentioned using vapor, finally obtains crude phenols product, and thick
Phenol purity is lower, complex process.
Chinese invention patent CN102492451A the method is the extraction separating method of high temperature coal-tar, and the invention is normal
Under the conditions of pressure, No. 1 and No. 2 solvents is used to carry out step extraction and separation to remove the impurity in coal tar, actually to coal tar
There is no being effectively separated to coal tar itself, the impurity in coal tar is only eliminated.
A kind of extraction separating method of high temperature coal-tar is described in Chinese invention patent CN102492451A, utilization is organic
The method of solvent fractional extraction can realize lightweight in coal tar, heavy ingredient dissolution and in raw coal tar ash content, coke powder with
And quinoline insolubles quick separating comes.The above isolated light components are enriched high added value whole in raw coal tar
Polycyclic aromatic hydrocarbon and important hetero atom polycyclic organic compound, concentrated in heavy component in raw coal tar except deash, coke powder
And the high-purity of quinoline insolubles refines asphalt component.
A kind of distillate dephenolizing process is described in Chinese invention patent CN101475817A and its device, coal tar distillation evaporate
Divide to be sufficiently mixed with basic phenate salt and react, into dephenolize tower, standing obtains mixing part and neutral phenol sodium；Mix part and 10-12%
Diluted alkaline mixing after enter secondary dephenolize tower, mixture settle and separate be basic phenate salt and washed mix part；Washed mixing part into
Enter dephenolize salt tower, basic phenate salt slot is entered after dephenolize salt tower settle and separate goes out remaining basic phenate salt, what is obtained has washed mixing
Part enters commercial naphthalene device and is further processed.
In conclusion energy consumption is high, multi-process handling in traditional coal Process of Tar Processing at present and many and diverse, product each component point
From with the problems such as utilization efficiency is lower, phenol wastewater amount is big, environmental pollution is serious, and be applied to the new of coal tar separation
Technology or it is there are major defect or is that there are the large scale equipment development problems in industrial application, it is difficult to enlargement industry
Production and cost of investment height, can only rest on laboratory stage.So currently seeking low energy consumption, low pollution, efficiently separating coal tar
The technology of oil has become the task of top priority of coal chemical industry low carbon development.
Summary of the invention
To overcome the problems in currently available technology, the object of the present invention is to provide a kind of coal tar oil ingredients continuously to separate work
Skill and device, the separating technology can realize that the efficiently separating of coal tar oil ingredient, energy saving technology is significant, operating condition is mild, without useless
Water discharge, environmentally protective, environmentally friendly, equipment investment is few, is easily enlarged production scale.
To achieve the goals above, The technical solution adopted by the invention is as follows:
A kind of coal tar oil ingredient continuous separation device, including coal tar storage tank, solvent A storage tank, solvent B preheating storage
Tank, coal tar extraction reaction kettle, asphalt component separate storage tank, asphalt component storage tank, the first adsorption tower, the second adsorption tower, solvent A
Remaining part storage tank, neutral oil ingredient knockout tower, neutral oil column overhead return tank, neutral oil tank, solvent B elution fraction are adsorbed in extraction
Storage tank, crude phenols component knockout tower, crude phenols column overhead return tank and crude phenols storage tank；
It is connected at the top of the coal tar extraction reaction kettle with coal tar storage tank and solvent A storage tank, coal tar extraction is anti-
Answer bottom portion separated with asphalt component tank top be connected, asphalt component separate tank bottom respectively with the first adsorption tower and second
It is connected at the top of adsorption tower；
It is connected at the top of the pre- hot tank of solvent B and the first adsorption tower and the second adsorption tower；
First adsorption tower and the second absorption tower bottom are respectively connected with solvent A extraction and adsorb remaining part storage tank, solvent B elution fraction
Storage tank and absorption be desorbed mix part storage tank；
Solvent A extraction adsorbs remaining part storage tank and is connected with neutral oil ingredient knockout tower, neutral oil ingredient separation column and
Be connected at the top of neutral oil column overhead return tank, neutral oil column overhead flow back pot bottom respectively with neutral oil ingredient knockout tower and solvent
A storage tank is connected；Neutral oil ingredient knockout tower tower bottom is connected with neutral oil tank；
Solvent B elution fraction storage tank is connected with crude phenols component knockout tower；Crude phenols component separation column overhead is separated with crude phenols component
Column overhead return tank is connected；Crude phenols component knockout tower tower bottom is connected with crude phenols storage tank.
A further improvement of the present invention lies in that further including that absorption mixes part storage tank, mixing part knockout tower with desorption and mixes
Close part column overhead return tank；
Absorption is connected with desorption mixing part storage tank with mixing part knockout tower；Mixing part separation column overhead with mix part knockout tower
Overhead reflux tank top is connected；
Mixing part knockout tower overhead reflux pot bottom is divided into two-way, separates column overhead with mixing part all the way and is connected, another way
It is connected with the pre- hot tank of solvent B；Mix at the top of part knockout tower tower bottom and the first adsorption tower and the second adsorption tower solvent A extract into
Tower tube road is connected.
A further improvement of the present invention lies in that described mixing part separation column overhead mixed part knockout tower overhead condenser with
Part knockout tower overhead reflux tank top is mixed to be connected；Mixing part knockout tower tower bottom is provided with mixing part knockout tower tower bottom reboiler,
And it mixes part knockout tower tower bottom reboiler entrance to be connected with mixing part knockout tower tower bottom.
A further improvement of the present invention lies in that the crude phenols component knockout tower overhead reflux pot bottom is divided into two-way, all the way
Column overhead is separated with crude phenols component to be connected；Another way is connected with the pre- hot tank of solvent B；The asphalt component separation storage tank is also connected with
There is asphalt component storage tank.
A further improvement of the present invention lies in that the neutrality oil ingredient knockout tower tower bottom is provided with neutral oil tower tower bottom and boils again
Device, and neutral oil tower tower bottom reboiler entrance is connected with neutral oil ingredient knockout tower tower bottom；Crude phenols component knockout tower tower
Bottom is provided with crude phenols component knockout tower tower bottom reboiler, and crude phenols component knockout tower tower bottom reboiler entrance with crude phenols group
Knockout tower tower bottom is divided to be connected.
A further improvement of the present invention lies in that it is described neutrality oil ingredient separation column through neutral oil column overhead condenser with
It is connected at the top of neutral oil column overhead return tank；Neutral oil ingredient knockout tower tower bottom is through neutral oil ingredient discharging condenser and neutral oil
Storage tank is connected；Crude phenols component separates column overhead through crude phenols component knockout tower overhead condenser and crude phenols component knockout tower overhead reflux
Tank is connected；Crude phenols component knockout tower tower bottom is connected through crude phenols component discharging condenser with crude phenols storage tank.
A kind of coal tar oil ingredient continuous separation technology, comprising the following steps:
1) solvent A mixes and extraction with coal tar: coal tar and solvent A are extracted, continuously in coal tar extraction reaction kettle
Stirring, heating obtain mixture, wherein the volume ratio of coal tar and solvent A is 1:1~1:20；
2) in solvent A mixture asphalt component separation: the mixture of step 1) injection asphalt component is separated into storage tank, warp
After crossing separation, obtains asphalt component and remove the solvent A extract of asphalt component；
3) solvent A extract adsorption tower adsorbing separation: by the solvent A extract of the removing asphalt component of step 2) through solvent
It after the pump pressurization of A extract feed, is sent into the first adsorption tower and carries out adsorbing separation, mixed liquor is stored in solvent A extraction after absorption
It adsorbs in remaining part storage tank；
4) the rectifying separation of neutral oil ingredient: the mixed liquor that step 3) adsorbing separation is obtained is by solvent A extraction absorption
Remaining part feed pump pressurization enters neutral oil ingredient knockout tower, obtains neutral oil ingredient and solvent A；Wherein, neutral oil ingredient point
Neutral oil product is collected from tower tower reactor and is stored in neutral oil tank, and overhead collection solvent A is back in solvent A storage tank；
5) the elution fraction separation of solvent B: when solvent A extraction has been adsorbed, and solvent B elution is switched to, solvent B is first through solvent
After the pre- hot tank preheating of B, enters in the first adsorption tower through the pressurization of solvent B feed pump and carry out elution separation, before elution is stablized
To eluent be stored in absorption and mix in part storage tank with desorption, obtained eluent is stored in solvent B and elutes after elution is stablized
In part storage tank；
While the elution fraction separation of solvent B, the solvent A extract of the removing asphalt component of step 2) is extracted through solvent A
It after taking object feed pump to pressurize, is sent into the second adsorption tower and carries out adsorbing separation, mixed liquor is stored in solvent A extraction absorption after absorption
In remaining part storage tank；
6) the rectifying separation of solvent B elution fraction: the eluent of solvent B enters crude phenols through the pressurization of solvent B elution fraction feed pump
Component knockout tower is isolated to solvent B and crude phenols, and wherein crude phenols component knockout tower tower reactor collects crude phenols product and is stored in crude phenols
Storage tank, overhead collection solvent B are back in the pre- hot tank of solvent B；
7) the mutual switching of the absorption of solvent A extract and solvent B elution: in the first adsorption tower or the second adsorption tower solvent A
It is switched to after the completion of extract absorbing process before solvent B elution is stablized or is switched to solvent A extract after the completion of elution processes
Before absorption is stablized, Ta Nei also nubbin solvent A extract liquor or solvent B eluent, in order to guarantee solvent A adsorb remaining part with it is molten
The quality of agent B elution fraction, therefore mix the other extraction of part progress before must stablizing absorption with elution processes and collect, therefore this is mixed
Part collection is stored in absorption and mixes part storage tank with desorption；
8) adsorb with elution mixing part rectifying separate: absorption with elution mix part mixed part feed pump pressurize into mix
Close part knockout tower, be isolated to solvent B with mix part except solvent B residue, wherein overhead collection solvent B reuse to solvent
The pre- hot tank of B, tower reactor are collected mixing part and are inhaled except the residue of solvent B enters the first adsorption tower and second through the pressurization of tower bottom discharging pump
The solvent A extract for receiving tower top carries out adsorbing separation into tower tube road and solvent A extract together；
9) the first adsorption tower mutually switches with the second adsorption tower, while carrying out absorption and realizing absorption and elution with elution action
It is carried out continuously；
Step 1) to step 9) can be realized the continuous separation of coal tar, obtain asphalt component, neutral oil ingredient and thick
Phenol component.
A further improvement of the present invention lies in that the solvent A is the mixture of one or more of alkane of C5~C8；
Wherein, the alkane of C5~C8 includes n-alkane or branched paraffin；
The coal tar is coalite tar, medium temperature coal tar or high temperature coal-tar；
The temperature range of the coal tar extraction reaction kettle heating is 60~100 DEG C；
The solvent A extract feed pump moulding pressure range is 0.2MPa~10MPa；
Silica gel is filled in first adsorption tower and the second adsorption tower.
A further improvement of the present invention lies in that the solvent B is one of ethyl acetate, toluene, ethyl alcohol, methanol or several
The mixture of kind；
The pre- hot tank preheating temperature range of solvent B is 20~60 DEG C.
A further improvement of the present invention lies in that the solvent B feed pump moulding pressure range is 0.2MPa~10MPa；
The solvent A extract is 0.2~0.5MPa, feeding temperature through solvent A extract feed pump moulding pressure range
Range is 60~100 DEG C；
Solvent A extraction adsorb remaining part feed pump moulding pressure range be 0.2MPa~10MPa, temperature be 60~
100℃；
The solvent B elution fraction feed pump moulding pressure range is 0.2~0.5MPa, and feed temperature range is 20-60 DEG C；
Mixing part feed pump moulding pressure range is 0.2~0.5MPa, and feed temperature range is 20-60 DEG C.
Compared with prior art, the invention has the benefit that the present invention by setting coal tar extract reaction kettle with
Asphalt component knockout drum is mixed with coal tar using solvent A, extracts, separates, available asphalt component；Pass through setting
Adsorption tower makes the solvent A extract for removing asphalt component after the pump pressurization of solvent A extract feed by adsorption tower, through inhaling
Attached isolated mixed liquor, which enters, carries out rectifying in neutral oil tower, obtain neutral oil ingredient；Absorption will be passed through after solvent B pressurization
Tower eluting solvent A extracts absorbed component, and the eluent after eluting enters crude phenols component knockout tower, through the isolated crude phenols of rectifying
Component completes the separation to coal tar oil ingredient.By the way that double adsorption towers are arranged into mutual switching, are adsorbed and washed simultaneously respectively
De- operation realizes that absorption is carried out continuously with elution.Present apparatus structure is simple, takes up little area, and is easily enlarged production.
Further, neutral oil column overhead reflux pump and crude phenols column overhead reflux pump are pre- with solvent A storage tank and solvent B respectively
Hot tank is connected, and the solvent in solvent tank is reused.
The present invention will extract reaction kettle in conjunction with separated from bitumen tank, be mixed using solvent A with coal tar, extract, stir
It mixes, separate, available asphalt component；By the way that adsorption tower is arranged, make the solvent A extract for removing asphalt component by solvent A
By adsorption tower after extract feed pump pressurization, enters through the mixed liquor that adsorbing separation obtains and carry out rectifying in neutral oil tower, obtain
To neutral oil ingredient；Solvent B is extracted into absorbed component by adsorption tower eluting solvent A after the pressurization of solvent B feed pump, through eluting
Eluent afterwards enters crude phenols component knockout tower, through the isolated crude phenols component of rectifying, solves existing coal tar processing process
Present in energy consumption is high, multi-process handling and it is complicated, the separation of product each component and utilization efficiency are lower, environmental pollution is serious asks
Topic.The present invention is green separation technique, does not generate waste water, waste residue and exhaust gas, and the operating condition of technique is mild, easy, work
Skill and equipment manufacturing cost is low, less investment.
Detailed description of the invention
Fig. 1 is that coal tar oil ingredient of the invention separates solvent A extraction absorption and solvent B elution processes process；
Fig. 2 is that coal tar oil ingredient of the invention separates the remaining part of solvent A extraction absorption and solvent B elution fraction rectification process stream
Journey；
Fig. 3 is that coal tar oil ingredient separation absorption of the invention mixes part rectification process process with elution；
Fig. 4 is the total ion chromatogram of neutral oil ingredient；
Fig. 5 is the total ion chromatogram of crude phenols component；
Fig. 6 is the hot weightless picture of asphalt component；
In figure, 1, coal tar storage tank, 2, solvent A storage tank；3, the pre- hot tank of solvent B；4, coal tar extracts reaction kettle；
5, asphalt component separates storage tank；6, solvent A feed pump；7, solvent A extract feed pumps；8, solvent B feed pump；9, asphalt component
Storage tank；10, the first adsorption tower；11, the second adsorption tower；12, remaining part storage tank is adsorbed in solvent A extraction；13, solvent A extraction absorption
Remaining part feed pump；14, neutral oil ingredient knockout tower；15, neutral oil column overhead condenser；16, neutral oil column overhead return tank；
17, neutral oil column overhead reflux pump；18, neutral oil tower tower bottom reboiler；19, neutral oil ingredient discharging condenser；20, neutral oil
Component discharging pump；21, neutral oil tank；22, solvent B elution fraction storage tank；23, solvent B elution fraction feed pump；24, crude phenols component
Knockout tower；25, crude phenols component knockout tower overhead condenser；26, crude phenols column overhead return tank；27, crude phenols column overhead reflux pump；
28, crude phenols tower tower bottom reboiler；29, crude phenols component discharging condenser；30, crude phenols component discharging pump；31, crude phenols storage tank；32, it inhales
It is attached to mix part storage tank with desorption；33, part feed pump is mixed；34, part knockout tower is mixed；35, part column overhead condenser is mixed；36,
Mix part column overhead return tank；37, part column overhead reflux pump is mixed；38, part tower tower bottom reboiler is mixed；39, part tower tower is mixed
Bottom discharging pump.
Specific embodiment
Below in conjunction with attached drawing, by embodiment, present invention is further described in detail.
Heretofore described all raw materials and intermediate products and storage tank all have Liquid level；The coal tar extraction
Reaction kettle band heating mantle and agitating device；The solvent A head tank has heating mantle；The adsorption tower bottom respectively with three
Pipeline is connected.
Referring to figure 1, figure 2 and figure 3, a kind of coal tar oil ingredient continuous separation device includes: coal tar storage tank 1, solvent A
The pre- hot tank 3 of storage tank 2, solvent B, coal tar extraction reaction kettle 4, asphalt component separation storage tank 5, solvent A feed pump 6, solvent A extraction
Object feed pump 7, solvent B feed pump 8, asphalt component storage tank 9, the first adsorption tower 10, the second adsorption tower 11, solvent A extraction is taken to inhale
It is cold that attached residue part storage tank 12, solvent A extraction adsorb remaining part feed pump 13, neutral oil ingredient knockout tower 14, neutral oil column overhead
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 elution
It is part feed pump 23, crude phenols component knockout tower 24, crude phenols component knockout tower 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 discharge condenser 29, crude phenols component discharging pump 30, thick
Phenol storage tank 31；It is cold that absorption mixes part storage tank 32, mixing part feed pump 33, mixing part knockout tower 34, mixing part column overhead with desorption
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 tower bottom discharging pump 39.
Referring to Fig. 1,1 bottom of coal tar storage tank is connected with coal tar extraction 4 top side of reaction kettle；Solvent A storage tank 2
Bottom is connected with 6 entrance of solvent A feed pump, and the outlet of solvent A feed pump 6 is connected with the coal tar extraction 4 top other side of reaction kettle；
Coal tar extraction 4 bottom of reaction kettle is separated with asphalt component to be connected at the top of storage tank 5；Asphalt component separate 5 one side bottom of storage tank with
Asphalt component storage tank 9 is connected；Asphalt component separates another side bottom of storage tank 5 and is connected with solvent A extract feed 7 entrances of pump, molten
7 outlet of agent A extract feed pump is connected at the top of the first adsorption tower 10 and the second adsorption tower 11 respectively；Pre- 3 bottom of hot tank solvent B
Portion is connected with 8 entrance of solvent B feed pump, and the outlet of solvent B feed pump 8 is respectively and at the top of the first adsorption tower 10 and the second adsorption tower 11
It is connected；First adsorption tower, 10 bottom is extracted with solvent A respectively to be adsorbed remaining part storage tank 12, solvent B elution fraction storage tank 22 and inhales
It is attached to be connected with desorption mixing part storage tank 32；Second adsorption tower, 11 bottom is extracted with solvent A respectively adsorbs remaining part storage tank 12, solvent
B elution fraction storage tank 22 and absorption are connected with desorption mixing part storage tank 32.
Referring to fig. 2, solvent A extraction adsorbs remaining part storage tank 12 and extracts the remaining 13 entrance phase of part feed pump of absorption with solvent A
Even, solvent A extraction is adsorbed remaining part feed pump 13 and is exported and is connected with neutral oil ingredient knockout tower 14；Neutral oil ingredient knockout tower 14
It is connected at the top of top and neutral oil column overhead condenser 15,15 condenser bottom of neutral oil column overhead and neutral oil column overhead flow back
It is connected at the top of tank 16；16 bottom of neutral oil column overhead return tank is connected with 17 entrance of neutral oil column overhead reflux pump, neutral oil tower
The outlet of tower top return pump 17 is divided into two-way, is connected all the way at the top of neutral oil ingredient knockout tower 14；Neutral oil column overhead reflux pump
17 outlet another ways are connected with solvent A storage tank 2；18 entrance of neutral oil tower tower bottom reboiler with neutral oil ingredient knockout tower 14
Tower bottom is connected；Neutral 14 tower bottom of oil ingredient knockout tower is connected with neutral oil ingredient discharging 19 entrance of condenser；Neutral oil ingredient goes out
The outlet of material condenser 19 is connected with neutral 20 entrance of oil ingredient discharging pump, the neutral outlet of oil ingredient discharging pump 20 and neutral oil tank
21 are connected；Solvent B elution fraction storage tank 22 is connected with 23 entrance of solvent B elution fraction feed pump, and solvent B elution fraction feed pump 23 exports
It is connected with crude phenols component knockout tower 24；24 tower top of crude phenols component knockout tower and 25 top phase of crude phenols component knockout tower overhead condenser
Even, it is connected at the top of 25 overhead condenser bottom of crude phenols component knockout tower and crude phenols component knockout tower return tank of top of the tower 26；Crude phenols group
26 bottom of knockout tower return tank of top of the tower is divided to be connected with 27 entrance of crude phenols component knockout tower tower top return pump, crude phenols component knockout tower tower
The top outlet of reflux pump 27 is divided into two-way, is connected all the way with 24 tower top of crude phenols component knockout tower；Crude phenols component knockout tower overhead reflux
27 outlet another way of pump is connected with the pre- hot tank 3 of solvent B；28 entrance of crude phenols component knockout tower tower bottom reboiler with crude phenols group
24 tower bottom of knockout tower is divided to be connected；24 tower bottom of crude phenols component knockout tower is connected with crude phenols component discharging 29 entrance of condenser；Crude phenols group
It separates the outlet of material condenser 29 to be connected with 30 entrance of crude phenols component discharging pump, the outlet of crude phenols component discharging pump 30 and crude phenols storage tank 31
It is connected；
Referring to Fig. 3, absorption is connected with desorption mixing part storage tank 32 with mixing 33 entrance of part feed pump, mixes part feed pump 33
Outlet is connected with mixing part knockout tower 34；Mixing 34 tower top of part knockout tower with mix 35 top phase of part knockout tower overhead condenser
Even, it is connected at the top of mixing 35 bottom of part knockout tower overhead condenser and mixing part knockout tower return tank of top of the tower 36；Mix part separation
36 bottom of column overhead return tank is connected with mixing 37 entrance of part knockout tower tower top return pump, mixes part knockout tower tower top return pump 37
Outlet is divided into two-way, is connected all the way with mixing 34 tower top of part knockout tower；It mixes part knockout tower tower top return pump 37 and exports another way
It is connected with the pre- hot tank 3 of solvent B；Mixing 38 entrance of part knockout tower tower bottom reboiler with mix 34 tower bottom phase of part knockout tower
Even；Mixing 34 tower bottom of part knockout tower is connected with mixing 39 entrance of part tower tower bottom discharging pump, and mixing part tower tower bottom discharging pump 39 exports
It is connected with the first adsorption tower, the second adsorption tower solvent overhead A extract into tower tube road.
Coal tar oil ingredient separating technology of the invention the following steps are included:
One, solvent A extraction absorption and solvent B elution processes process
(1) solvent A extraction and absorbing process process
Coal tar raw material continuity is stored up by certain flow into coal tar storage tank 1, and coal tar raw material is then injected coal
Tar extraction reaction kettle 4.Solvent A is pumped into coal tar extraction reaction kettle 4 through solvent A feed pump 6 by solvent A storage tank 2 simultaneously.It opens
Stirring is mixed evenly solvent A with coal tar raw material, and control coal tar extraction 4 temperature of reaction kettle is 60~100 DEG C, and extraction is certain
After time.Solvent 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 extraction, stores into asphalt component storage tank 9.Except the solvent A extract of asphalt component is by 5 overhead stream of asphalt component knockout drum
Out, it is forced into that 0.2~10MPa is pumped into the first adsorption tower 10 or the second adsorption tower 11 is inhaled through solvent A extract feed pump 7
Attached, solvent A extraction adsorbs remaining part after the first adsorption tower 10 or the extraction of 11 tower bottom of the second adsorption tower are collected after adsorbing separation, into
Enter solvent A extraction and adsorbs remaining 12 storage of part storage tank.First adsorption tower 10 is adsorbed and is eluted with 11 rotation of the second adsorption tower
It operates (when i.e. the first adsorption tower 10 is adsorbed, the second adsorption tower 11 is eluted, and vice versa), realizes continuous operation.
(2) solvent B elution processes process
After being switched to solvent B elution stabilization after the completion of the absorption of solvent A extract, solvent B is pre- through the pre- hot tank 3 of solvent B
Heat is forced into 0.2MPa~10MPa through the pump of solvent B feed pump 8 and is pumped into the first adsorption tower 10 or the second absorption to after 20~60 DEG C
11 tower top of tower adsorbs surplus substance to tower internal solvent A and elutes, by solvent B elution fraction by the first adsorption tower 10 or the second absorption
After 11 tower bottom of tower is collected, stored into solvent B elution fraction storage tank 22.
(3) process flow when solvent A/B absorption switches with elution
Before being switched to solvent B elution stabilization after the completion of 11 solvent adsorption technique of the first adsorption tower 10 or the second adsorption tower,
Or be switched to after the completion of elution processes before the absorption of solvent A extract stablizes, Ta Nei also nubbin solvent A extraction absorption is remaining
Liquid or solvent B eluent, in order to guarantee that the quality of remaining part and solvent B elution fraction is adsorbed in solvent A extraction, therefore must will absorption and
The progress of mixing part in addition collect by extraction before elution processes are stablized.Therefore it is extracted in the first adsorption tower 10 or 11 solvent A of the second adsorption tower
Solvent A extraction is switched to before solvent B elution processes are stablized or is switched to after the completion of solvent B elution processes after the completion of object absorbing process
Before taking object absorption to stablize, before the solvent A from 11 tower bottom of the first adsorption tower 10 or the second adsorption tower/B absorption is stablized with elution
Mixing part is collected in absorption and mixes the storage of part storage tank 32 with desorption.
Two, remaining part and solvent B elution fraction rectification process process are adsorbed in solvent A extraction
(1) remaining part rectifying (neutral oil production) technique is adsorbed in solvent A extraction
In the solvent A extract absorbing process normal table operation of adsorption tower, remaining part storage is adsorbed from solvent A extraction
The solvent A of tank 12 adsorbs remaining part and is pumped into neutral oil component knockout tower 14 by remaining 13 pressurization of part feed pump of solvent A extraction absorption
Carry out rectifying separation.Neutral 14 tower top output solvent A steam of oil ingredient knockout tower, solvent A steam is through neutral tower top complete condenser 15
It all is condensed into liquid phase, the solvent A after coagulating entirely enters neutral oil column overhead return tank 16, then through neutral oil column overhead reflux pump
17 a part are back to neutral 14 tower top of oil ingredient knockout tower by certain reflux ratio, and another part returns to solvent A storage tank 2 and returns
With.
Neutral oil a part of 14 outputs of neutral oil ingredient knockout tower is through 18 heating and gasifying of neutral oil tower tower bottom reboiler
After be back in neutral oil ingredient knockout tower 14, another part is as tower reactor product output.The neutral oil ingredient of output is cold through discharging
Condenser 19 is cooling, and neutral oil after cooling is pumped out through neutral oil ingredient discharging pump 20, enters neutral oil tank 21 as product and stores up
It deposits.
(2) rectifying of solvent B elution fraction (crude phenols production) process flow
In the operation of adsorption tower solvent B elution processes normal table, the solvent B elution from solvent B elution fraction storage tank 22
Part enters crude phenols component knockout tower 24 by solvent B elution fraction feed pump 23 and carries out rectifying separation.24 tower top of crude phenols component knockout tower
Output solvent B steam, solvent B steam is all condensed into liquid phase through crude phenols component knockout tower overhead condenser 25, molten after coagulating entirely
Agent B enters crude phenols column overhead return tank 26, then returns through 27 a part of crude phenols knockout tower tower top return pump by certain reflux ratio
It is flow to 24 tower top of crude phenols component knockout tower, another part returns to the pre- hot tank 3 of solvent B.
Crude phenols a part of 24 outputs of crude phenols component knockout tower is after 28 heating and gasifying of crude phenols knockout tower tower bottom reboiler
It is back in crude phenols component knockout tower 24, another part is as tower reactor product output.The crude phenols of output discharge through crude phenols component and condense
Device 29 is cooling, and crude phenols after cooling enter crude phenols storage tank 31 as product through the pump of crude phenols component discharging pump 30.
Three, absorption mixes part rectification process with elution
Before being switched to solvent B elution stabilization after the completion of 11 solvent adsorption technique of the first adsorption tower 10 or the second adsorption tower,
Or before being switched to solvent A extract absorption stabilization after the completion of elution processes, during this period, mixed when being collected in absorption with desorption
Before the solvent A of part storage tank 32/B absorb-elute is stablized mixing part it is to be achieved it is a certain amount of after, enter mixing by mixing part feed pump 33
Part 34 rectifying of knockout tower separation.34 tower top output solvent B steam of part knockout tower is mixed, it is cold that solvent B steam is mixed part column overhead
Condenser 35 is all condensed into liquid phase, and the solvent B after coagulating entirely enters mixing part column overhead return tank 36, is then mixed part column overhead
For 37 a part of reflux pump by certain reflux ratio blowback to mixing 34 tower top of part knockout tower, another part returns to solvent B preheating
Storage tank 3.
Remaining a part is mixed the heating of part tower tower bottom reboiler 38 after 34 output separation solvent B of mixing part knockout tower
It is back to after gasification in mixing part knockout tower 34, another part discharges as tower reactor.Tower reactor discharging is mixed part tower tower bottom discharging pump
The solvent A extract that 39 the first adsorption towers of blowback 10 and second absorption tower 11 push up is into tower tube road, in the first adsorption tower 10 or the second
When 11 solvent A absorbing process normal table of adsorption tower is run, 5 upper solvent A extract one of storage tank is separated with from asphalt component
It rises and is adsorbed into the first adsorption tower 10 or the second adsorption tower 11.
The solvent A be C5~C8 alkane in single alkane or several single alkane mixture (C5~C8's
Alkane includes n-alkane or branched paraffin).
The solvent B is the mixture of one or more of ethyl acetate, toluene, ethyl alcohol, methanol.
Silica gel is filled in first adsorption tower 10 and the second adsorption tower 11.
The neutrality oil ingredient, crude phenols component and asphalt component are product.Obtained solvent A and solvent B can be with simultaneously
It is recycled.
In order to illustrate effect of the invention, following embodiment is using low temperature coal tar in the progress of coal tar oil ingredient separating technology
Oil ingredient separation test is distinguished in order to accurate Analyze & separate product using gas chromatograph-mass spectrometer (GC-MS) and thermal analyzer
Composition and thermal weight loss process to product are measured.It is now the coal tar for being derived from semi-coke factory of northern Shensi Fugu County with experimental raw
(heavy oil) is separated as experimental subjects, and heavy oil (tar clarifying basin subsurface layer oil) is shown in Table 1 by the fundamental property that national standard measures.
The fundamental property of 1 coal tar heavy oil of table
Note: * minusing
Using coal tar oil ingredient continuous separation technology of the present invention, solvent A (the specially alkane of C7) and solvent B are selected respectively
(specially polar solvent ethyl acetate) is eluant, eluent, and silica gel is adsorbent, neutral oil ingredient, the crude phenols in separation in coal tar
Component and asphalt component.
It takes a certain amount of coal tar to be tested according to foregoing schemes, is obtained after the test and respectively to from products pot
Neutral oil ingredient and each 1mL of crude phenols component, then with the acetone solution of 5mL, then carry out GC-MS analysis, analysis result is shown in figure
4, Fig. 5 and table 2 and table 3.Obtained asphalt component weighs 5mg and is analyzed with TG, and analysis result is shown in Fig. 6.
Coalite tar neutral oil forms in table 2
Coalite tar crude phenols form in table 3
The present invention has carried out product analysis to the peak of peak 1-37 in Fig. 4, carries out in Fig. 5 to the peak that peak number is 1-24
Product analysis, the peak number in figure can be found in table.
By the experimental studies results of Fig. 4, Fig. 5 and Fig. 6 as it can be seen that continuously separating new work using coal tar oil ingredient of the invention
Skill can efficiently separate to obtain neutral oil ingredient, crude phenols component and asphalt component in coal tar, be compared with the traditional method, this
Invention is a kind of method of continuous separation coal tar of green, does not generate waste water, waste residue and exhaust gas and device tradition separation dress relatively
It sets and takes up little area, small investment, is easily enlarged production.The present invention overcomes energy consumptions existing during existing coal tar processing simultaneously
Greatly, the problems such as multi-process handling and many and diverse, product each component low separation efficiency, phenol wastewater amount are big, environmental pollution is serious.
Claims (9)
1. a kind of coal tar oil ingredient continuous separation device, which is characterized in that including coal tar storage tank (1), solvent A storage tank
(2), the pre- hot tank of solvent B (3), coal tar extraction reaction kettle (4), asphalt component separation storage tank (5), asphalt component storage tank (9),
Remaining part storage tank (12), neutral oil ingredient knockout tower are adsorbed in first adsorption tower (10), the second adsorption tower (11), solvent A extraction
(14), neutral oil column overhead return tank (16), neutral oil tank (21), solvent B elution fraction storage tank (22), crude phenols component knockout tower
(24), crude phenols column overhead return tank (26) and crude phenols storage tank (31)；
It is connected at the top of coal tar extraction reaction kettle (4) with coal tar storage tank (1) and solvent A storage tank (2), coal tar extraction
It takes reaction kettle (4) bottom to separate with asphalt component at the top of storage tank (5) to be connected, asphalt component separates storage tank (5) bottom respectively with the
It is connected at the top of one adsorption tower (10) and the second adsorption tower (11)；
It is connected at the top of the pre- hot tank of solvent B (3) and the first adsorption tower (10) and the second adsorption tower (11)；
First adsorption tower (10) and the second adsorption tower (11) bottom are respectively connected with solvent A extraction and adsorb remaining part storage tank (12), molten
Agent B elution fraction storage tank (22) and absorption be desorbed mix part storage tank (32)；
Solvent A extraction adsorbs remaining part storage tank (12) and is connected with neutral oil ingredient knockout tower (14), neutral oil ingredient knockout tower
(14) top with neutral oil column overhead return tank (16) top be connected, neutral oil column overhead return tank (16) bottom respectively with neutrality
Oil ingredient knockout tower (14) is connected with solvent A storage tank (2)；Neutral oil ingredient knockout tower (14) tower bottom and neutral oil tank (21) phase
Even；
Solvent B elution fraction storage tank (22) is connected with crude phenols component knockout tower (24)；Crude phenols component knockout tower (24) tower top and crude phenols
Component knockout tower return tank of top of the tower (26) is connected；Crude phenols component knockout tower (24) tower bottom is connected with crude phenols storage tank (31)；
It further include that absorption mixes part storage tank (32), mixing part knockout tower (34) and mixing part column overhead return tank with desorption
(36)；
Absorption is connected with desorption mixing part storage tank (32) with mixing part knockout tower (34)；Mixing part knockout tower (34) tower top with mix
It is connected at the top of part knockout tower return tank of top of the tower (36)；
Mixing part knockout tower return tank of top of the tower (36) bottom is divided into two-way, is connected all the way with mixing part knockout tower (34) tower top, separately
It is connected all the way with the pre- hot tank of solvent B (3)；Mix part knockout tower (34) tower bottom and the first adsorption tower (10) and the second adsorption tower
(11) top solvent A extract is connected into tower tube road.
2. a kind of coal tar oil ingredient continuous separation device according to claim 1, which is characterized in that mixing part separation
Tower (34) tower top is mixed to be connected at the top of part knockout tower overhead condenser (35) and mixing part knockout tower return tank of top of the tower (36)；It is mixed
It closes part knockout tower (34) tower bottom and is provided with mixing part knockout tower tower bottom reboiler (38), and mix a part knockout tower tower bottom reboiler
(38) entrance is connected with mixing part knockout tower (34) tower bottom.
3. a kind of coal tar oil ingredient continuous separation device according to claim 1, which is characterized in that the crude phenols component point
It is divided into two-way from column overhead return tank (26) bottom, is connected all the way with crude phenols component knockout tower (24) tower top；Another way and solvent B
Pre- hot tank (3) is connected；Asphalt component separation storage tank (5) is also connected with asphalt component storage tank (9).
4. a kind of coal tar oil ingredient continuous separation device according to claim 1, which is characterized in that the neutrality oil ingredient
Knockout tower (14) tower bottom is provided with neutral oil tower tower bottom reboiler (18), and neutral oil tower tower bottom reboiler (18) entrance is equal
It is connected with neutral oil ingredient knockout tower (14) tower bottom；Crude phenols component knockout tower (24) tower bottom is provided with crude phenols component knockout tower tower bottom
Reboiler (28), and crude phenols component knockout tower tower bottom reboiler (28) entrance with crude phenols component knockout tower (24) tower bottom phase
Even.
5. a kind of coal tar oil ingredient continuous separation device according to claim 1, which is characterized in that the neutrality oil ingredient
Through being connected at the top of neutral oil column overhead condenser (15) and neutral oil column overhead return tank (16) at the top of knockout tower (14)；Neutral oil
Component knockout tower (14) tower bottom is connected through neutral oil ingredient discharging condenser (19) with neutral oil tank (21)；The separation of crude phenols component
Tower (24) tower top is connected through crude phenols component knockout tower overhead condenser (25) with crude phenols component knockout tower return tank of top of the tower (26)；Slightly
Phenol component knockout tower (24) tower bottom is connected through crude phenols component discharging condenser (29) with crude phenols storage tank (31).
6. a kind of coal tar oil ingredient continuous separation technology, which comprises the following steps:
1) solvent A mixes and extraction with coal tar: coal tar and solvent A are stirred in coal tar extraction reaction kettle (4) extraction, continuously
It mixes, heat and obtain mixture, wherein the volume ratio of coal tar and solvent A is 1:1~1:20；
2) in solvent A mixture asphalt component separation: by the mixture of step 1) injection asphalt component separation storage tank (5), warp
After crossing separation, obtains asphalt component and remove the solvent A extract of asphalt component；
3) solvent A extract adsorption tower adsorbing separation: the solvent A extract of the removing asphalt component of step 2) is extracted through solvent A
After taking object feed pump (7) to pressurize, it is sent into the first adsorption tower (10) and carries out adsorbing separation, mixed liquor is stored in solvent A after absorption
Extraction is adsorbed in remaining part storage tank (12)；
4) the rectifying separation of neutral oil ingredient: the mixed liquor that step 3) adsorbing separation is obtained is remaining by solvent A extraction absorption
Part feed pump (13), which pressurizes, enters neutral oil ingredient knockout tower (14), obtains neutral oil ingredient and solvent A；Wherein, neutral oil group
Divide knockout tower (14) tower reactor to collect neutral oil product to be stored in neutral oil tank (21), overhead collection solvent A is back to solvent A and goes out
In storage tank (2)；
5) the elution fraction separation of solvent B: when solvent A extraction has been adsorbed, and solvent B elution is switched to, solvent B is first pre- through solvent B
After hot tank (3) preheating, enters in the first adsorption tower (10) through solvent B feed pump (8) pressurization and carry out elution separation, elution is steady
The eluent obtained before fixed is stored in absorption and mixes in part storage tank (32) with desorption, and the eluent that elution obtains after stablizing is stored in
In solvent B elution fraction storage tank (22)；
While the elution fraction separation of solvent B, by the solvent A extract of the removing asphalt component of step 2) through solvent A extract
It after feed pump (7) pressurization, is sent into the second adsorption tower (11) and carries out adsorbing separation, mixed liquor is stored in solvent A extraction after absorption
It adsorbs in remaining part storage tank (12)；
6) the rectifying separation of solvent B elution fraction: the eluent of solvent B enters crude phenols through solvent B elution fraction feed pump (23) pressurization
Component knockout tower (24), is isolated to solvent B and crude phenols, and wherein crude phenols component knockout 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 A extract and solvent B elution: molten in the first adsorption tower (10) or the second adsorption tower (11)
It is switched to after the completion of agent A extract absorbing process before solvent B elution is stablized or is switched to solvent A extraction after the completion of elution processes
Before taking object absorption to stablize, Ta Nei also nubbin solvent A extract liquor or solvent B eluent, in order to guarantee that solvent A adsorbs remaining part
With the quality of solvent B elution fraction, therefore must will absorption stablize with elution processes before mix part carry out it is other produce collection, therefore this
Mixing part collection is stored in absorption and mixes part storage tank (32) with desorption；
8) adsorb and separate with the rectifying for eluting mixing part: absorption mixes part with elution and is mixed the pressurization of part feed pump into mixing part
Knockout tower, be isolated to solvent B with mix part remove solvent B residue, wherein overhead collection solvent B reuse is pre- to solvent B
Hot tank (3), tower reactor collect mixing part except the residue of solvent B enters the first adsorption tower (10) and the through the pressurization of tower bottom discharging pump
The solvent A extract on two absorption towers (11) top carries out adsorbing separation into tower tube road and solvent A extract together；
9) the first adsorption tower mutually switches with the second adsorption tower, while carrying out absorption and realizing that absorption is continuous with elution with elution action
It carries out；
Step 1) to step 9) can be realized the continuous separation of coal tar, obtain asphalt component, neutral oil ingredient and crude phenols group
Point.
7. a kind of coal tar oil ingredient continuous separation technology according to claim 6, which is characterized in that the solvent 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；
The coal tar is coalite tar, medium temperature coal tar or high temperature coal-tar；
The temperature range of the coal tar extraction reaction kettle heating is 60~100 DEG C；
Described solvent A extract feed pump (7) moulding pressure range is 0.2MPa~10MPa；
Silica gel is filled in first adsorption tower (10) and the second adsorption tower (11).
8. a kind of coal tar oil ingredient continuous separation technology according to claim 6, which is characterized in that the solvent B is second
The mixture of one or more of acetoacetic ester, toluene, ethyl alcohol, methanol；
The pre- hot tank of solvent B (3) the preheating temperature range is 20~60 DEG C.
9. a kind of coal tar oil ingredient continuous separation technology according to claim 6, which is characterized in that the solvent B charging
Pump (8) moulding pressure range is 0.2MPa~10MPa；
The solvent A extract is 0.2~0.5MPa, feeding temperature model through solvent A extract feed pump (7) moulding pressure range
Enclose is 60~100 DEG C；
Solvent A extraction adsorb remaining part feed pump (13) moulding pressure range be 0.2MPa~10MPa, temperature be 60~
100℃；
Solvent B elution fraction feed pump (23) the moulding pressure range is 0.2~0.5MPa, and feed temperature range is 20-60 DEG C；
Mixing part feed pump (33) moulding pressure range is 0.2~0.5MPa, and feed temperature range is 20-60 DEG C.
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| CN108384567B (en) * | 2018-05-07 | 2024-01-16 | 西北大学 | Coal tar component separation device and process |
| KR102428396B1 (en) * | 2018-05-08 | 2022-08-02 | 오씨아이 주식회사 | Method for treating high solid coal tar |
| CN110980988B (en) * | 2019-12-12 | 2023-10-31 | 伊犁新天煤化工有限责任公司 | System and method for treating crushed coal pressurized gasification solid-liquid mixture |
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