CN105152437B - A kind of Coal Tar Wastewater on-line extraction dephenolization method - Google Patents
A kind of Coal Tar Wastewater on-line extraction dephenolization method Download PDFInfo
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Abstract
The invention discloses a kind of Coal Tar Wastewater on-line extraction dephenolization method, be that aqueous coal tar is heated, after vacuum flashing, obtain mixed vapour, mixed vapour is sent into into rectifying column, extractant is introduced as backflow from tower top simultaneously, sequence of constant boiling and rectification, lateral line withdrawal function of component of the boiling point between 170～210 DEG C from rectifying column is carried out in rectifying column,, by fractional distillation in the heavy oil component in the middle part of tower, other components are by overhead extraction for component of the boiling point more than 210 DEG C；Overhead extraction thing feeding overhead condensation cooler is cooled to into temperature less than 40 DEG C, being then fed into return tank of top of the tower carries out that profit is settlement separate, and isolated moisture content is the water for sloughing phenol；Isolated oil content merges feeding dephenolize device dephenolize with the component of lateral line withdrawal function.The method of the present invention is directly realized by online extracting and dephenolizing in the rectifying column during coal tar distillation, has both reached the purpose that coal tar distillation, aldehydes matter are removed simultaneously, has saved cost again.
Description
Technical field
The invention belongs to coal tar production technical field, more particularly to a kind of Coal Tar Wastewater on-line extraction dephenolization method.
Background technology
In coal tar, contained phenolic compound is important industrial chemicals and high value added product, can manufacture dyestuff, doctor
Medicine, resin, adhesive, preservative etc..Phenol is protoplasm highly toxic substance again simultaneously, has toxic action to all living things individuality,
And it is difficult to degrade, phenol is entered in waste water, can cause serious water pollution, and current phenol wastewater is in China's water pollution control
It is to be listed in one of harmful waste water of emphasis solution.Dissolubility of the phenol in water is very big, and what is produced during coal tar processing is useless
Water contains substantial amounts of phenol, and its content can reach 10000～20000mg/L, and the efficient recovery of these phenolic compounds can be significantly
Lift the industrial value of coal tar, it is also possible to reduce pollution of the phenolic compound to environment.
Phenol in coal tar is concentrated mainly in 170～210 DEG C of component, usually first passes through the method for distillation by this portion
Carbolic oil is divided to separate, carbolic oil is sent to three company's cleaning devices of alkali liquor again then carries out dephenolize.The method of this dephenolize is
A kind of conventional method, can reclaim most phenol in coal tar.But with substantial amounts of during due to coal tar distillation
Moisture, the phenol amount taken away with water evaporation are also very big.Phenol in water containing phenol reclaim generally using rectification method, absorption method, extraction,
Steam dephenolize is reclaimed.Find that above-mentioned technique generally existing reclaims effect by understanding polytechnic ruuning situation at this stage
Rate is low, stable difference, solvent loss is big, secondary pollution is heavy, the problem that operation energy consumption is high.For rectification method, need to arrange single
Only extraction equipment separates phenol therein, and then rectification extraction phase obtains phenolic product again, and this method operating cost is high, energy consumption is big, work
Skill is complicated.The particularly high problem of operation energy consumption is very serious, and this is not mainly due to carrying out rational heat integration.
There is enterprise for the phenol in recycle-water, the method for employing extraction, actual motion are carried out repeatedly to water as technique needs
Heating cooling causes energy consumption suddenly high, and the phenol cost recovery of one ton of water of last EQUILIBRIUM CALCULATION FOR PROCESS is up to hundreds of units, has had a strong impact on technique
Feasibility
The content of the invention
It is an object of the invention to provide a kind of Coal Tar Wastewater on-line extraction dephenolization method, solves existing method for extracting and dephenolizing
High cost, energy consumption are big, complex process and do not take into full account the problem utilized because of the extractant increment for polluting deterioration of efficiency.
The technical solution used in the present invention is that a kind of Coal Tar Wastewater on-line extraction dephenolization method is comprised the following steps：
Step 1, coal tar heating vacuum flashing：
Aqueous coal tar is warmed up to into 120-180 DEG C, then intensification after aqueous coal tar send into coal tar decompression and dodge
Steaming pot, enters the gasification of water-filling, oil and volatile phenol at reduced pressure conditions, mixed vapour is deviate from.
Step 2, on-line extraction dephenolize：
Mixed vapour is sent into into the middle and upper part of rectifying column, while extractant is introduced as backflow, mixed vapour from tower top
Sequence of constant boiling and rectification is carried out in rectifying column with extractant；Component fractionation of the boiling point more than 210 DEG C is entered in heavy oil component, boiling point is existed
Lateral line withdrawal function of the component between 170～210 DEG C from rectifying column, other light components are by overhead extraction；Overhead extraction thing is sent
Enter overhead condensation cooler and temperature is cooled to less than 40 DEG C, be then re-fed into return tank of top of the tower settlement separate, the profit that carries out profit
The settlement separate water for obtaining is the water for sloughing phenol.
The present invention also has the characteristics that：
Preferably, the pressure of coal tar reduced-pressure flash tank is -40～-95kPa (G).
Preferably, rectifying column adopts plate column, and effective tower tray number of plies is 2-5 layers, and tower top temperature is 50-100 DEG C, and tower is intrinsic pressure
It is by force -40～-95kPa (G).
Preferably, in step 2, extractant is mixture, by benzene mixed or crude benzol in it is a kind of with washing oil or in heavy benzol one
Kind mix, washing oil or heavy benzol account for the 10-50% of extractant gross mass.
Preferably, during sequence of constant boiling and rectification, control tower fight back flow is 1～4 with the mass ratio of overhead extraction thing:1.
The settlement separate oil content for obtaining of profit merge with the component of lateral line withdrawal function feeding dephenolize device, at a certain temperature with
Sig water carries out counter current contacting dephenolize into dephenolize oil, and dephenolize oil enters back into water washing device and returns essence after washing removes sodium ion
Evaporate tower to be continuing with as new extractant.
Preferably, the temperature of dephenolize is 80～85 DEG C.
Preferably, sig water is sodium hydroxide solution that mass concentration is 6～15%.
Through repeatedly extraction, the extractant that extraction efficiency is deteriorated introduces hydrogenation pans by pipeline and is used as hydrogenating materials,
The extractant of reduction by extractor in fresh extractant supplement, to improve extraction efficiency.
The invention has the beneficial effects as follows：Using the Coal Tar Wastewater on-line extraction dephenolization method of the present invention, can be by water
Phenol content drop to below 2000mg/L from 10000～20000mg/L, make water reach the requirement of postprocessing working procedures, directly send outside
To rear process unit.Component of the present invention by boiling point more than 210 DEG C passes through in the heavy oil component that fractional distillation is entered in the middle part of tower in addition, its
Its component realizes the separation of high low boiling phenol and the back extraction of high boiling point oil in extraction phase by overhead extraction.Partially due to point
The extractant not enough entered in heavy oil component from precision carries out increment recovery by the method being hydrogenated with, and further prepares cleaning former
Material, while eliminating secondary pollution.The method of the present invention is compared with existing rectification method, it is not necessary to arrange segregation apparatuss in addition,
Online extracting and dephenolizing is directly realized by rectifying column during coal tar distillation, coal tar distillation, aldehydes matter has both been reached and has been gone
The purpose removed, saves cost again, reduces investment, simplifies processing step, is adapted to commercial production.
Description of the drawings
Fig. 1 is the process schematic of the Coal Tar Wastewater on-line extraction dephenolization method of the present invention.
In figure, 1. coal tar oil tank, 2. heat exchanger, 3. coal tar reduced-pressure flash tank, 4. rectifying column, 5. overhead condensation cooling
Device, 6. return tank of top of the tower, 7. dephenolize device, 8. water washing device.
Specific embodiment
The present invention is described in detail with reference to the accompanying drawings and detailed description.
The invention provides a kind of Coal Tar Wastewater on-line extraction dephenolization method, with reference to the equipment of Fig. 1, including following step
Suddenly：
Step 1, coal tar heating vacuum flashing：
Aqueous coal tar is transported to into coal tar oil tank 1, to prevent coal tar profit to be layered, coal tar oil tank 1 should set and stir
Mix device, and periodic agitation.For the water that Che tanks middle and upper part is substantially layered is discharged to coal tar profit storage tank by water dividing gap.Profit
Before water in storage tank sends into heat exchanger by pump-metered in normal production, mix with coal tar.By aqueous coal tar by changing
Hot device 2 exchanges heat, and reaches 120-180 DEG C, enters back into coal tar reduced-pressure flash tank 3, enters water-filling, oil and volatile phenol at reduced pressure conditions
Gasification, mixed vapour is deviate from.
Step 2, on-line extraction dephenolize：
Mixed vapour is sent into into the middle and upper part of rectifying column 4, while extractant is introduced as backflow, mixed vapour from tower top
Sequence of constant boiling and rectification, heavy oil component that boiling point component more than 210 DEG C by fractional distillation entered tower in the middle part of are carried out in rectifying column with extractant
In, as the raw material of follow-up hydrogenation process；By component of the boiling point between 170～210 DEG C from the lateral line withdrawal function of rectifying column,
Other components are by overhead extraction；Overhead extraction thing is sent into into overhead condensation cooler 5 and is cool below 40 DEG C, be then re-fed into
Return tank of top of the tower 6 carries out that profit is settlement separate, and the settlement separate water for obtaining of profit is the water for sloughing phenol.
The settlement separate oil content for obtaining of profit merges feeding dephenolize device 7 with the component of lateral line withdrawal function, at a certain temperature
Counter current contacting dephenolize is carried out into dephenolize oil with sig water, dephenolize oil enters back into water washing device 8 and returns after washing removes sodium ion
Return rectifying column to be continuing with as new extractant.
Through repeatedly extraction, the extractant that extraction efficiency is deteriorated introduces hydrogenation pans by pipeline and is used as hydrogenating materials,
The extractant of reduction by extractor in fresh extractant supplement, to improve extraction efficiency.
Wherein, in step 1, the pressure of coal tar reduced-pressure flash tank 3 is -40～-95kPa (G).
In step 2, rectifying column 4 adopts plate column, and effective tower tray number of plies is 2-5, and tower top temperature is 50-100 DEG C, and tower is intrinsic pressure
It is by force -40～-95kPa (G).Preferably, tower top temperature is 50-65 DEG C.
In step 2, extractant is mixture, by benzene mixed or crude benzol in a kind of mix with a kind of in washing oil or heavy benzol
Form, washing oil or heavy benzol account for the 10-50% of extractant gross mass.
During sequence of constant boiling and rectification, control tower fight back flow is 1～4 with the mass ratio of overhead extraction thing:1.
In dephenolize device, the temperature of dephenolize is at 80～85 DEG C；Sig water is sodium hydroxide that mass concentration is 6～15%
Solution.
When extraction efficiency declines, crude benzol, benzene mixed can be filled in dephenolize oil and improve extraction partition coefficient, unnecessary extraction
Agent then pumpable hydrogenation plant, becomes high-quality fuel through hydrogenation.
Embodiment 1
Coal Tar Wastewater on-line extraction dephenolize, comprises the following steps：
Step 1, coal tar heating vacuum flashing：
Aqueous coal tar is transported to into coal tar oil tank, to prevent coal tar profit to be layered, coal tar oil tank should set stirring
Device, and periodic agitation.For the water that Che tanks middle and upper part is substantially layered is discharged to coal tar profit storage tank by water dividing gap.Profit is stored up
Before water in tank sends into heat exchanger by pump-metered in normal production, mix with coal tar.By aqueous coal tar by heat exchange
Device exchanges heat, and reaches 120 DEG C, enters back into coal tar reduced-pressure flash tank, and flash tank top pressure is by force -95kPa (G), at reduced pressure conditions
Enter the gasification of water-filling, oil and volatile phenol, mixed vapour is deviate from.
Step 2, on-line extraction dephenolize：
Mixed vapour is sent into into the middle and upper part of rectifying column, while introduce extractant as backflow from tower top, extractant by
80% benzene mixed and 20% washing oil composition, the introduction volume of extractant and the mass ratio of overhead extraction thing are 1:1, mixed vapour
Sequence of constant boiling and rectification is carried out in rectifying column with extractant, the effective tower tray number of plies of rectifying column is 5, and tower top temperature is 50 DEG C, in tower pressure for-
95kPa(G).The lateral line withdrawal function of the extractant of 170～210 DEG C of components from rectifying column is extracted into, component of the boiling point more than 210 DEG C is led to
Fractional distillation is crossed in the heavy oil component in the middle part of tower, as the raw material of hydrocracking process；Other light components are by overhead extraction；Will
Overhead extraction thing is sent into overhead condensation cooler and is cooled to temperature less than 40 DEG C, is then re-fed into carrying out oil into return tank of top of the tower
Water is settlement separate, and the settlement separate water for obtaining of profit is the water for sloughing phenol.The profit settlement separate oil content for obtaining is taken out with side line
The component that goes out merges sends into dephenolize device, is that 15% sodium hydroxide solution carries out counter current contacting and takes off at 80 DEG C with mass concentration
Into dephenolize oil, dephenolize oil after washing removes sodium ion returns rectifying column and continues extraction as new extractant phenol again.
Embodiment 2
Coal Tar Wastewater on-line extraction dephenolize, comprises the following steps：
Step 1, coal tar heating vacuum flashing：
Aqueous coal tar is transported to into coal tar oil tank, to prevent coal tar profit to be layered, coal tar oil tank should high stirring
Device, and periodic agitation.For the water that Che tanks middle and upper part is substantially layered is discharged to coal tar profit storage tank by water dividing gap.Profit is stored up
Before water in tank sends into heat exchanger by pump-metered in normal production, mix with coal tar.By aqueous coal tar by heat exchange
Device exchanges heat, and reaches 180 DEG C, enters back into coal tar reduced-pressure flash tank, and flash tank top pressure is by force -40kPa (G), at reduced pressure conditions
Enter the gasification of water-filling, oil and volatile phenol, mixed vapour is deviate from.
Step 2, on-line extraction dephenolize：
Mixed vapour is sent into into the middle and upper part of rectifying column, while introduce extractant as backflow from tower top, extractant by
90% crude benzol and 10% heavy benzol composition, the introduction volume of extractant and the mass ratio of overhead extraction thing are 2:1, mixed vapour with
Extractant carries out sequence of constant boiling and rectification in rectifying column, and the effective tower tray number of plies of rectifying column is 2, and tower top temperature is 100 DEG C, in tower pressure for-
40kPa(G).The lateral line withdrawal function of the extractant of 170～210 DEG C of components from rectifying column is extracted into, component of the boiling point more than 210 DEG C is led to
Fractional distillation is crossed in the heavy oil component in the middle part of tower, as the raw material of hydrocracking process；Other light components are by overhead extraction；Will
Overhead extraction thing is sent into overhead condensation cooler and is cooled to temperature less than 40 DEG C, is then re-fed into carrying out oil into return tank of top of the tower
Water is settlement separate, and the settlement separate water for obtaining of profit is the water for sloughing phenol.The profit settlement separate oil content for obtaining is taken out with side line
The component that goes out merges sends into dephenolize device, is that 6% sodium hydroxide solution carries out counter current contacting and takes off at 85 DEG C with mass concentration
Into dephenolize oil, dephenolize oil after washing removes sodium ion returns rectifying column and continues extraction as new extractant phenol again.
Embodiment 3
Coal Tar Wastewater on-line extraction dephenolize, comprises the following steps：
Step 1, coal tar heating vacuum flashing：
Aqueous coal tar is transported to into coal tar oil tank, to prevent coal tar profit to be layered, coal tar oil tank should high stirring
Device, and periodic agitation.For the water that Che tanks middle and upper part is substantially layered is discharged to coal tar profit storage tank by water dividing gap.Profit is stored up
Before water in tank sends into heat exchanger by pump-metered in normal production, mix with coal tar.By aqueous coal tar by heat exchange
Device exchanges heat, and reaches 150 DEG C, enters back into coal tar reduced-pressure flash tank, and flash tank top pressure is by force -60kPa (G), at reduced pressure conditions
Enter the gasification of water-filling, oil and volatile phenol, mixed vapour is deviate from.
Step 2, on-line extraction dephenolize：
Mixed vapour is sent into into the middle and upper part of rectifying column, while introduce extractant as backflow from tower top, extractant by
70% benzene mixed and 30% washing oil composition, the introduction volume of extractant and the mass ratio of overhead extraction thing are 4:1, mixed vapour
Sequence of constant boiling and rectification is carried out in rectifying column with extractant, the effective tower tray number of plies of rectifying column is 3, and tower top temperature is 85 DEG C, in tower pressure for-
60kPa(G).The lateral line withdrawal function of the extractant of 170～210 DEG C of components from rectifying column is extracted into, component of the boiling point more than 210 DEG C is led to
Fractional distillation is crossed in the heavy oil component in the middle part of tower, as the raw material of hydrocracking process；Other light components are by overhead extraction；Will
Overhead extraction thing is sent into overhead condensation cooler and is cooled to temperature less than 40 DEG C, is then re-fed into carrying out oil into return tank of top of the tower
Water is settlement separate, and the settlement separate water for obtaining of profit is the water for sloughing phenol.The profit settlement separate oil content for obtaining is taken out with side line
The component that goes out merges sends into dephenolize device, is that 10% sodium hydroxide solution carries out counter current contacting and takes off at 82 DEG C with mass concentration
Into dephenolize oil, dephenolize oil after washing removes sodium ion returns rectifying column and continues extraction as new extractant phenol again.
Embodiment 4
Coal Tar Wastewater on-line extraction dephenolize, comprises the following steps：
Step 1, coal tar heating vacuum flashing：
Aqueous coal tar is transported to into coal tar oil tank, to prevent coal tar profit to be layered, coal tar oil tank should high stirring
Device, and periodic agitation.For the water that Che tanks middle and upper part is substantially layered is discharged to coal tar profit storage tank by water dividing gap.Profit is stored up
Before water in tank sends into heat exchanger by pump-metered in normal production, mix with coal tar.By aqueous coal tar by heat exchange
Device exchanges heat, and reaches 180 DEG C, enters back into coal tar reduced-pressure flash tank, and flash tank top pressure is by force -55kPa (G), at reduced pressure conditions
Enter the gasification of water-filling, oil and volatile phenol, mixed vapour is deviate from.
Step 2, on-line extraction dephenolize：
Mixed vapour is sent into into the middle and upper part of rectifying column, while introduce extractant as backflow from tower top, extractant by
50% benzene mixed and 50% heavy benzol composition, the introduction volume of extractant and the mass ratio of overhead extraction thing are 2:1, mixed vapour
Sequence of constant boiling and rectification is carried out in rectifying column with extractant, the effective tower tray number of plies of rectifying column is 2, and tower top temperature is 65 DEG C, in tower pressure for-
55kPa(G).The lateral line withdrawal function of the extractant of 170～210 DEG C of components from rectifying column is extracted into, component of the boiling point more than 210 DEG C is led to
Fractional distillation is crossed in the heavy oil component in the middle part of tower, as the raw material of hydrocracking process；Other light components are by overhead extraction；Will
Overhead extraction thing is sent into overhead condensation cooler and is cooled to temperature less than 40 DEG C, is then re-fed into carrying out oil into return tank of top of the tower
Water is settlement separate, and the settlement separate water for obtaining of profit is the water for sloughing phenol.The profit settlement separate oil content for obtaining is taken out with side line
The component that goes out merges sends into dephenolize device, is that 6% sodium hydroxide solution carries out counter current contacting and takes off at 85 DEG C with mass concentration
Into dephenolize oil, dephenolize oil after washing removes sodium ion returns rectifying column and continues extraction as new extractant phenol again.
Embodiment 5
Coal Tar Wastewater on-line extraction dephenolize, comprises the following steps：
Step 1, coal tar heating vacuum flashing：
Aqueous coal tar is transported to into coal tar oil tank, to prevent coal tar profit to be layered, coal tar oil tank should high stirring
Device, and periodic agitation.For the water that storage tank middle and upper part is substantially layered is discharged to coal tar profit storage tank by water dividing gap.Profit is stored up
Before water in tank sends into heat exchanger by pump-metered in normal production, mix with coal tar.By aqueous coal tar by heat exchange
Device exchanges heat, and reaches 180 DEG C, enters back into coal tar reduced-pressure flash tank, and flash tank top pressure is by force -65kPa (G), at reduced pressure conditions
Enter the gasification of water-filling, oil and volatile phenol, mixed vapour is deviate from.
Step 2, on-line extraction dephenolize：
Mixed vapour is sent into into the middle and upper part of rectifying column, while introduce extractant as backflow from tower top, extractant by
60% crude benzol and 40% washing oil composition, the introduction volume of extractant and the mass ratio of overhead extraction thing are 2:1, mixed vapour with
Extractant carries out sequence of constant boiling and rectification in rectifying column, and the effective tower tray number of plies of rectifying column is 2, and tower top temperature is 60 DEG C, in tower pressure for-
65kPa(G).The lateral line withdrawal function of the extractant of 170～210 DEG C of components from rectifying column is extracted into, component of the boiling point more than 210 DEG C is led to
Fractional distillation is crossed in the heavy oil component in the middle part of tower, as the raw material of hydrocracking process；Other light components are by overhead extraction；Will
Overhead extraction thing is sent into overhead condensation cooler and is cooled to temperature less than 40 DEG C, is then re-fed into carrying out oil into return tank of top of the tower
Water is settlement separate, and the settlement separate water for obtaining of profit is the water for sloughing phenol.The profit settlement separate oil content for obtaining is taken out with side line
The component that goes out merges sends into dephenolize device, is that 6% sodium hydroxide solution carries out counter current contacting and takes off at 85 DEG C with mass concentration
Into dephenolize oil, dephenolize oil after washing removes sodium ion returns rectifying column and continues extraction as new extractant phenol again.
Phenol content detection is carried out to the water for sloughing phenol of embodiment 1-5, as a result respectively 1365,1688,1821,1710,
1696ppm, it is seen that by the method for the coal tar on-line extraction of the present invention, by the phenol content in water from 10000～20000mg/L
Below 2000mg/L is dropped to, directly outer rear process unit can be sent to.The extractant of loss is rised in value by the method being hydrogenated with
Reclaim, while eliminating secondary pollution.
Component of the boiling point of the present invention more than 210 DEG C passes through in the heavy oil component that fractional distillation is entered in the middle part of tower in addition, other groups
Point by overhead extraction, the separation of high low boiling phenol and the back extraction of high boiling point oil in extraction phase are realized.The extractant of loss leads to
The method for crossing hydrogenation carries out increment recovery, further prepares cleaning raw material, while eliminating secondary pollution.
The method of the present invention is compared with existing rectification method, it is not necessary to arrange segregation apparatuss in addition, in coal tar distillation mistake
Online extracting and dephenolizing is directly realized by rectifying column in journey, the purpose that coal tar distillation, aldehydes matter are removed both has been reached simultaneously,
Cost is saved again.
Above description of the present invention is part case study on implementation, but the invention is not limited in above-mentioned specific embodiment party
Formula.Above-mentioned specific embodiment is schematic, is not restricted.Every employing method of the present invention, without departing from
In the case of present inventive concept and scope of the claimed protection, all concrete expansions belong within protection scope of the present invention.
Claims (8)
1. a kind of Coal Tar Wastewater on-line extraction dephenolization method, it is characterised in that comprise the following steps：
Step 1, coal tar heating vacuum flashing：
Aqueous coal tar is warmed up between 120-180 DEG C, the aqueous coal tar after will heat up sends into coal tar reduced-pressure flash tank,
Enter the gasification of water-filling, oil and volatile phenol at reduced pressure conditions, mixed vapour is deviate from；
Step 2, on-line extraction dephenolize：
Mixed vapour is sent into into the middle and upper part of rectifying column, while extractant is introduced as backflow, mixed vapour and extraction from tower top
Taking agent carries out sequence of constant boiling and rectification in rectifying column；Boiling point is entered in heavy oil component more than 210 DEG C of component fractionation, by boiling point 170～
Lateral line withdrawal function of the component between 210 DEG C from rectifying column, other light components are by overhead extraction；Overhead extraction thing is sent into into tower top
Condensate cooler is cooled to temperature less than 40 DEG C, is then re-fed into return tank of top of the tower settlement separate, the profit sedimentation point that carries out profit
It is the water for sloughing phenol from the water for obtaining.
2. Coal Tar Wastewater on-line extraction dephenolization method according to claim 1, it is characterised in that coal described in step 1
The pressure of tar reduced-pressure flash tank is -40～-95kPa (G).
3. Coal Tar Wastewater on-line extraction dephenolization method according to claim 1, it is characterised in that essence described in step 2
Evaporate tower and adopt plate column, effective tower tray number of plies is 2-5 layers, and tower top temperature is 50-100 DEG C, and pressure is -40～-95kPa in tower
(G)。
4. Coal Tar Wastewater on-line extraction dephenolization method according to claim 1, it is characterised in that extract in the step 2
Agent is taken for mixture, by benzene mixed or crude benzol in a kind of one kind with washing oil or heavy benzol mix, washing oil or heavy benzol are accounted for
The 10-50% of extractant gross mass.
5. Coal Tar Wastewater on-line extraction dephenolization method according to claim 1, it is characterised in that azeotropic described in step 2
In distillation process, control tower fight back flow is 1～4 with the mass ratio of overhead extraction thing:1.
6. Coal Tar Wastewater on-line extraction dephenolization method according to claim 1, it is characterised in that oil described in step 2
Water precipitating is dropped isolated oil content and is merged feeding dephenolize device with the component of lateral line withdrawal function, is carried out with sig water at a certain temperature
Into dephenolize oil, dephenolize oil enters back into water washing device and rectifying column is returned after washing removes sodium ion as new for counter current contacting dephenolize
Extractant be continuing with.
7. Coal Tar Wastewater on-line extraction dephenolization method according to claim 6, it is characterised in that in the dephenolize device
The temperature of counter current contacting dephenolize is 80～85 DEG C.
8. Coal Tar Wastewater on-line extraction dephenolization method according to claim 6, it is characterised in that the sig water is matter
Amount concentration is 6～15% sodium hydroxide solution.
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| CN109097085B (en) * | 2017-06-20 | 2021-11-16 | 中国石油化工股份有限公司 | Coal tar pretreatment method |
| CN107739299A (en) * | 2017-11-23 | 2018-02-27 | 魏艳娟 | The refining spearation combined dehydration method and device of mixed phenol |
| CN111348998A (en) * | 2020-04-17 | 2020-06-30 | 湖北三里枫香科技有限公司 | Energy-saving environment-friendly acetic acid production process |
| CN113817490B (en) * | 2021-10-18 | 2022-12-16 | 胜帮科技股份有限公司 | Coupling device and coupling process for coal tar phenol extraction and phenol-containing water treatment |
| CN114409004A (en) * | 2022-03-05 | 2022-04-29 | 北京中科康仑环境科技研究院有限公司 | Energy-saving recycling process for treating wastewater containing volatile substances |
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| CN1314780C (en) * | 2005-07-27 | 2007-05-09 | 中钢集团鞍山热能研究院 | Technique for processing hypothermal tar oil |
| CN1919818A (en) * | 2006-09-18 | 2007-02-28 | 清华大学 | Method of recovery phenol from waste water and system thereof |
| CN101289234A (en) * | 2008-06-16 | 2008-10-22 | 南昌大学 | Process for treating industrial waste water containing hydroxybenzene and ammine by double-tower stripping |
| CN101597124B (en) * | 2009-01-09 | 2011-05-11 | 华南理工大学 | Method for treating coal gasification wastewater containing phenol and ammonia |
| KR101142295B1 (en) * | 2011-08-24 | 2012-05-07 | 재원산업 주식회사 | Method of purifying coal tar sludge and coal tar sludge |
| CN102674608A (en) * | 2012-05-11 | 2012-09-19 | 华南理工大学 | Method for recycling and treating high-concentration phenol/ammonia wastewater |
| CN103496813B (en) * | 2013-09-29 | 2015-09-16 | 青岛科技大学 | A kind of method and device thereof getting reason coal chemical industrial waste water without side line Single-tower stripping |
| CN104671566A (en) * | 2013-12-01 | 2015-06-03 | 朱伟萍 | Steam-saving coal chemical wastewater treatment method with side line |
| CN204211590U (en) * | 2014-11-14 | 2015-03-18 | 西安百特瑞化工工程有限公司 | A kind of deamination of Phenol-Containing Wastewater Treatment carries phenol device |
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