CN106145426A - In a kind of coal chemical industrial waste water, carbolic oil is combined removing system and processes technique - Google Patents
In a kind of coal chemical industrial waste water, carbolic oil is combined removing system and processes technique Download PDFInfo
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Abstract
The invention provides carbolic oil in a kind of coal chemical industrial waste water combine removing system and process technique, it includes oil removing system, extracting system, back extraction system and cleaning system and corresponding technical process thereof.Wherein extraction process comprises the steps: that (1) extracts tar, and garbage tar is recycled；(2) extracting and dephenolizing, waste water phenol clearance reaches more than 99.7%；(3) recycling in intermediate layer.Extractant, phenols are fully recycled, it is to avoid secondary waste water is polluted.Coal chemical industrial wastewater processing system that the present invention provides and process technique energy simultaneous removing, reclaim garbage tar and phenol in waste water, it is achieved extractant farthest recycles.Factory's original equipment is changed little, low cost by the present invention, stable, and after process, water outlet total phenols clearance is more than 94%, and COD clearance is more than 98%, meets the follow-up ammonia still process of sewage and processes requirement.
Description
Technical field
The invention belongs to water-treatment technology field, combine removing system particularly to carbolic oil in a kind of coal chemical industrial waste water
System and process technique.
Background technology
Coal chemical industrial waste water is the industrial wastewater that the processes such as coking, gas purification and chemical products refine produce, main
The heterocyclic compound such as volatile phenol to be contained, polycyclic aromatic hydrocarbon and oxygen, sulfur, nitrogen, be a kind of high COD, high phenol value,
High ammonia nitrogen and the most intractable industrial organic waste water.During it mostlys come from remained ammonia, gas purification
The waste water of generation and refining and the waste water of other occasion generation of tar, crude benzol etc..Coal chemical industrial waste water is to contain
Having the industrial wastewater of a large amount of persistent organic pollutants, environment is caused serious pollution by discharge beyond standards.
Due to this water quality and quantity change greatly, complicated component, so process coal chemical industrial waste water technique the most numerous.
Domestic many employing pretreatment oil removings, air-extraction removes ammonia, the operations such as extraction removes phenol, cyanogen, Biochemical method.
Patent CN10332067A discloses the new method of a kind for the treatment of of residual coking ammonia water.This invention is by five
Operation forms: ammonia still process deacidification, air stripping dephenolize, extracting and dephenolizing, oxidation processes and water reuse.
Patent CN101597124A discloses a kind of method processed containing Coal Chemical Industry coal gasification waste water, the method
Including single column pressurization stripping removing sour gas and ammonia, survey line extract out the fractional condensation of three grades of gas, diisopropyl ether extract phenol,
Solvent recovery process, and obtain crude phenols product.This invention solvent recovery tower and solvent stripper reclaim extractant,
Obtain crude phenols, and achieve coal gasification waste water single column and combine removing sour gas and the process of ammonia.
But above-mentioned each technique is only detar, does not reclaims the tar that content in coal chemical industrial waste water is bigger
Utilize.And there is significant problem in unresolved extraction process always, i.e. extract the existence in intermediate layer.Extraction
The generation in intermediate layer can waste the resources such as a large amount of extractant and callable phenols, and may result in factory can not be normal
Operation, even needs the regulation that stops production time serious.
Summary of the invention
In order to overcome above-mentioned the deficiencies in the prior art, the invention provides carbolic oil associating in a kind of coal chemical industrial waste water
Removing process.Original Process ba-sis adds coke tar recovery system and intermediate layer recovery system, improves work
Sequence, solves to produce a large amount of intermediate layer a unserviceable difficult problem in existing extraction process, improves extractant, benzene
The recovery utilization rate of phenol etc., the side-product tar class that in combined recovery waste water, content is higher, thus reduce waste water
Processing cost, reduces pollutant discharge amount, makes the COD content of water outlet reach subsequent treatment requirement.
For reaching this purpose, the present invention by the following technical solutions:
In a kind of coal chemical industrial waste water, removing system combined by carbolic oil, and described system includes oil removing system, extraction successively
System, back extraction system and cleaning system.
Described oil removing system includes coal chemical industrial waste water storage tank, coke filter, purpose ceramic-film filter successively and takes off
Oil waste water medial launder, coal chemical industrial waste water is stored in coal chemical industrial waste water storage tank, coke filter and ceramic membrane mistake
Filter is for removing the solid pollutant in coal chemical industrial waste water and fraction solids tar.
Described extracting system includes heat exchanger, extraction tank, extraction tower, extractant medial launder, intermediate layer handles
Reactor, dephenolize water medial launder and Alkali liquid compounding groove, wherein heat exchanger discharging opening and extraction tank charging aperture phase
Even, extraction tank bottom discharge mouth and extraction tower tower top charging aperture and be connected, the intermediate layer discharging opening of extraction tank and
Intermediate layer handles reactor feed mouth is connected, and extraction tower tower top discharging opening is connected with extraction tank extractant entrance,
The intermediate layer discharging opening of extraction tower is connected with intermediate layer handles reactor feed mouth, discharging opening at the bottom of extraction tower tower with
Dephenolize water medial launder charging aperture is connected, and extractant medial launder discharging opening is connected with extraction tower extractant entrance, in
The outlet of interbed treatment reactor aqueous phase is connected with dephenolize water medial launder charging aperture.
Described back extraction system includes back extraction tower, rich phenol organic facies medial launder and phenol sodium medial launder, wherein back extraction tower
Discharging opening at the bottom of tower is connected with phenol sodium medial launder charging aperture, in rich phenol organic facies medial launder aqueous phase discharging opening and phenol sodium
Between groove charging aperture be connected.
Preferably, the number of described back extraction tower is 1,2 or 3, in technical process can be 1 anti-
Extraction tower, 2 back extraction tower parallel connections or 3 back extraction towers are in parallel.
Described cleaning system includes extractant purifying column, overhead condenser, tar medial launder and purifies extractant
Medial launder, wherein extractant purifying column tower top discharging opening is connected with overhead condenser charging aperture, overhead condenser
Export and be connected with purification extractant medial launder charging aperture, discharging opening at the bottom of extractant purifying column tower and tar medial launder
It is connected.
In described oil removing system, degreased wastewater medial launder discharging opening is connected with heat exchanger entrance, and extraction tank top goes out
Material mouth is connected with back extraction column overhead charging aperture, intermediate layer handles reactor discharging opening and rich phenol organic facies medial launder
Charging aperture is connected, charging aperture at the bottom of Alkali liquid compounding groove discharging opening and back extraction tower tower and rich phenol organic facies medial launder charging
Mouthful be connected, back extraction column overhead discharging opening is connected with extractant medial launder charging aperture, back extraction column overhead discharging opening and
Charging aperture at the bottom of extractant purifying column tower is connected, and rich phenol organic facies medial launder organic facies discharging opening purifies with extractant
Charging aperture at the bottom of tower tower is connected, and purifies extractant medial launder discharging opening and is connected with extractant medial launder charging aperture.
In the above coal chemical industrial waste water, the process technique of removing system combined by carbolic oil, and described process technique includes
Oil removal process, extraction process, stripping process and purification process.
Described oil removal process is preprocessing process, and it comprises the following steps: coal chemical industrial waste water enters Coal Chemical Industry and gives up
Water storage tank, flows through coke filter successively and purpose ceramic-film filter enters degreased wastewater medial launder, coke filtration
Solid pollutant in device and purpose ceramic-film filter removing coal chemical industrial waste water and fraction solids tar, removing thing enters
Row burning disposal, the waste water after process enters degreased wastewater medial launder.
Described extraction process comprises the following steps:
(1) extraction detar: the waste water of degreased wastewater medial launder enters extraction tank after heat exchanger is lowered the temperature, and uses
Tar in waste water and phenol extraction are gone out by extraction.The rich phenol that extractant used is extracted by extraction tower is organic
Circulating supply mutually, the waste water that extraction tank bottom land is discharged enters extraction tower, the rich tar extracted in extraction tank and
Phenol organic facies enters back extraction tower, and extraction tank intermediate layer liquid enters intermediate layer handles reactor.
(2) extracting and dephenolizing: the waste water that extraction tank bottom land is discharged enters extraction tower, and extractant used is from extraction
Agent medial launder also enters the phenols in extraction tower counter-current extraction waste water.Extraction tower tower top richness phenol organic facies is as extraction
Take agent circulation supply and enter intermediate layer handles reactor, extraction tower tower to extraction tank, extraction tower intermediate layer liquid
Dephenolize waste water in the end enters dephenolize water medial launder, treats further subsequent treatment.
(3) process of intermediate layer liquid: intermediate layer handles reactor oil-water separation is biphase, the oil phase of abjection enters
Entering rich phenol organic facies medial launder, the aqueous phase of intermediate layer handles reactor abjection enters dephenolize water medial launder.
Described stripping process comprises the following steps: rich tar and phenol organic facies that extraction process extraction tank is discharged are entered
Entering back extraction tower, the phenol in back extraction removing organic facies, its alkali liquor used is from alkali liquor configured slot.Back extraction
Crude phenols product at the bottom of tower tower enters phenol sodium medial launder, and back extraction column overhead organic facies enters extractant medial launder and extraction
Agent purifying column, in alkali liquor configured slot, alkali liquor enters back extraction tower and rich phenol organic facies medial launder.In rich phenol organic facies
Between groove periodically filled into alkali liquor by alkali liquor configured slot and synchronize back extraction, the isolated rich phenol sodium of rich phenol organic facies medial launder
Aqueous phase enters phenol sodium medial launder, and the rich phenol isolated organic facies of organic facies medial launder enters extractant purifying column.
Described purification process comprises the following steps: back extraction column overhead organic facies separates with rich phenol organic facies medial launder
The organic facies interval gone out enters extractant purifying column regenerating extracting agent, within 2～5 days, carries out once this operation.Extraction
The extractant that agent purifying column tower top is discharged enters purification extractant medial launder after overhead condenser, then pumps into extraction
Take agent medial launder, it is achieved extractant recycles.The tar discharged at the bottom of extractant purifying column tower enters in tar
Between groove proceed to tar storage tank again and recycle.
In described extraction process step (1), the waste water of degreased wastewater medial launder is cooled to 20～50 DEG C through heat exchanger,
Such as 20 DEG C, 23 DEG C, 25 DEG C, 27 DEG C, 30 DEG C, 33 DEG C, 35 DEG C, 37 DEG C, 40 DEG C, 43 DEG C,
45 DEG C, 47 DEG C or 50 DEG C etc..
In described extraction process step (1), in extraction tank, extractant is extraction tower tower top richness phenol organic facies, makes richness
Phenol organic facies is recycled.
In described extraction process step (2) extractant medial launder, extractant is that patent CN103848468A is announced
Coal chemical industrial waste water extractant, this extractant contains following components by mass fraction:
Neutral containing phosphorus extractant 4～25%
Acid containing phosphorus extractant 0.5～10%
Cosolvent 0.5～5%
Diluent 60～95%
Because the formula of extractant has been disclosed prior art, the most no longer its concrete composition is repeated.
Profit phase volume ratio 1:1～5 in described extraction process step (2) extraction tower, such as 1:1,1:1.5,
1:2,1:2.5,1:3,1:3.5,1:4,1:4.5 or 1:5 etc..
In described extraction process step (2) extraction tower, extraction temperature is 20～30 DEG C, such as 20 DEG C, 21 DEG C,
22 DEG C, 23 DEG C, 24 DEG C, 25 DEG C, 26 DEG C, 27 DEG C, 28 DEG C, 29 DEG C or 30 DEG C etc..
In described stripping process alkali liquor configured slot, alkali liquor is sodium hydrate aqueous solution.
In described stripping process alkali liquor configured slot, the mass concentration of sodium hydrate aqueous solution is 10～30%, such as
10%, 13%, 15%, 17%, 20%, 23%, 25%, 27% or 30% etc..
In described stripping process, back extraction column overhead organic facies and rich phenol organic facies medial launder are isolated organic alternate
Have a rest and enter extractant purifying column.
Extractant purifying column 2～carry out the operation of primary recycling extractant for 5 days in described purification process, such as 2
My god, 3 days, 4 days or 5 days etc..
In described purification process, extractant purifying column tower top temperature is 120～180 DEG C, such as 120 DEG C,
125℃、130℃、135℃、140℃、145℃、150℃、155℃、160℃、165℃、
170 DEG C, 175 DEG C or 180 DEG C etc..
In described purification process, extractant purifying column tower top pressure is 0.05～0.25MPa, such as 0.05MPa,
0.07MPa, 0.10MPa, 0.13MPa, 0.15MPa, 0.17MPa, 0.20MPa, 0.23MPa or
0.25MPa etc..
In described purification process, extractant purifying column column bottom temperature is 110～150 DEG C, such as 110 DEG C,
115 DEG C, 120 DEG C, 125 DEG C, 130 DEG C, 135 DEG C, 140 DEG C, 145 DEG C or 150 DEG C etc..
In described purification process, extractant purifying column tower bottom pressure is 0.10～0.20MPa, such as 0.10MPa,
0.11MPa、0.12MPa、0.13MPa、0.14MPa、0.15MPa、0.16MPa、0.17MPa、
0.18MPa, 0.19MPa or 0.20MPa etc..
Compared with prior art, the method have the advantages that
(1) reclaim tar product, make full use of waste water resource.The many employings of existing coal chemical wastewater treating technique
Tar and solid waste in waste water are Tong Bu filtered by the technology such as filtration, the technique having no efficient recovery tar, and de-
Depollution thing is more intractable.Phenol extraction agent rich in " extraction tower " is recycled to " extraction tank " by this technique, profit
The tar separated in coal chemical industrial waste water is carried with useless extractant, finally thick burnt in " extractant purifying column " removing
Oil product.Avoid the wasting phenomenon of tar product, add the output of product during waste water processes.
(2) extractant recovery utilization rate is high.The generation of Middle emulsion layer is inevitable in extraction process
, the Middle emulsion layer removed from extraction tank, extraction tower contains a large amount of organic solvent.In this technology utilization
Emulsifying water-oil phase is completely separated by interbed treatment reactor device, and the extractant response rate reaches more than 99.5%.
I.e. effectively reduce the processing cost produced because of solvent loss, avoid again secondary waste water to pollute.
(3) extractant excellent performance, processes waste water effect good.Coal chemical industrial waste water is through four process processed waste water
The coal-tar middle oil response rate > 94%, phenol clearance > 99%, COD clearance > 98%.Discharge water and meet follow-up
Ammonia still process processes technological requirement.
Accompanying drawing explanation
Fig. 1 is that in one coal chemical industrial waste water of the present invention, removing system and device schematic diagram combined by carbolic oil；
Wherein, 1-coal chemical industrial waste water storage tank, 2-coke filter, 3-purpose ceramic-film filter, 4-degreased wastewater
Medial launder, 5-heat exchanger, 6-extraction tank, 7-extraction tower, 8-extractant medial launder, 9-intermediate layer handles is reacted
Device, 10-dephenolize water medial launder, 11-Alkali liquid compounding groove, 12-richness phenol organic facies medial launder, in the middle of 13-phenol sodium
Groove, 14-back extraction tower, 15-extractant purifying column, 16-overhead condenser, 17-tar medial launder, 18-purifies
Extractant medial launder.
Detailed description of the invention
Further illustrate technical scheme below in conjunction with the accompanying drawings and by detailed description of the invention.
Fig. 1 is that in one coal chemical industrial waste water of the present invention, removing system and device schematic diagram combined by carbolic oil.
Embodiment 1:
Feed coal wastewater from chemical industry character is shown in Table 1.Handled coal chemical industrial waste water water quality is bronzing, and pH value is
8.9, water temperature is 92 DEG C, and flow 102 ton hour, flow process processes as shown in Figure 1.
Table 1: feed coal wastewater from chemical industry property list (mg/L)
Raw material waste water flows through the solid pollutions such as coal tar, the granule that coke filter 2 removes in coal chemical industrial waste water
Thing.Degreased wastewater enters extraction tank 6 in extracting system after heat exchanger 5 is cooled to 25 DEG C and removes tar and portion
Dividing phenol, extractant is by phenol extraction agent circulation supply rich in extraction tower 7.Extraction tank 6 bottom land discharges waste water from tower
The end, enters extraction tower 7 dephenolize, and extractant is preparation in patent of invention " CN103848468A embodiment "
Extractant 3.
Wherein the preparation method of extractant 3 is: take 14g isopentyl diformazan pentyl ester, 4g 2-ethylhexyl phosphonic acid
Single-2-ethyl hexyl ester-and 5g di-(2-ethylhexyl)phosphoric acid, 2g 3-heptanone, 0.3g propandiol butyl ether,
74.7g kerosene, mix homogeneously at 40 DEG C, it is cooled to room temperature and is the extractant 3 of the present invention.
Extraction oil water is in a ratio of 1:1, and temperature is 20 DEG C.The circulation supply extraction of extraction tower 7 tower top richness phenol organic facies
Groove 6.Dephenolize waste water at the bottom of extraction tower 7 tower enters dephenolize water medial launder 10, treats that further ammonia still process processes.
It is biphase that the intermediate layer that extraction tank 6 and extraction tower 7 produce enters intermediate layer handles reactor 9 oil-water separation,
The oil phase of abjection enters rich phenol organic facies medial launder 12.The aqueous phase of abjection enters dephenolize water medial launder 10, dephenolize
Water treats that follow-up ammonia still process processes.
Rich tar and phenol organic facies that extraction tank 6 is discharged enter back extraction tower 14, and back extraction tower 14 is by 2 back extraction towers
Compose in parallel, phenols in back extraction abjection organic facies.The alkali liquor used is for from alkali liquor configured slot 11 concentration to be
The sodium hydrate aqueous solution of 16%.Back extraction tower 14 tower low crude phenols product enters phenol sodium medial launder 13.Back extraction tower 14
Tower top organic facies enters extractant medial launder 8, recycles.Rich phenol organic facies medial launder 12 is configured by alkali liquor
Groove 11 fills into alkali liquor and synchronizes back extraction, and isolated rich phenol sodium aqueous phase enters phenol sodium medial launder 13, and organic facies enters
Extractant purifying column 15 regenerates.
Extractant regeneration in extractant purifying column 15 is carried out once for every 3 days.Extractant purifying column 15 tower top
Temperature is 130 DEG C, and pressure is 0.12MPa；Extractant purifying column 15 column bottom temperature is 110 DEG C, and pressure is
0.10MPa.Extractant purifying column 15 tower top is discharged extractant and is entered purification extraction after overhead condenser 16 cools down
Take agent medial launder 18, be then pumped into extractant medial launder 8, it is achieved extractant recycles.Extractant purifies
Remove tar at the bottom of tower 15 tower and enter tar tank through tar medial launder 17, recycle.
Respectively oil removing system sewage, extraction tank outlet sewage, back extraction tower waste water discharge opening water quality are carried out at random
Sample analysis, its analysis result is shown in Table 2, table 3, table 4.
Table 2: oil removing system sewage quality information table (randomization)
Table 3: extraction tank outlet water quality information table (randomization)
From table 2 and table 3, this technique can effectively remove, reclaim tar, and clearance is more than 98%, returns
Receive utilization rate more than 94%.
Table 4: back extraction tower waste water discharge opening water quality information table (randomization)
As can be seen from Table 4, after in coal chemical industrial waste water of the present invention, removing system combined by carbolic oil, Coal Chemical Industry
In waste water, total phenols clearance reaches 94.16%, and tar clearance is more than 98%, and recovery utilization rate is more than 94%.
COD clearance 98.68%.
Embodiment 2:
Except the waste water of extraction process degreased wastewater medial launder 4 is cooled to 20 DEG C through heat exchanger 5, in extraction tower 7
Profit is in a ratio of 1:3, and in extraction tower 7, extraction temperature is 25 DEG C, and in alkali liquor configured slot 11, sodium hydroxide is water-soluble
Liquid mass concentration is 10%, and back extraction tower 14 is made up of 1 back extraction tower, the extraction in extractant purifying column 15
Agent regeneration is carried out once for every 2 days, and extractant purifying column 15 tower top temperature is 120 DEG C, extractant purifying column 15
Tower top pressure is 0.05MPa, and extractant purifying column 15 column bottom temperature is 135 DEG C, extractant purifying column 15 tower
Bottom pressure is outside 0.15MPa, and remaining process is the most in the same manner as in Example 1, through coal chemical industrial waste water of the present invention
After removing system combined by middle carbolic oil, in coal chemical industrial waste water, total phenols clearance reaches 95.20%, and tar clearance is more than
99%, recovery utilization rate is more than 94%, COD clearance 98.72%.
Embodiment 3:
The waste water of degreased wastewater medial launder 4 is cooled to 50 DEG C through heat exchanger 5, and in extraction tower 7, profit is in a ratio of
1:5, in extraction tower 7, extraction temperature is 30 DEG C, sodium hydrate aqueous solution mass concentration in alkali liquor configured slot 11
Being 30%, back extraction tower 14 is composed in parallel by 3 back extraction towers, the extractant regeneration in extractant purifying column 15
Within every 5 days, carrying out once, extractant purifying column 15 tower top temperature is 180 DEG C, extractant purifying column 15 tower top pressure
Power is 0.25MPa, and extractant purifying column 15 column bottom temperature is 150 DEG C, extractant purifying column 15 tower bottom pressure
For 0.2MPa, remaining process is the most in the same manner as in Example 1, carbolic oil associating in coal chemical industrial waste water of the present invention
After removing system, in coal chemical industrial waste water, total phenols clearance reaches 94.10%, and tar clearance is more than 98%, reclaims
Utilization rate is more than 95%, COD clearance 99.20%.
In sum, in a kind of coal chemical industrial waste water that the present invention announces, carbolic oil combines removing system and place's science and engineering
Skill, coal chemical industrial waste water treated total phenols clearance is more than 94%, and tar clearance is more than 98%, recycles
Rate is more than 94%, and COD clearance is more than 98%.This technology utilization intermediate layer handles reactor assembly is by emulsifying
Water-oil phase is completely separated, and extractant cyclic utilization rate is high.Phenol extraction agent rich in extraction tower is recycled to extraction
Groove, utilizes useless extractant to carry the tar separated in coal chemical industrial waste water, finally removes out at extractant purifying column
Crude tar oil product, it is to avoid the wasting phenomenon of tar product, processed waste water meets factory subsequent technique and wants
Ask, it is possible to reuse.
Applicant states, the present invention illustrates the method detailed of the present invention by above-described embodiment, but the present invention
It is not limited to above-mentioned method detailed, does not i.e. mean that the present invention has to rely on above-mentioned method detailed ability real
Execute.Person of ordinary skill in the field is it will be clearly understood that any improvement in the present invention, to product of the present invention
The equivalence of each raw material is replaced and the interpolation of auxiliary element, concrete way choice etc., all falls within the guarantor of the present invention
Within the scope of protecting scope and disclosure.
Claims (11)
1. in a coal chemical industrial waste water, removing system combined by carbolic oil, it is characterised in that described system includes oil removing system, extracting system, back extraction system and cleaning system successively.
System the most according to claim 1, it is characterised in that described oil removing system includes coal chemical industrial waste water storage tank (1), coke filter (2), purpose ceramic-film filter (3) and degreased wastewater medial launder (4) successively.
nullSystem the most according to claim 1 and 2，It is characterized in that，Described extracting system includes heat exchanger (5)、Extraction tank (6)、Extraction tower (7)、Extractant medial launder (8)、Intermediate layer handles reactor (9)、Dephenolize water medial launder (10) and Alkali liquid compounding groove (11)，Wherein heat exchanger (5) discharging opening is connected with extraction tank (6) charging aperture，Extraction tank (6) bottom discharge mouth is connected with extraction tower (7) tower top charging aperture，The intermediate layer discharging opening of extraction tank (6) is connected with intermediate layer handles reactor (9) charging aperture，Extraction tower (7) tower top discharging opening is connected with extraction tank (6) extractant entrance，The intermediate layer discharging opening of extraction tower (7) is connected with intermediate layer handles reactor (9) charging aperture，Discharging opening at the bottom of extraction tower (7) tower is connected with dephenolize water medial launder (10) charging aperture，Extractant medial launder (8) discharging opening is connected with extraction tower (7) extractant entrance，The outlet of intermediate layer handles reactor (9) aqueous phase is connected with dephenolize water medial launder (10) charging aperture.
4. according to the system described in any one of claim 1-3, it is characterized in that, described back extraction system includes back extraction tower (14), rich phenol organic facies medial launder (12) and phenol sodium medial launder (13), wherein discharging opening at the bottom of back extraction tower (14) tower is connected with phenol sodium medial launder (13) charging aperture, and rich phenol organic facies medial launder (12) aqueous phase discharging opening is connected with phenol sodium medial launder (13) charging aperture；
Preferably, the number of described back extraction tower (14) is 1,2 or 3.
5. according to the system described in any one of claim 1-4, it is characterized in that, described cleaning system includes extractant purifying column (15), overhead condenser (16), tar medial launder (17) and purifies extractant medial launder (18), wherein extractant purifying column (15) tower top discharging opening is connected with overhead condenser (16) charging aperture, overhead condenser (16) exports and purifies extractant medial launder (18) charging aperture and be connected, and at the bottom of extractant purifying column (15) tower, discharging opening is connected with tar medial launder (17).
null6. according to the system described in any one of claim 1-5，It is characterized in that，In described oil removing system, degreased wastewater medial launder (4) discharging opening is connected with heat exchanger (5) entrance，Extraction tank (6) top discharge mouth is connected with back extraction tower (14) tower top charging aperture，Intermediate layer handles reactor (9) discharging opening is connected with rich phenol organic facies medial launder (12) charging aperture，Alkali liquid compounding groove (11) discharging opening is connected with charging aperture at the bottom of back extraction tower (14) tower and rich phenol organic facies medial launder (12) charging aperture，Back extraction tower (14) tower top discharging opening is connected with extractant medial launder (8) charging aperture，Back extraction tower (14) tower top discharging opening is connected with charging aperture at the bottom of extractant purifying column (15) tower，Rich phenol organic facies medial launder (12) organic facies discharging opening is connected with charging aperture at the bottom of extractant purifying column (15) tower，Purify extractant medial launder (18) discharging opening to be connected with extractant medial launder (8) charging aperture.
7. the process technique of a system as described in any one of claim 1-6, it is characterised in that described process technique includes oil removal process, extraction process, stripping process and purification process successively.
Process technique the most according to claim 7, it is characterized in that, described oil removal process is preprocessing process, it comprises the following steps: coal chemical industrial waste water enters coal chemical industrial waste water storage tank (1), flows through coke filter (2) successively and purpose ceramic-film filter (3) enters degreased wastewater medial launder (4)；
Preferably, described extraction process comprises the following steps:
(1) extraction detar: the waste water of degreased wastewater medial launder (4) enters extraction tank (6) detar and phenol after heat exchanger (5) is lowered the temperature, the waste water that extraction tank (6) bottom land is discharged enters extraction tower (7), in extraction tank (7), rich tar and phenol organic facies enter back extraction tower (14), and extraction tank (6) intermediate layer liquid enters intermediate layer handles reactor (9)；
(2) extracting and dephenolizing: the waste water that extraction tank (6) bottom land is discharged enters extraction tower (7), extractant is entered extraction tower by extractant medial launder (8), extraction tower (7) tower top richness phenol organic facies enters extraction tank (6), extraction tower (7) intermediate layer liquid enters intermediate layer handles reactor (9), and waste water at the bottom of extraction tower (7) tower enters dephenolize water medial launder (10)；
(3) process of intermediate layer liquid: the oil phase that intermediate layer handles reactor (9) is deviate from enters rich phenol organic facies medial launder (12), the aqueous phase that intermediate layer handles reactor (9) is deviate from enters dephenolize water medial launder (10)；
Preferably, described stripping process comprises the following steps: in extraction tank (6), rich tar and phenol organic facies enter back extraction tower (14), back extraction tower (14) bottom product enters phenol sodium medial launder (13), back extraction tower (14) tower top organic facies enters extractant medial launder (8) and extractant purifying column (15), in alkali liquor configured slot (11), alkali liquor enters back extraction tower (14) and rich phenol organic facies medial launder (12), the isolated rich phenol sodium aqueous phase of rich phenol organic facies medial launder (12) enters phenol sodium medial launder (13), rich phenol organic facies medial launder (12) isolated organic facies enters extractant purifying column (15)；
Preferably, described purification process comprises the following steps: back extraction tower (14) tower top organic facies and rich phenol organic facies medial launder (12) isolated organic facies enter extractant purifying column (15) regenerating extracting agent, the extractant that extractant purifying column (15) tower top is discharged enters after overhead condenser (16) condenses and purifies extractant medial launder (18), pumping into extractant medial launder (8) again, the tar discharged at the bottom of extractant purifying column (15) tower enters tar medial launder (17).
9. according to the process technique described in claim 7 or 8, it is characterised in that in described extraction process step (1), the waste water of degreased wastewater medial launder (4) is cooled to 20～50 DEG C through heat exchanger (5)；
Preferably, in described extraction process step (1), in extraction tank (6), extractant is extraction tower (7) tower top richness phenol organic facies；
Preferably, in described extraction process step (2) extractant medial launder (8), extractant is the phenol ammonia waste water extractant that patent CN103848468A is announced；
Preferably, in described extraction process step (2) extraction tower (7), profit phase volume ratio is 1:1～5；
Preferably, in described extraction process step (2) extraction tower (7), extraction temperature is 20～30 DEG C.
10. according to the process technique described in any one of claim 7-9, it is characterised in that in described stripping process alkali liquor configured slot (11), alkali liquor is sodium hydrate aqueous solution；
Preferably, in described stripping process alkali liquor configured slot (11), the mass concentration of sodium hydrate aqueous solution is 10～30%；
Preferably, in described stripping process, back extraction tower (14) tower top organic facies and rich phenol organic facies medial launder (12) isolated organic facies interval enter extractant purifying column (15).
11. according to the process technique described in any one of claim 7-10, it is characterised in that in described purification process, extractant purifying column carries out the operation of primary recycling extractant for (15) 2～5 days；
Preferably, in described purification process, extractant purifying column (15) tower top temperature is 120～180 DEG C；
Preferably, in described purification process, extractant purifying column (15) tower top pressure is 0.05～0.25MPa；
Preferably, in described purification process, extractant purifying column (15) column bottom temperature is 110～150 DEG C；
Preferably, in described purification process, extractant purifying column (15) tower bottom pressure is 0.10～0.20MPa.
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| CN201510147583.5A CN106145426B (en) | 2015-03-31 | 2015-03-31 | Carbolic oil joint removing system and treatment process in a kind of coal chemical industrial waste water |
| PCT/CN2015/079705 WO2016155101A1 (en) | 2015-03-31 | 2015-05-25 | System and treatment process for combined removal of phenol oil from phenol-ammonia wastewater |
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| CN201510147583.5A CN106145426B (en) | 2015-03-31 | 2015-03-31 | Carbolic oil joint removing system and treatment process in a kind of coal chemical industrial waste water |
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| CN106145426B (en) | 2019-04-09 |
| WO2016155101A1 (en) | 2016-10-06 |
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