CN106145426B - Carbolic oil joint removing system and treatment process in a kind of coal chemical industrial waste water - Google Patents
Carbolic oil joint removing system and treatment process in a kind of coal chemical industrial waste water Download PDFInfo
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Abstract
The present invention provides carbolic oil joint removing system and treatment process in a kind of coal chemical industrial waste water comprising oil removing system, extracting system, back extraction system and purification system and its corresponding technical process.Wherein extraction process includes the following steps: that (1) extracts tar, and waste tar is recycled；(2) extracting and dephenolizing, waste water phenol removal rate is up to 99.7% or more；(3) recycling of middle layer.Extractant, phenols are sufficiently recycled, and secondary waste water is avoided to pollute.Waste tar and phenol in coal chemical industrial wastewater processing system provided by the invention and its treatment process energy simultaneous removing, recycling waste water, realize that extractant recycles to the greatest extent.The present invention is small, at low cost to the change of factory's original equipment, stable, and total phenol removal rate is discharged after processing and is greater than 94%, COD removal rate greater than 98%, meets the subsequent ammonia still process processing requirement of sewage.
Description
Technical field
The invention belongs to water-treatment technology field, in particular to carbolic oil joint removing system and place in a kind of coal chemical industrial waste water
Science and engineering skill.
Background technique
Coal chemical industrial waste water is the industrial wastewater that the processes such as coking, gas purification and chemical products purification generate, and is mainly contained
The heterocyclic compounds such as volatile phenol, polycyclic aromatic hydrocarbon and oxygen, sulphur, nitrogen are a kind of high COD, high phenol value, high ammonia nitrogen and very intractable work
Industry organic wastewater.Its purification for mostling come from the waste water and tar, crude benzol etc. that generate during remained ammonia, gas purification
And the waste water that other occasions generate.Coal chemical industrial waste water is the industrial wastewater containing a large amount of persistent organic pollutants, discharge beyond standards
Serious pollution is caused to environment.
Due to the water quality and quantity variation greatly, complicated component, so handle coal chemical industrial waste water technique it is also numerous.It is domestic to adopt more
With pretreatment oil removing, air- extraction removes ammonia, and extraction removes phenol, cyanogen, the processes such as Biochemical method.
Patent CN10332067A discloses a kind of new method for the treatment of of residual coking ammonia water.The invention is by five process groups
At: ammonia still process depickling, air lift dephenolize, extracting and dephenolizing, oxidation processes and water reuse.
Patent CN101597124A discloses a kind of method for handling the coal gasification waste water containing coal chemical industry, and this method includes single column
Pressurization stripping removing sour gas and ammonia, survey line extraction gas three-level segregates, diisopropyl ether extracts phenol, solvent recovery process, and
To crude phenols product.The invention solvent recovery tower and solvent stripper recycle extractant, obtain crude phenols, and realize coal gasification waste water
The process of single column joint removing sour gas and ammonia.
But above-mentioned each technique is only detar, is not recycled to the biggish tar of content in coal chemical industrial waste water.
And significant problem is always existed in unresolved extraction process, that is, extract the presence of middle layer.The generation for extracting middle layer can wave
Take the resources such as a large amount of extractants and recyclable phenols, can lead to factory and be unable to normal operation, when serious or even needs to stop production whole
It controls.
Summary of the invention
In order to overcome the above-mentioned deficiencies of the prior art, the present invention provides carbolic oil joint removing works in a kind of coal chemical industrial waste water
Skill.Coke tar recovery system and middle layer recovery system are added on original Process ba- sis, are improved process, are solved existing extraction process
The a large amount of middle layers of middle generation and unserviceable problem, improve the recovery utilization rate of extractant, phenol etc., in combined recovery waste water
The higher byproduct tar class of content reduces pollutant discharge amount to reduce cost for wastewater treatment, makes the COD content of water outlet
Reach subsequent processing requirement.
To achieve this purpose, the present invention adopts the following technical scheme:
Carbolic oil joint removing system in a kind of coal chemical industrial waste water, the system successively includes oil removing system, extracting system, anti-
Extraction system and purification system.
The oil removing system successively includes coal chemical industrial waste water storage tank, coke filter, purpose ceramic-film filter and degreased wastewater
Medial launder, coal chemical industrial waste water are stored in coal chemical industrial waste water storage tank, and coke filter and purpose ceramic-film filter are for removing coalification
Solid pollutant and fraction solids tar in work waste water.
The extracting system includes heat exchanger, extraction tank, extraction tower, extractant medial launder, intermediate layer handles reactor, takes off
Phenol water medial launder and Alkali liquid compounding slot, wherein heat exchanger discharge port is connected with extraction tank feed inlet, extraction tank bottom discharge port with
Extraction and is connected at column overhead feed inlet, and the middle layer discharge port of extraction tank is connected with intermediate layer handles reactor feed mouth, extracts
Column overhead discharge port is connected with extraction tank extractant entrance, the middle layer discharge port of extraction tower and intermediate layer handles reactor feed
Mouth is connected, and extraction tower tower bottom discharge port is connected with dephenolize water medial launder feed inlet, and extractant medial launder discharge port and extraction tower extract
Agent entrance is taken to be connected, the outlet of intermediate layer handles reactor water phase is connected with dephenolize water medial launder feed inlet.
The back extraction system includes back extraction tower, rich phenol organic phase medial launder and phenol sodium medial launder, wherein back extraction tower tower bottom goes out
Material mouth is connected with phenol sodium medial launder feed inlet, and rich phenol organic phase medial launder water phase discharge port is connected with phenol sodium medial launder feed inlet.
Preferably, the number of the back extraction tower is 1,2 or 3, in technical process can for 1 back extraction tower, 2 it is anti-
Extract tower parallel connection or 3 back extraction towers are in parallel.
The purification system includes extractant purifying column, overhead condenser, tar medial launder and purifies extractant medial launder,
Wherein extractant purification column overhead discharge port is connected with overhead condenser feed inlet, in overhead condenser outlet and purification extractant
Between slot feed inlet be connected, extractant purifying column tower bottom discharge port is connected with tar medial launder.
Degreased wastewater medial launder discharge port is connected with heat exchanger entrance in the oil removing system, extraction tank top discharge mouth with
It is stripped column overhead feed inlet to be connected, intermediate layer handles reactor discharge port is connected with rich phenol organic phase medial launder feed inlet, lye
Make-up tank discharge port is connected with back extraction tower tower bottom feed inlet and rich phenol organic phase medial launder feed inlet, be stripped column overhead discharge port and
Extractant medial launder feed inlet is connected, and back extraction column overhead discharge port is connected with extractant purifying column tower bottom feed inlet, and rich phenol is organic
Phase medial launder organic phase discharge port is connected with extractant purifying column tower bottom feed inlet, purification extractant medial launder discharge port and extraction
Agent medial launder feed inlet is connected.
The treatment process of carbolic oil joint removing system, the treatment process include oil removing in coal chemical industrial waste water described above
Journey, extraction process, stripping process and purification process.
The oil removal process is preprocessing process comprising following steps: coal chemical industrial waste water enters coal chemical industrial waste water storage tank,
Enter degreased wastewater medial launder followed by coke filter and purpose ceramic-film filter, coke filter and purpose ceramic-film filter are de-
Except the solid pollutant and fraction solids tar in coal chemical industrial waste water, removes object and carry out burning disposal, treated, and waste water enters
Degreased wastewater medial launder.
The extraction process the following steps are included:
(1) extract detar: the waste water of degreased wastewater medial launder enters extraction tank after heat exchanger cools down, will with extraction
Tar and phenol extraction in waste water go out.The rich phenol organic phase circulation supply that extractant used is extracted by extraction tower, extraction tank
The waste water of slot bottom discharge enters extraction tower, and the rich tar and phenol organic phase extracted in extraction tank enters back extraction tower, in extraction tank
Interbed liquid enters intermediate layer handles reactor.
(2) extracting and dephenolizing: the waste water of extraction tank slot bottom discharge enters extraction tower, and extractant used comes from extractant medial launder
And enter the phenols in extraction tower counter-current extraction waste water.Column overhead richness phenol organic phase is extracted as extractant circulation supply to extraction
Slot, extraction tower middle layer liquid enter intermediate layer handles reactor, and extraction tower tower bottom dephenolize waste water enters dephenolize water medial launder, to
Further subsequent processing.
(3) processing of middle layer liquid: intermediate layer handles reactor oil-water separation two-phase, the oil of abjection mutually have into rich phenol
The water phase of machine phase medial launder, the abjection of intermediate layer handles reactor enters dephenolize water medial launder.
The stripping process is the following steps are included: the rich tar and phenol organic phase of the discharge of extraction process extraction tank enter back extraction
Tower, through the phenol in back extraction removing organic phase, used lye comes from lye configured slot.Tower tower bottom crude phenols product is stripped to enter
Phenol sodium medial launder, back extraction column overhead organic phase enter extractant medial launder and extractant purifying column, in lye configured slot lye into
Enter to be stripped tower and rich phenol organic phase medial launder.Rich phenol organic phase medial launder periodically fills into the synchronous back extraction of lye by lye configured slot,
The rich phenol sodium water phase that rich phenol organic phase medial launder is isolated enters phenol sodium medial launder, and rich phenol organic phase medial launder is isolated organic
Mutually enter extractant purifying column.
The purification process is the following steps are included: back extraction column overhead organic phase has with what rich phenol organic phase medial launder was isolated
Mutually interval enters extractant purifying column regenerating extracting agent to machine, carries out within 2~5 days the primary operation.Extractant purifies column overhead discharge
Extractant enter purification extractant medial launder after overhead condenser, then be pumped into extractant medial launder, realize extractant circulation
It utilizes.The tar of extractant purifying column tower bottom discharge, which enters tar medial launder and is transferred to tar storage tank again, to be recycled.
The waste water of degreased wastewater medial launder is cooled to 20~50 DEG C through heat exchanger in the extraction process step (1), 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..
Extractant is extraction column overhead richness phenol organic phase in extraction tank in the extraction process step (1), keeps rich phenol organic
Mutually recycled.
Extractant is the coal chemical industry that patent CN103848468A is announced in extraction process step (2) the extractant medial launder
Waste water extractant, the extractant contain following components by mass fraction:
Neutrality contains phosphorus extractant 4~25%
Acidity contains phosphorus extractant 0.5~10%
Cosolvent 0.5~5%
Diluent 60~95%
Because the formula of extractant be disclosed in the prior art, no longer its specific ingredient is repeated herein.
Grease phase volume ratio 1:1~5 in 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..
Extraction temperature is 20~30 DEG C in extraction process step (2) extraction tower, 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..
Lye is sodium hydrate aqueous solution in the stripping process lye configured slot.
In the stripping process lye configured slot mass concentration of sodium hydrate aqueous solution be 10~30%, such as 10%,
13%, 15%, 17%, 20%, 23%, 25%, 27% or 30% etc..
Be stripped column overhead organic phase in the stripping process and organic phase interval that rich phenol organic phase medial launder is isolated into
Enter extractant purifying column.
In the purification process extractant purifying column 2~5 days carry out primary recycling extractant operation, such as 2 days, 3 days,
4 days or 5 days etc..
In the purification process extractant purification column overhead temperatures be 120~180 DEG C, such as 120 DEG C, 125 DEG C, 130 DEG C,
135 DEG C, 140 DEG C, 145 DEG C, 150 DEG C, 155 DEG C, 160 DEG C, 165 DEG C, 170 DEG C, 175 DEG C or 180 DEG C etc..
In the purification process extractant purifying column tower top pressure be 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 the purification process extractant purifying column column bottom temperature be 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 the purification process extractant purifying column tower bottom pressure be 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 invention has the following advantages:
(1) tar product is recycled, waste water resource is made full use of.Existing coal chemical wastewater treating technique mostly uses the skills such as filtering
Art by tar and solid waste in waste water synchronize filter out, the technique for having no effectively recycling tar, and it is more intractable to remove pollutant.This
Phenol extraction agent rich in " extraction tower " is recycled to " extraction tank " by technique, carries the coke in separation coal chemical industrial waste water using useless extractant
Oil finally removes crude tar oil product at " extractant purifying column ".The wasting phenomenon for avoiding tar product, increases wastewater treatment
The output of middle product.
(2) extractant recovery utilization rate is high.The generation of Middle emulsion layer is inevitable in extraction process, from extraction
The Middle emulsion layer removed in slot, extraction tower contains a large amount of organic solvents.This technology utilization intermediate layer handles reactor assembly will
Emulsification water-oil phase is completely separated, and the extractant rate of recovery is up to 99.5% or more.It effectively reduces and to be generated because of solvent loss
Processing cost, and secondary waste water is avoided to pollute.
(3) extractant is had excellent performance, and processing waste water effect is good.Coal chemical industrial waste water is returned through tar in four process processed waste waters
Yield > 94%, phenol removal rate > 99%, COD removal rate > 98%.Discharge water meets subsequent ammonia still process treatment process requirement.
Detailed description of the invention
Fig. 1 is carbolic oil joint removing system and device schematic diagram in a kind of coal chemical industrial waste water of the present invention；
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 reactor, 10- dephenolize water medial launder,
11- Alkali liquid compounding slot, 12- richness phenol organic phase medial launder, 13- phenol sodium medial launder, 14- are stripped tower, 15- extractant purifying column, 16-
Overhead condenser, 17- tar medial launder, 18- purify extractant medial launder.
Specific embodiment
To further illustrate the technical scheme of the present invention below with reference to the accompanying drawings and specific embodiments.
Fig. 1 is carbolic oil joint removing system and device schematic diagram in a kind of coal chemical industrial waste water of the present invention.
Embodiment 1:
Raw material coal chemical industrial waste water property is shown in Table 1.Handled coal chemical industrial waste water water quality is in bronzing, pH value 8.9, water temperature
It is 92 DEG C, 102 ton/hours of flow, process is handled as shown in Figure 1.
Table 1: raw material coal chemical industrial waste water property list (mg/L)
Raw material waste water flows through the solid pollutants such as coal tar, the particle that coke filter 2 removes in coal chemical industrial waste water.De-oiling
Waste water enters extraction tank 6 in extracting system after heat exchanger 5 is cooled to 25 DEG C and removes tar and part phenol, and extractant is by extraction tower
Rich phenol extraction agent circulation supply in 7.6 slot bottom of extraction tank is discharged waste water and enters 7 dephenolize of extraction tower from tower bottom, and extractant is that invention is special
The extractant 3 prepared in sharp " CN103848468A embodiment ".
Wherein extractant 3 the preparation method comprises the following steps: take 14g isopentyl diformazan pentyl ester, 4g 2- ethylhexyl phosphonic acid mono -2- second
Base hexyl ester-and 5g di-(2-ethylhexyl)phosphoric acid, 2g 3- heptanone, 0.3g propandiol butyl ether, 74.7g kerosene mix at 40 DEG C
Uniformly, it is cooled to room temperature as extractant 3 of the invention.
Extraction oil water is comparably 1:1, and temperature is 20 DEG C.7 tower top richness phenol organic phase of extraction tower circulation supply extraction tank 6.Extraction
It takes 7 tower bottom dephenolize waste water of tower to enter dephenolize water medial launder 10, is handled to further ammonia still process.
The middle layer that extraction tank 6 and extraction tower 7 generate enters 9 oil-water separation two-phase of intermediate layer handles reactor, abjection
It is oily mutually to enter rich phenol organic phase medial launder 12.The water phase of abjection enters dephenolize water medial launder 10, and dephenolize water waits for subsequent ammonia still process processing.
The rich tar and phenol organic phase that extraction tank 6 is discharged enter back extraction tower 14, are stripped tower 14 by 2 back extraction tower parallel connection groups
At through phenols in back extraction abjection organic phase.The lye used is the sodium hydroxide water for being 16% from 11 concentration of lye configured slot
Solution.The low crude phenols product of back extraction 14 tower of tower enters phenol sodium medial launder 13.Back extraction 14 tower top organic phase of tower enters extractant medial launder
8, it recycles.Rich phenol organic phase medial launder 12 fills into the synchronous back extraction of lye, the rich phenol sodium water isolated by lye configured slot 11
Mutually enter phenol sodium medial launder 13, organic phase enters extractant purifying column 15 and regenerated.
It carries out within extractant regeneration every 3 days in extractant purifying column 15 primary.15 tower top temperature of extractant purifying column is 130
DEG C, pressure 0.12MPa；15 column bottom temperature of extractant purifying column is 110 DEG C, pressure 0.10MPa.15 tower of extractant purifying column
Top row goes out extractant and enters purification extractant medial launder 18 after overhead condenser 16 is cooling, is then pumped into extractant medial launder 8,
Realize that extractant recycles.15 tower bottom of extractant purifying column removes tar and enters tar tank, recycling through tar medial launder 17
It utilizes.
Grab sample point is carried out to oil removing system sewage, extraction tank outlet sewage, back extraction tower waste water discharge opening water quality respectively
Analysis, analysis the results are shown in Table 2, table 3, table 4.
Table 2: oil removing system sewage quality information table (grab sample)
Table 3: extraction tank exports water quality information table (grab sample)
By table 2 and table 3 it is found that the technique can be removed effectively, recycle tar, removal rate is greater than 98%, and recovery utilization rate is big
In 94%.
Table 4: back extraction tower waste water discharge opening water quality information table (grab sample)
As can be seen from Table 4, total in coal chemical industrial waste water after carbolic oil joint removing system in coal chemical industrial waste water of the present invention
Phenol removal rate is up to 94.16%, and tar removal rate is greater than 98%, and recovery utilization rate is greater than 94%.COD removal rate 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, grease is compared in extraction tower 7
For 1:3, extraction temperature is 25 DEG C in extraction tower 7, and sodium hydrate aqueous solution mass concentration is 10% in lye configured slot 11, back extraction
Tower 14 is made of 1 back extraction tower, carries out within the extractant regeneration in extractant purifying column 15 every 2 days primary, extractant purifying column 15
Tower top temperature is 120 DEG C, and 15 tower top pressure of extractant purifying column is 0.05MPa, and 15 column bottom temperature of extractant purifying column is 135
DEG C, 15 tower bottom pressure of extractant purifying column is outside 0.15MPa, remaining process is in the same manner as in Example 1, by coalification of the present invention
After work Phenol for Waste Water oil joint removing system, up to 95.20%, tar removal rate is greater than total phenol removal rate in coal chemical industrial waste water
99%, recovery utilization rate is greater than 94%, COD removal rate 98.72%.
Embodiment 3:
The waste water of degreased wastewater medial launder 4 is cooled to 50 DEG C through heat exchanger 5, and grease is comparably 1:5 in extraction tower 7, extraction
Extraction temperature is 30 DEG C in tower 7, and sodium hydrate aqueous solution mass concentration is 30% in lye configured slot 11, is stripped tower 14 by 3
Back extraction tower composes in parallel, and carries out within the extractant regeneration in extractant purifying column 15 every 5 days primary, 15 tower top temperature of extractant purifying column
Degree is 180 DEG C, and 15 tower top pressure of extractant purifying column is 0.25MPa, and 15 column bottom temperature of extractant purifying column is 150 DEG C, extraction
15 tower bottom pressure of agent purifying column is 0.2MPa, remaining process is in the same manner as in Example 1, by phenol in coal chemical industrial waste water of the present invention
After oily joint removing system, for total phenol removal rate up to 94.10%, tar removal rate is greater than 98% in coal chemical industrial waste water, recycles
Rate is greater than 95%, COD removal rate 99.20%.
In conclusion carbolic oil joint removing system and treatment process, coalification in a kind of coal chemical industrial waste water that the present invention announces
Work waste water is greater than 94% through processing total phenol removal rate, and tar removal rate is greater than 98%, and recovery utilization rate is removed greater than 94%, COD
Rate is greater than 98%.This technology utilization intermediate layer handles reactor assembly is completely separated water-oil phase is emulsified, extractant circulation benefit
With rate height.Phenol extraction agent rich in extraction tower is recycled to extraction tank, carries the coke in separation coal chemical industrial waste water using useless extractant
Oil finally removes out crude tar oil product in extractant purifying column, avoids the wasting phenomenon of tar product, and processed waste water meets
The requirement of factory's subsequent technique, can also reuse.
The Applicant declares that the present invention is explained by the above embodiments method detailed of the invention, but the present invention not office
Be limited to above-mentioned method detailed, that is, do not mean that the invention must rely on the above detailed methods to implement.Technical field
Technical staff it will be clearly understood that any improvement in the present invention, equivalence replacement and auxiliary element to each raw material of product of the present invention
Addition, selection of concrete mode etc., all of which fall within the scope of protection and disclosure of the present invention.
Claims (23)
1. carbolic oil joint removing system in a kind of coal chemical industrial waste water, which is characterized in that the system successively includes oil removing system, extraction
Take system, back extraction system and purification system；
The 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 slot (11), wherein heat exchanger (5) discharge port and extraction tank (6) are fed
Mouthful be connected, extraction tank (6) bottom discharge port is connected with extraction tower (7) tower top feed inlet, the middle layer discharge port of extraction tank (6) and
Intermediate layer handles reactor (9) feed inlet is connected, and extraction tower (7) tower top discharge port is connected with extraction tank (6) extractant entrance, extraction
The middle layer discharge port of tower (7) is taken to be connected with intermediate layer handles reactor (9) feed inlet, extraction tower (7) tower bottom discharge port and de-
Phenol water medial launder (10) feed inlet is connected, and extractant medial launder (8) discharge port is connected with extraction tower (7) extractant entrance, intermediate
The outlet of layer treatment reactor (9) water phase is connected with dephenolize water medial launder (10) feed inlet.
2. system according to claim 1, which is characterized in that the oil removing system successively includes coal chemical industrial waste water storage tank
(1), coke filter (2), purpose ceramic-film filter (3) and degreased wastewater medial launder (4).
3. system according to claim 1, which is characterized in that the back extraction system is organic including back extraction tower (14), rich phenol
Phase medial launder (12) and phenol sodium medial launder (13), wherein back extraction tower (14) tower bottom discharge port and phenol sodium medial launder (13) feed inlet phase
Even, rich phenol organic phase medial launder (12) water phase discharge port is connected with phenol sodium medial launder (13) feed inlet.
4. system according to claim 3, which is characterized in that the number of back extraction tower (14) is 1,2 or 3.
5. system according to claim 3, which is characterized in that the purification system includes extractant purifying column (15), tower
Condenser (16), tar medial launder (17) and purification extractant medial launder (18) are pushed up, wherein extractant purifying column (15) tower top goes out
Material mouth is connected with overhead condenser (16) feed inlet, overhead condenser (16) outlet and purification extractant medial launder (18) feed inlet
It is connected, extractant purifying column (15) tower bottom discharge port is connected with tar medial launder (17).
6. system according to claim 5, which is characterized in that degreased wastewater medial launder (4) discharges in the oil removing system
Mouth is connected with heat exchanger (5) entrance, and extraction tank (6) top discharge mouth is connected with back extraction tower (14) tower top feed inlet, at middle layer
Reason reactor (9) discharge port is connected with rich phenol organic phase medial launder (12) feed inlet, Alkali liquid compounding slot (11) discharge port and back extraction
Tower (14) tower bottom feed inlet is connected with rich phenol organic phase medial launder (12) feed inlet, is stripped tower (14) tower top discharge port and extractant
Medial launder (8) feed inlet is connected, and back extraction tower (14) tower top discharge port is connected with extractant purifying column (15) tower bottom feed inlet, rich phenol
Organic phase medial launder (12) organic phase discharge port is connected with extractant purifying column (15) tower bottom feed inlet, purifies extractant medial launder
(18) discharge port is connected with extractant medial launder (8) feed inlet.
7. a kind for the treatment of process of the system as described in claim any one of 1-6, which is characterized in that the treatment process is successively wrapped
Include oil removal process, extraction process, stripping process and purification process；
The extraction process the following steps are included:
(1) extract detar: the waste water of degreased wastewater medial launder (4) enters extraction tank (6) detar after heat exchanger (5) cool down
And phenol, the waste water of extraction tank (6) slot bottom discharge enter extraction tower (7), rich tar and phenol organic phase enter back extraction in extraction tank (7)
Tower (14), extraction tank (6) middle layer liquid enter intermediate layer handles reactor (9)；
(2) extracting and dephenolizing: the waste water of extraction tank (6) slot bottom discharge enters extraction tower (7), and extractant is by extractant medial launder (8)
Into extraction tower, extraction tower (7) tower top richness phenol organic phase enters extraction tank (6), and extraction tower (7) middle layer liquid enters middle layer
Treatment reactor (9), extraction tower (7) tower bottom waste water enter dephenolize water medial launder (10)；
(3) processing of middle layer liquid: the oil of intermediate layer handles reactor (9) abjection mutually enters rich phenol organic phase medial launder
(12), the water phase of intermediate layer handles reactor (9) abjection enters dephenolize water medial launder (10).
8. treatment process according to claim 7, which is characterized in that the oil removal process is preprocessing process comprising
Following steps: coal chemical industrial waste water enters coal chemical industrial waste water storage tank (1), followed by coke filter (2) and purpose ceramic-film filter
(3) enter degreased wastewater medial launder (4).
9. treatment process according to claim 7, which is characterized in that the stripping process is the following steps are included: extraction tank
(6) rich tar and phenol organic phase enter back extraction tower (14) in, and back extraction tower (14) bottom product enters phenol sodium medial launder (13), is stripped
Tower (14) tower top organic phase enters extractant medial launder (8) and extractant purifying column (15), in lye configured slot (11) lye into
Enter to be stripped tower (14) and rich phenol organic phase medial launder (12), the rich phenol sodium water phase that rich phenol organic phase medial launder (12) is isolated enters
Phenol sodium medial launder (13), the organic phase that rich phenol organic phase medial launder (12) is isolated enter extractant purifying column (15).
10. treatment process according to claim 7, which is characterized in that the purification process is the following steps are included: back extraction tower
(14) organic phase that tower top organic phase and rich phenol organic phase medial launder (12) are isolated enters extractant purifying column (15) regeneration extraction
Agent is taken, the extractant of extractant purifying column (15) tower top discharge enters after overhead condenser (16) condensation among purification extractant
Slot (18), then extractant medial launder (8) are pumped into, the tar of extractant purifying column (15) tower bottom discharge enters tar medial launder
(17)。
11. treatment process according to claim 7, which is characterized in that in the extraction process step (1) in degreased wastewater
Between the waste water of slot (4) be cooled to 20~50 DEG C through heat exchanger (5).
12. treatment process according to claim 7, which is characterized in that extraction tank (6) in the extraction process step (1)
Middle extractant is extraction tower (7) tower top richness phenol organic phase.
13. treatment process according to claim 7, which is characterized in that extraction process step (2) the extractant medial launder
(8) extractant contains following components by mass fraction in: neutrality contains phosphorus extractant 0.5 containing phosphorus extractant 4~25%, acidity
~10%, cosolvent 0.5~5%, diluent 60~95%.
14. treatment process according to claim 7, which is characterized in that in extraction process step (2) extraction tower (7)
Grease phase volume ratio is 1:1~5.
15. treatment process according to claim 7, which is characterized in that in extraction process step (2) extraction tower (7)
Extraction temperature is 20~30 DEG C.
16. treatment process according to claim 9, which is characterized in that alkali in the stripping process lye configured slot (11)
Liquid is sodium hydrate aqueous solution.
17. treatment process according to claim 9, which is characterized in that hydrogen in the stripping process lye configured slot (11)
The mass concentration of aqueous solution of sodium oxide is 10~30%.
18. treatment process according to claim 9, which is characterized in that being stripped tower (14) tower top in the stripping process has
The organic phase interval that machine phase and rich phenol organic phase medial launder (12) are isolated enters extractant purifying column (15).
19. treatment process according to claim 10, which is characterized in that extractant purifying column (15) in the purification process
Carry out within 2~5 days the operation of primary recycling extractant.
20. treatment process according to claim 10, which is characterized in that extractant purifying column (15) in the purification process
Tower top temperature is 120~180 DEG C.
21. treatment process according to claim 10, which is characterized in that extractant purifying column (15) in the purification process
Tower top pressure is 0.05~0.25MPa.
22. treatment process according to claim 10, which is characterized in that extractant purifying column (15) in the purification process
Column bottom temperature is 110~150 DEG C.
23. treatment process according to claim 10, which is characterized in that extractant purifying column (15) in the purification process
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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| CN107434335B (en) * | 2017-09-01 | 2021-01-12 | 中国科学院过程工程研究所 | Comprehensive treatment method for recycling semi-coke wastewater phenol ammonia |
| CN107827315B (en) * | 2017-10-27 | 2020-08-04 | 陕西煤业化工集团神木天元化工有限公司 | Semi-coke wastewater treatment method |
| CN108751317A (en) * | 2018-07-25 | 2018-11-06 | 合肥中亚环保科技有限公司 | A kind of novel extraction dephenolize system |
| CN108862800A (en) * | 2018-08-02 | 2018-11-23 | 合肥中亚环保科技有限公司 | A kind of coal gasification phenol wastewater ammonia still process extraction multiple treating system and its processing method |
| CN109651092B (en) * | 2019-01-24 | 2024-01-05 | 山西永东化工股份有限公司 | Clean production method and device for gas circulation coking crude phenol |
| CN109734149A (en) * | 2019-03-15 | 2019-05-10 | 北京赛科康仑环保科技有限公司 | A kind of coal chemical industrial waste water pre-extracted waste-oil scavenger |
| CN110330988A (en) * | 2019-07-25 | 2019-10-15 | 内蒙古万众炜业科技环保股份公司 | A kind of wholegrain diameter coal cracking sub-prime utilizes production technology |
| CN110655259B (en) * | 2019-10-18 | 2021-11-02 | 北京赛科康仑环保科技有限公司 | Coal chemical wastewater extraction dephenolization recycling treatment process |
| CN112062332A (en) * | 2020-09-02 | 2020-12-11 | 查都（上海）科技有限公司 | Semi-coke phenolic wastewater phenol extraction process |
| CN113264628A (en) * | 2021-05-07 | 2021-08-17 | 内蒙古万众炜业科技环保股份公司 | Comprehensive utilization method of oily ammonia water generated in coal cracking |
| CN114873823B (en) * | 2022-06-10 | 2023-11-28 | 爱智环境科技(西安)有限公司 | Comprehensive treatment device and process method for coking wastewater |
| CN114832436A (en) * | 2022-06-20 | 2022-08-02 | 运城市盐湖区禾呈信息技术有限公司 | Process for extracting crude phenol from phenol oil by secondary extraction of composite extracting agent |
| CN116003222B (en) * | 2022-12-16 | 2024-09-13 | 湖北科林博伦新材料有限公司 | Device and process for recycling benzyl alcohol and phenol from dephenolized residual liquid |
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