CN103496757A - Method for extraction dephenolization of high-concentration chemical wastewater containing phenol ammonia coals - Google Patents
Method for extraction dephenolization of high-concentration chemical wastewater containing phenol ammonia coals Download PDFInfo
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Abstract
The invention discloses a method for extraction dephenolization of high-concentration chemical wastewater containing phenol ammonia coals. According to the method, the high-concentration chemical wastewater containing the phenol ammonia coals is in countercurrent contact with butyl acetate in an extraction tower, an extraction phase is obtained at the top of the tower, and an extraction residual phase is obtained at the bottom of the tower; the extraction phase is subjected to rectification to recover an extracting agent and a product of crude phenol, the extracting agent is recycled, and the crude phenol is sold or refined. Compared with an extraction technology related in the prior art, the recovery energy consumption of butyl acetate is lower, the process flow of the method disclosed by the invention is simple, and the extraction rate of phenol is high. By using the extracting agent in the method, the burden of follow-up biochemical treatment of wastewater can be reduced more effectively, the cost can be saved, and the recycling and up-to-standard release of wastewater are ensured.
Description
Technical field
The present invention relates to the extracting and dephenolizing technical field of coal chemical industrial waste water, relate in particular to the method for extracting and dephenolizing of a kind of high density containing phenol ammonia coal chemical industrial waste water.
Background technology
Coal Chemical Industry can produce a large amount of containing the phenol ammonia waste water in producing, complicated component, and directly discharge can serious environment pollution.Simultaneously, phenols is also important industrial chemicals, and resourcebility is recycled.Thereby, remove efficiently and reclaim the aldehydes matter in coal chemical industrial waste water, not only there is environment protection significance, also there is certain economic implications.
At present, for coal chemical industrial waste water, extraction agent commonly used has isopropyl ether, hexone, tert amyl methyl ether(TAME), heavy benzol, N503 etc.But these extraction agents have its open defect, such as the application number described extraction agent isopropyl ether of patent of invention that is 2012103555982.7 to the extracting power of polyphenol a little less than, the effect of extracting to high-concentration phenol in extraction process of extraction agent hexone described in the patent of invention that application number is 200910192442.X is not good, the market value of isopropyl ether and hexone is higher, and (the isopropyl ether price is at 20000 yuan/tons, the hexone price is at 12000-17000 yuan/ton), and hexone toxicity is larger.When heavy benzol and N503 extraction, the solvent partition ratio is low, and long flow path consumes high.
As the patent of invention that on September 19th, 2012, disclosed application number was 20121014513.7 discloses a kind of recovery and treatment method of high-concentration phenol ammonia waste water, at first adopt sour gas to carry out saturated absorption to waste water, adopt again isopropyl ether after reducing PH, hexone, tert amyl methyl ether(TAME) is as the extraction agent dephenolize, and then adopt single tower pressurization stripping to carry out depickling deamination and solution stripping, its not middle part is: on the one hand a little less than the extraction agent extracting power, energy consumption is too high, price is high, first want on the other hand the saturated adjustment of acid adding PH, then also want depickling, complex process, two aspect factors directly cause the low and high cost of the processing efficiency of waste water.
The processing that the patent of invention that the application number of authorizing on May 11st, 2011 for another example is 200910036541.9 provides is containing the method for phenol ammonia coal gasification waste water.Comprise that single tower alkali injection pressurization stripping removes sour gas and ammonia, three grades of fractional condensation of lateral line withdrawal function gas, diisopropyl ether extraction phenol and solvent recuperation process.Change in its scheme and adopt isopropyl ether to carry out phenol extraction, percentage extraction is low, makes the Phenol for Waste Water content overproof of getting.
Summary of the invention
The object of the invention is to overcome has the deficiency existed in technology now, and a kind of extraction efficiency is high and cost the is low high density method for extracting and dephenolizing containing phenol ammonia coal chemical industrial waste water is provided.
For realizing that the technical scheme that purpose of the present invention adopts is: a kind of high density, containing the method for extracting and dephenolizing of phenol ammonia coal chemical industrial waste water, comprises following processing step:
A, take butylacetate as extraction agent, high density is containing phenol ammonia coal chemical industrial waste water and butylacetate counter current contact in extraction tower, obtain extraction phase and extracting phase, extraction temperature is 25-75 ℃, extraction pH=3.0-8.0, butylacetate and high density are 1:10-30 containing phenol ammonia coal chemical industrial waste water input material volume ratio, and the progression of extraction is the 1-12 level;
B, extraction phase is carried out to rectifying, reclaim butylacetate and product crude phenols; The rectification process condition is: rectifying tower progression 8-25 level, and reflux ratio 0.3-0.5, working pressure 0.01-0.09MPa, the tower top service temperature is 35-110 ℃, at the bottom of tower, service temperature is 90-150;
C, by extracting phase distillation, reclaim residual butylacetate; The Distillation recovery processing condition are: distillation tower top service temperature is 35-98 ℃, and the base product service temperature is 105-140 ℃;
D, the butylacetates that step 2 and 3 is reclaimed recycle.
Further, as preferred version of the present invention, in described step a, extraction temperature is 35 ℃, extraction pH=4.0, and butylacetate and high density are 1:15 containing phenol ammonia coal chemical industrial waste water input material volume ratio, the progression of extraction is 5 grades;
In described step b, 15 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.04MPa, the rectifying tower top service temperature is 60 ℃, at the bottom of rectifying tower, service temperature is 120 ℃;
In described step c, distillation tower top service temperature is 40 ℃, and the base product service temperature is 120 ℃.
Further, as another kind of preferred version of the present invention, in described step a, extraction temperature is 65 ℃, extraction pH=6.0, and butylacetate and high density are 1:25 containing phenol ammonia coal chemical industrial waste water input material volume ratio, the progression of extraction is 8 grades;
In described step b, 20 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.07MPa, the rectifying tower top service temperature is 90 ℃, at the bottom of rectifying tower, service temperature is 140 ℃;
In described step c, distillation tower top service temperature is 60 ℃, and the base product service temperature is 130 ℃.
Further, as another preferred version of the present invention, in described step a, extraction temperature is 55 ℃, extraction pH=5.0, and butylacetate and high density are 1:20 containing phenol ammonia coal chemical industrial waste water input material volume ratio, the progression of extraction is 10 grades;
In described step b, 18 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.05MPa, the rectifying tower top service temperature is 75 ℃, at the bottom of rectifying tower, service temperature is 100 ℃;
In described step c, distillation tower top service temperature is 50 ℃, and the base product service temperature is 125 ℃.
The mixed structure tower that described extraction tower is packing tower or tray column or packing tower and tray column.
In the present invention, adopt butylacetate as extraction agent, the butylacetate of equal volume and traditional extraction agent, ethyl acetate can extract more high densitys containing phenol ammonia coal chemical industrial waste water and more phenol, exceeds several times than traditional extraction agent, extracting process of the present invention, when envrionment temperature reaches more than 25 ℃, can heat, extract under normal temperature, effectively save energy consumption, reduce production cost, greatly improved extraction efficiency; Reflux ratio adopts the scope of 0.3-0.5, has both ensured product separation effect, disintegrate-quality, has reduced the costs such as energy consumption and equipment and has dropped into, and makes separating effect, energy consumption, equipment investment reach a desirable equilibrium state, has effectively improved economic benefit; On the one hand effectively reclaim and remain in the butylacetate in extracting phase by distillation, avoid the waste of butylacetate, on the other hand, for follow-up deamination, etc. processing facilitate.
The present invention is at the extraction tower middle and high concentration containing phenol ammonia coal chemical industrial waste water and butylacetate counter current contact, and tower top is extracted phase, obtains extracting phase at the bottom of tower; Extraction phase reclaims extraction agent and product crude phenols by rectifying, the extraction agent recycle, and crude phenols are sold or are refining, with the abstraction technique related in conventional art, compare, and the recovery energy consumption of butylacetate is lower, and technical process of the present invention is simple, and the percentage extraction of phenol is high.Extraction agent in use the present invention can more effectively alleviate the burden of follow-up biochemical treatment waste water, cost-saving, guarantees recycling and the qualified discharge of waste water.
Embodiment
The high density that extraction efficiency of the present invention is high and cost is low, containing the method for extracting and dephenolizing of phenol ammonia coal chemical industrial waste water, comprises following processing step:
A, take butylacetate as extraction agent, high density passes into extraction tower from top and the bottom of extraction tower respectively containing phenol ammonia coal chemical industrial waste water and butylacetate, carry out the counter current contact extraction, obtain extraction phase and extracting phase, extraction temperature is 25-75 ℃, extraction pH=3.0-8.0, butylacetate and high density are 1:10-30 containing phenol ammonia coal chemical industrial waste water input material volume ratio, the progression of extraction is the 1-12 level;
Extraction agent adopts butylacetate, cost is low, extraction efficiency is high, the ethyl acetate of 1 volume can extract the high density of 10-30 times of volume containing phenol ammonia coal chemical industrial waste water, the butylacetate of same volume is compared and can be extracted more phenol with the traditional extraction agent in other words, exceeds the several times of traditional extraction agent.
B, extraction phase is carried out to rectifying, reclaim butylacetate and product crude phenols; The rectification process condition is: rectifying tower progression 8-25 level, and reflux ratio 0.3-0.5, working pressure 0.01-0.09MPa, the tower top service temperature is 35-110 ℃, at the bottom of tower, service temperature is 90-150 ℃;
Adopt rectifying tower reclaim butylacetate and isolate the crude phenols product, efficiency is high, and purity is high, can effectively reduce the content of butylacetate and crude phenols impurity.Reflux ratio of the present invention adopts the scope of 0.3-0.5, has both ensured product separation effect, disintegrate-quality, has reduced the costs such as energy consumption and equipment and has dropped into, and makes separating effect, energy consumption, equipment investment reach a preferably equilibrium state, makes largeizationr of economic benefit.
C, by extracting phase distillation, reclaim residual butylacetate; The Distillation recovery processing condition are: distillation tower top service temperature is 35-98 ℃, and the base product service temperature is 105-140 ℃;
On the one hand effectively reclaim and remain in the butylacetate in extracting phase by distillation, avoid the waste of butylacetate, on the other hand, for follow-up deamination, etc. processing facilitate.
D, the butylacetates that step 2 and 3 is reclaimed recycle, and by recycling butylacetate, have greatly improved the utilization ratio of ethyl acetate, have reduced the extraction production cost.
The mixed structure tower that described extraction tower is packing tower or tray column or packing tower and tray column.
Further, as preferred version of the present invention, in described step a, extraction temperature is 35 ℃, extraction pH=4.0, and butylacetate and high density are 1:15 containing phenol ammonia coal chemical industrial waste water input material volume ratio, the progression of extraction is 5 grades;
In described step b, 15 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.04MPa, the rectifying tower top service temperature is 60 ℃, at the bottom of rectifying tower, service temperature is 120 ℃;
In described step c, distillation tower top service temperature is 40 ℃, and the base product service temperature is 120 ℃.
Further, as another kind of preferred version of the present invention, in described step a, extraction temperature is 65 ℃, extraction pH=6.0, and butylacetate and high density are 1:25 containing phenol ammonia coal chemical industrial waste water input material volume ratio, the progression of extraction is 8 grades;
In described step b, 20 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.07MPa, the rectifying tower top service temperature is 90 ℃, at the bottom of rectifying tower, service temperature is 140 ℃;
In described step c, distillation tower top service temperature is 60 ℃, and the base product service temperature is 130 ℃.
Further, as another preferred version of the present invention, in described step a, extraction temperature is 55 ℃, extraction pH=5.0, and butylacetate and high density are 1:20 containing phenol ammonia coal chemical industrial waste water input material volume ratio, the progression of extraction is 10 grades;
In described step b, 18 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.05MPa, the rectifying tower top service temperature is 75 ℃, at the bottom of rectifying tower, service temperature is 100 ℃;
In described step c, distillation tower top service temperature is 50 ℃, and the base product service temperature is 125 ℃.
Through Applicant none's test and study analysis of repeatability for several times, be surprised to find that butylacetate is in the temperature and pH=4.0-7.0 potential of hydrogen environment of 30-70 ℃, in the situation that other conditions are identical, its extraction efficiency and extraction quality all exceed efficiency and the quality under other temperature and potential of hydrogen.In the identical situation of other conditions, when butylacetate and high density are controlled at 1:15-25 containing phenol ammonia coal chemical industrial waste water input material volume ratio, also show higher extraction quality and extraction efficiency.The test and study analysis of repeatability many times, in reflux ratio, it is 0.4 o'clock, rectifying tower progression can be controlled at the 15-20 level, product separation effect, disintegrate-quality had both been ensured, having reduced the costs such as energy consumption and equipment drops into, make separating effect, energy consumption, equipment investment reach the equilibrium state an of the best, make maximization of economic benefit.In distil process, in this temperature range, the rate of recovery of butylacetate is higher, be more convenient for follow-up deamination and biochemical treatment.
Adopt butylacetate as extraction agent, at the extraction tower middle and high concentration, containing phenol ammonia coal chemical industrial waste water and butylacetate counter current contact, tower top is extracted phase, obtains extracting phase at the bottom of tower; Extraction phase reclaims extraction agent and product crude phenols by rectifying, the extraction agent recycle, and crude phenols are sold or are refining, with the abstraction technique related in conventional art, compare, and the recovery energy consumption of butylacetate is lower, and technical process of the present invention is simple, and the percentage extraction of phenol is high.Extraction agent in use the present invention can more effectively alleviate the burden of follow-up biochemical treatment waste water, cost-saving, guarantees recycling and the qualified discharge of waste water.
embodiment mono-
A set of processing power is the extracting and dephenolizing devices of 80 t/h high densitys containing phenol ammonia coal chemical industrial waste water, and total phenol content is 5000 mg/L, COD 40000 mg/L.
Adopt the method for extracting and dephenolizing of high density of the present invention containing phenol ammonia coal chemical industrial waste water, butylacetate and high density are pumped into from top and the bottom of extraction tower respectively by the 1:10 volume ratio containing phenol ammonia coal chemical industrial waste water, counter current contact, extraction temperature is 25 ℃, extraction pH=3.0, extraction progression is 1 grade, is extracted mutually and extracting phase;
Then process extraction phase by the rectifying mode in rectifying tower, 8 grades of rectifying tower progression, reflux ratio 0.3, working pressure 0.01 MPa, the rectifying tower top service temperature is 35 ℃, at the bottom of tower, service temperature is 105 ℃, reclaims butylacetate and product crude phenols;
Process extracting phase in distillation tower, distillation tower top service temperature is 35 ℃, and the base product service temperature is 105 ℃, reclaims residual butylacetate in extracting phase;
The butylacetate reclaimed enters in the extracting and dephenolizing of next circulation and uses.
Total phenol content in processed waste water is less than 400 mg/L, and COD is less than 1300 mg/L.
embodiment bis-
A set of processing power is the extracting and dephenolizing devices of 130 t/h high densitys containing phenol ammonia coal chemical industrial waste water, and total phenol content is 16320 mg/L, pH=6.0, COD 32500 mg/L.
Adopt the method for extracting and dephenolizing of high density of the present invention containing phenol ammonia coal chemical industrial waste water, butylacetate and high density are pumped into from top and the bottom of extraction tower respectively by the 1:15 volume ratio containing phenol ammonia coal chemical industrial waste water, counter current contact, extraction temperature is 35 ℃, extraction pH=4.0, extraction progression is 5 grades, is extracted mutually and extracting phase;
Extraction phase is carried out to rectifying, 15 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.04 MPa, the rectifying tower top service temperature is controlled at 60 ℃, and at the bottom of tower, service temperature is 120 ℃, reclaims butylacetate and product crude phenols;
Process extracting phase in distillation tower, distillation tower top service temperature is 40 ℃, and the base product service temperature is 120 ℃, reclaims residual butylacetate in extracting phase;
The butylacetate reclaimed enters in the extracting and dephenolizing of next circulation and uses.
Total phenol content in processed waste water is about 350 mg/L, and COD is less than 1800 mg/L.
embodiment tri-
A set of processing power is the extracting and dephenolizing devices of 200 t/h high densitys containing phenol ammonia coal chemical industrial waste water, and total phenol content is 12800 mg/L, pH=8.7, COD 37000 mg/L.
Adopt the method for extracting and dephenolizing of high density of the present invention containing phenol ammonia coal chemical industrial waste water, butylacetate and high density are pumped into from top and the bottom of extraction tower respectively by the 1:25 volume ratio containing phenol ammonia coal chemical industrial waste water, counter current contact, extraction temperature is 65 ℃, extraction pH=6.0, extraction progression is 8 grades, is extracted mutually and extracting phase;
Extraction phase is carried out to rectifying, 20 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.07 MPa, the rectifying tower top service temperature is controlled in 90 ℃, and at the bottom of tower, service temperature is controlled in 140 ℃, reclaims butylacetate and product crude phenols;
Process extracting phase in distillation tower, distillation tower top service temperature is 60 ℃, and the base product service temperature is 130 ℃, reclaims residual butylacetate in extracting phase;
The butylacetate reclaimed enters in the extracting and dephenolizing of next circulation and uses.
Total phenol content in processed waste water is about 380 mg/L, and COD is less than 1500 mg/L.
embodiment tetra-
A set of processing power is the extracting and dephenolizing devices of 350 t/h high densitys containing phenol ammonia coal chemical industrial waste water, and total phenol content is 28600 mg/L, pH=8.7, COD 41000 mg/L.
Adopt the method for extracting and dephenolizing of high density of the present invention containing phenol ammonia coal chemical industrial waste water, butylacetate and high density are pumped into from top and the bottom of extraction tower respectively by the 1:20 volume ratio containing phenol ammonia coal chemical industrial waste water, counter current contact, extraction temperature is 55 ℃, extraction pH=5.0, extraction progression is 10 grades, is extracted mutually and extracting phase;
Extraction phase is carried out to rectifying, 18 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.05 MPa, the rectifying tower top service temperature is 75 ℃, at the bottom of tower, service temperature is 100 ℃, reclaims butylacetate and product crude phenols;
Process extracting phase in distillation tower, distillation tower top service temperature is 50 ℃, and the base product service temperature is 125 ℃, reclaims residual butylacetate in extracting phase;
The butylacetate reclaimed enters in the extracting and dephenolizing of next circulation and uses.
Total phenol content in processed waste water is about 400 mg/L, and COD is less than 2500 mg/L.
embodiment five
A set of processing power is the extracting and dephenolizing devices of 200 t/h high densitys containing phenol ammonia coal chemical industrial waste water, and total phenol content is 18460 mg/L, pH=8.7, COD 41000 mg/L.
Adopt the method for extracting and dephenolizing of high density of the present invention containing phenol ammonia coal chemical industrial waste water, butylacetate and high density are pumped into from top and the bottom of extraction tower respectively by the 1:20 volume ratio containing phenol ammonia coal chemical industrial waste water, counter current contact, extraction temperature is 60 ℃, extraction pH=8.0, extraction progression is 8 grades, is extracted mutually and extracting phase;
Extraction phase is carried out to rectifying, 20 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.07 MPa, the rectifying tower top service temperature is 50 ℃, at the bottom of tower, service temperature is 140 ℃, reclaims butylacetate and product crude phenols;
Process extracting phase in distillation tower, distillation tower top service temperature is 80 ℃, and the base product service temperature is 130 ℃, reclaims residual butylacetate in extracting phase;
The butylacetate reclaimed enters in the extracting and dephenolizing of next circulation and uses.
Total phenol content in processed waste water is about 350 mg/L, and COD is less than 1800 mg/L.
embodiment six
A set of processing power is the extracting and dephenolizing devices of 300 t/h high densitys containing phenol ammonia coal chemical industrial waste water, and total phenol content is 22260 mg/L, COD 48000 mg/L.
Adopt the method for extracting and dephenolizing of high density of the present invention containing phenol ammonia coal chemical industrial waste water, butylacetate and high density are pumped into from top and the bottom of extraction tower respectively by the 1:30 volume ratio containing phenol ammonia coal chemical industrial waste water, counter current contact, extraction temperature is 75 ℃, extraction pH=8.0, extraction progression is 12 grades, is extracted mutually and extracting phase;
Extraction phase is carried out to rectifying, 25 grades of rectifying tower progression, reflux ratio 0.5, working pressure 0.09MPa, the rectifying tower top service temperature is 110 ℃, at the bottom of tower, service temperature is 160 ℃, reclaims butylacetate and product crude phenols;
Process extracting phase in distillation tower, distillation tower top service temperature is 98 ℃, and the base product service temperature is 140 ℃, reclaims residual butylacetate in extracting phase;
The butylacetate reclaimed enters in the extracting and dephenolizing of next circulation and uses.
Total phenol content in processed waste water is about 400 mg/L, and COD is less than 2300 mg/L.
Claims (5)
1. a high density is containing the method for extracting and dephenolizing of phenol ammonia coal chemical industrial waste water, and it is characterized in that: it comprises following processing step:
A, take butylacetate as extraction agent, high density is containing phenol ammonia coal chemical industrial waste water and butylacetate counter current contact in extraction tower, obtain extraction phase and extracting phase, extraction temperature is 25-75 ℃, extraction pH=3.0-8.0, butylacetate and high density are 1:10-30 containing phenol ammonia coal chemical industrial waste water input material volume ratio, and the progression of extraction is the 1-12 level;
B, extraction phase is carried out to rectifying, reclaim butylacetate and product crude phenols; The rectification process condition is: rectifying tower progression 8-25 level, and reflux ratio 0.3-0.5, working pressure 0.01-0.09MPa, the tower top service temperature is 35-110 ℃, at the bottom of tower, service temperature is 90-150;
C, by extracting phase distillation, reclaim residual butylacetate; The Distillation recovery processing condition are: distillation tower top service temperature is 35-98 ℃, and the base product service temperature is 105-140 ℃;
D, the butylacetates that step 2 and 3 is reclaimed recycle.
2. high density as claimed in claim 1 is containing the method for extracting and dephenolizing of phenol ammonia coal chemical industrial waste water, it is characterized in that: in described step a, extraction temperature is 35 ℃, extraction pH=4.0, butylacetate and high density are 1:15 containing phenol ammonia coal chemical industrial waste water input material volume ratio, and the progression of extraction is 5 grades;
In described step b, 15 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.04MPa, the rectifying tower top service temperature is 60 ℃, at the bottom of rectifying tower, service temperature is 120 ℃;
In described step c, distillation tower top service temperature is 40 ℃, and the base product service temperature is 120 ℃.
3. high density as claimed in claim 1 is containing the method for extracting and dephenolizing of phenol ammonia coal chemical industrial waste water, it is characterized in that: in described step a, extraction temperature is 65 ℃, extraction pH=6.0, butylacetate and high density are 1:25 containing phenol ammonia coal chemical industrial waste water input material volume ratio, and the progression of extraction is 8 grades;
In described step b, 20 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.07MPa, the rectifying tower top service temperature is 90 ℃, at the bottom of rectifying tower, service temperature is 140 ℃;
In described step c, distillation tower top service temperature is 60 ℃, and the base product service temperature is 130 ℃.
4. high density as claimed in claim 1 is containing the method for extracting and dephenolizing of phenol ammonia coal chemical industrial waste water, it is characterized in that: in described step a, extraction temperature is 55 ℃, extraction pH=5.0, butylacetate and high density are 1:20 containing phenol ammonia coal chemical industrial waste water input material volume ratio, and the progression of extraction is 10 grades;
In described step b, 18 grades of rectifying tower progression, reflux ratio 0.4, working pressure 0.05MPa, the rectifying tower top service temperature is 75 ℃, at the bottom of rectifying tower, service temperature is 100 ℃;
In described step c, distillation tower top service temperature is 50 ℃, and the base product service temperature is 125 ℃.
5. as the method for extracting and dephenolizing of the described high density of any one claim in claim 1-4 containing phenol ammonia coal chemical industrial waste water, it is characterized in that: the mixed structure tower that described extraction tower is packing tower or tray column or packing tower and tray column.
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| CN104276618A (en) * | 2014-10-30 | 2015-01-14 | 河南龙成煤高效技术应用有限公司 | Dephenolizing extraction agent for coal chemical wastewater and use thereof and method for dephenolizing coal chemical wastewater |
| CN104276618B (en) * | 2014-10-30 | 2015-11-18 | 河南龙成煤高效技术应用有限公司 | The dephenolization method of a kind of coal chemical industrial waste water dephenolize extraction agent and uses thereof and coal chemical industrial waste water |
| CN105668677A (en) * | 2014-11-17 | 2016-06-15 | 河南龙成煤高效技术应用有限公司 | Synergistic extracting agent for oil and phenol in waste water of coal chemical industry |
| CN105084656A (en) * | 2015-08-10 | 2015-11-25 | 蓝星（北京）技术中心有限公司 | Treatment method for industrial waste water of methionine |
| CN106865853A (en) * | 2017-02-27 | 2017-06-20 | 广东工业大学 | A kind of method for separating Phenolic Compounds From Wastewater Containing Phenols compound |
| CN107739299A (en) * | 2017-11-23 | 2018-02-27 | 魏艳娟 | The refining spearation combined dehydration method and device of mixed phenol |
| CN108793304A (en) * | 2018-07-17 | 2018-11-13 | 大唐（北京）水务工程技术有限公司 | A method of coal chemical industrial waste water containing phenol is extracted |
| CN108793304B (en) * | 2018-07-17 | 2021-07-20 | 大唐（北京）水务工程技术有限公司 | Method for extracting phenol-containing coal chemical wastewater |
| CN109776277A (en) * | 2019-02-20 | 2019-05-21 | 湘潭大学 | A method of from extraction phenolic substances in feedstock oil containing phenol |
| CN109776277B (en) * | 2019-02-20 | 2022-07-05 | 湘潭大学 | Method for extracting phenolic substances from phenol-containing raw oil |
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