CN106044916A - Application of methyl isopropyl methylketone to treatment of high-concentration phenolic wastewater - Google Patents
Application of methyl isopropyl methylketone to treatment of high-concentration phenolic wastewater Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/26—Treatment of water, waste water, or sewage by extraction
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
- C02F2101/345—Phenols
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
Abstract
The invention discloses application of methyl isopropyl methylketone to treatment of high-concentration phenolic wastewater. The application includes the particular steps that the high-concentration phenolic wastewater is extracted with methyl isopropyl methylketone at the temperature of 40-75 DEG C to obtain an extract phase and a raffinate phase, and the volume ratio of the high-concentration phenolic wastewater to a dephenolizing extraction agent is (1-10):1. Compared with an existing dephenolizing extraction agent, the dephenolizing extraction agent has high distribution coefficients to monophenol and polyphenol, can greatly reduce the content of COD and has low boiling point and solubility, energy consumption of recovering the extraction agent can be reduced, and the extraction agent is easy to recover.
Description
Technical field
The invention belongs to sewage treatment area, be specifically related to methyl isopropyl ketone answering in processing highly concentrated phenol wastewater
With.
Background technology
The highly concentrated phenol wastewater of Coal Chemical Industry typically from colm the Coal Chemical Industry processing procedure of 400-1100 DEG C, such as coal
Classification upgrading, lurgi gasifier gasification, BGL furnace gas, coal low temperature distillation, oil shale low temperature distillation.This kind of waste water generally includes coal tar
Oil, dust, sulfide, phosphate radical material, COD and aldehydes matter.The material such as coal tar and dust can be through coal gas moisture
Deviating from from technology, sulfide, carbonate material are removed through deacidification deamination, and the reduction of phenols and COD relies primarily on solvent extraction
The way taken reclaims and reduces.Wherein the concentration stage that high pollution is the heaviest is that the coal low temperature when 400-800 DEG C is done
Evaporating the stage, waste water COD may be up to 5 ten thousand to 8 ten thousand, and it is all polynary that total phenols is up to more than more than 15000mg/L, and 2/3rds
Phenol.
The dephenolize extractant that the highly concentrated phenol wastewater of Coal Chemical Industry is conventional at present is diisopropyl ether and hexone.Domestic
Many coal chemical industry enterprises still use diisopropyl ether to be extractant, mostly be lurgi gasifier field of gasification, but effect of extracting is not very
Good, water COD and total phenol content after process are the highest, and COD is generally up to 5000-8000mg/L, total phenols 500-1100mg/L,
And the heat exchanger blocking before extracting is seriously, maintenance trouble；Either lurgi gasifier produces waste water or BGL stove, or coal low temperature is done
Evaporate the waste water of generation, use hexone that COD and total phenols are all had bigger reduction, blocking is also had the most slow
Solving, the time between overhauls(TBO) is up to 8～more than 12 months, but hexone boiling point higher (116 DEG C), relative energy consumption is higher.In
In state's patent CN104129827B, methyl-tert .-butyl ketone boiling point and the recovery observable index hexone of protection also have relatively
Big improvement, but yet suffer from boiling point and reclaim the deficiency that energy consumption is higher.
Summary of the invention
Low for solving dephenolize extractant efficiency in prior art, that energy consumption is high shortcoming, the primary and foremost purpose of the present invention is to carry
For a kind of dephenolize extractant.
Another object of the present invention is to provide the application of above-mentioned dephenolize extractant.
The object of the invention is achieved through the following technical solutions:
A kind of novel dephenolize extractant, described dephenolize extractant is methyl isopropyl ketone.Described methyl isopropyl ketone
(having another name called 3-espeleton, 1,1-dimethyl acetone), unit phenol, polyhydric phenols and COD are respectively provided with higher removal ability；Boiling
Point (94.7 DEG C), than hexone and methyl-tert .-butyl ketone will be little, therefore reclaim observable index above-mentioned two and take off
Phenol extraction agent low.
The application in processing highly concentrated phenol wastewater of the above-mentioned dephenolize extractant methyl isopropyl ketone.
Described application concrete steps include: carried out at 40-75 DEG C by described highly concentrated phenol wastewater methyl isopropyl ketone
Extraction, is extracted mutually and raffinate phase；Wherein said highly concentrated phenol wastewater is (1-10) with the volume ratio of dephenolize extractant: 1.
It is furthermore preferred that described extraction is carried out in the extraction tower that extraction progression is 2-8 level.
It is furthermore preferred that the concrete steps of described application also include: described extraction phase to be carried out in the first rectifying column rectification,
Obtaining methyl isopropyl ketone and crude phenols product, gained methyl isopropyl ketone is cycled to used in the highly concentrated phenol wastewater of extraction；By institute
State raffinate phase in Second distillation column, carry out rectification, obtain methyl isopropyl ketone and the dephenolize waste water of residual.
Being more highly preferred to, the operating condition of described first rectifying column includes: bottom temperature can be 108-218 DEG C, preferably
For 198-218 DEG C, pressure can be 0.1-0.2MPa, be preferably 0.1-0.15MPa, rectification theoretical stage can be 5-18 level,
It is preferably 8-18 level.The operating condition of described Second distillation column includes: bottom temperature can be 92-108 DEG C, be preferably 98-106
DEG C, pressure can be 0.1-0.2MPa, be preferably 0.1-0.15MPa, and rectification theoretical stage can be 5-22 level, be preferably 10-
19 grades.
In described highly concentrated phenol wastewater, total phenol content is not less than 2000mg/L.
Preferably, in described highly concentrated phenol wastewater, the content of total phenols is 2000-25000mg/L, and COD value is 10000-
65000mg/L, pH value is less than 9.
It is furthermore preferred that the pH value of described highly concentrated phenol wastewater is 4-8.
It is furthermore preferred that described total phenols includes unit phenol and polyhydric phenols, and the content of described polyhydric phenols is 1000-16000mg/
L, the content of unit phenol is 1000-9000mg/L.
Preferably, described highly concentrated phenol wastewater is the highly concentrated phenol wastewater of Coal Chemical Industry.
Compared with prior art, the present invention has the following advantages and beneficial effect:
(1) methyl isopropyl ketone boiling point 94.7 DEG C, azeotrope with water point 78-79 DEG C, the most moderate, is especially suitable for phenol recovery ammonia
Extraction cells in system.Ethers normally boiling is on the low side, and hexone and methyl-tert .-butyl ketone boiling point are higher.
(2) in methyl isopropyl ketone extraction phase rectification recycling design, tower top bottom temperature difference is bigger, is more easy to reclaim, loss
Less.Compared to hexone, methyl-tert .-butyl ketone has less dissolubility, and azeotrope with water forms relative to first
Base isobutyl ketone, methyl-tert .-butyl ketone have lower water content, and therefore, the raffinate phase after extracting and dephenolizing is in solvent recovery
When go out less water at water tower tower top azeotropic distillation, the energy consumption of water tower also can be substantially reduced,
(3) methyl isopropyl ketone molecular weight ratio hexone and methyl-tert .-butyl ketone are little, it is meant that identical
The methyl isopropyl ketone molecular number of volume or quality is more, it is easier to the aldehydes matter in capture extraction wastewater.
(4) methyl isopropyl ketone is verified by experiments the effect of extracting to unit phenol Yu polyhydric phenols and is superior to existing methyl
Isobutyl ketone and methyl-tert .-butyl ketone.
Detailed description of the invention
Below in conjunction with embodiment, the present invention is described in further detail, but embodiments of the present invention are not limited to this.
The invention provides the dephenolize extractant of a kind of methyl isopropyl ketone.
Present invention also offers the application of above-mentioned dephenolize extractant, described application concrete steps include: highly concentrated contain described
Phenol waste water methyl isopropyl ketone extracts at 40-75 DEG C, is extracted mutually and raffinate phase；Wherein said phenol wastewater
It is (1-10) with the volume ratio of dephenolize extractant: 1.In described highly concentrated phenol wastewater, total phenol content is not less than 2000mg/L.
In the present invention, described " extraction " is to instigate the aldehydes matter in described highly concentrated phenol wastewater to be dissolved in dephenolize extraction
Agent, basically reaches balance until dissolving.
The application process of dephenolize extractant that the present invention provides is applicable to the process to all highly concentrated phenol wastewater, such as,
In described highly concentrated phenol wastewater, the content of total phenols can be 2000-25000mg/L, and COD value can be 10000-65000mg/L.
Wherein, described total phenol content refers to the total content of phenolic compound.Described phenolic compound refers to phenyl ring in aromatic compound
On hydrogen atom be optionally substituted by a hydroxyl group generated compound, it includes polyhydric phenols and unit phenol, i.e. contain in described phenol wastewater
Polyhydric phenols and unit phenol.Wherein, described polyhydric phenols refers to be bonded on phenyl ring the phenolic compound of two or more phenolic hydroxyl group；Described
Unit phenol refers to only be bonded on phenyl ring the phenolic compound of a phenolic hydroxyl group.The example of described polyhydric phenols includes but not limited to:
Hydroquinone, resorcinol, catechol, 2-methyl hydroquinone, 2-methylresorcinol, 3-methyl pyrocatechol, 2,6-
One or more in dimethyl hydroquinone, 2,5-dimethyl resorcinol etc..The example of described unit phenol includes but does not limits
In: phenol, 2,5-xylenol, 2,4-xylenol, 2-acrylic phenol, 3-ethyl-5-methylphenol, 2-ethyl-
5-methylphenol, 3,5-xylenol, ortho-methyl phenol, 2-ethyl-phenol, 3-ethyl-phenol, 4-ethyl-phenol, to methyl
One or more in phenol, m-methyl phenol and alpha-Naphthol etc..Preferably, in described highly concentrated phenol wastewater, described many
The content of unit's phenol is 1000-16000mg/L, and the content of unit phenol is 1000-9000mg/L.It is highly preferred that it is described highly concentrated containing phenol
Waste water is the highly concentrated phenol wastewater of Coal Chemical Industry.
According to the present invention, the amount of the highly concentrated phenol wastewater that the consumption of described dephenolize extractant should process as required is entered
Row suitably selects, and as a rule, described highly concentrated phenol wastewater can be 1-10:1 with the volume ratio of dephenolize extractant.Additionally, institute
The temperature stating extraction can be 40-75 DEG C.
According to the present invention, the pH value of the highly concentrated phenol wastewater contacted with described dephenolize extractant is preferably smaller than 9, more preferably
4-8, so can significantly more reduce unit phenol and the content of polyhydric phenols in highly concentrated phenol wastewater.But, as a rule, wait to locate
The pH value of the highly concentrated phenol wastewater of reason is usually 6-7.5, therefore, so that will give up containing phenol with what described dephenolize extractant contacted
In the pH value regulation extremely above-mentioned target zone of water, highly concentrated phenol wastewater that can be the most pending adds acidic materials or alkalescence
Material, the most as well known to those skilled in the art, therefore not to repeat here.
According to the present invention, containing crude phenols and a large amount of dephenolize extractant in described extraction phase, and containing a small amount of in described raffinate phase
Dephenolize extractant and substantial amounts of dephenolize waste water.The processing method of the highly concentrated phenol wastewater that the present invention provides further preferably includes described
Extraction phase carries out rectification, obtains dephenolize extractant and crude phenols product, and it is highly concentrated useless containing phenol that described dephenolize extractant is cycled to used in extraction
Water, so can utilize dephenolize extractant fully, reduces processing cost.Further, what the present invention provided is highly concentrated useless containing phenol
The processing method of water further preferably includes described raffinate phase is carried out rectification, obtains dephenolize extractant and the dephenolize sewage of residual,
The dephenolize sewage so enabled to is directly used in next step biochemical treatment.Described extraction phase and raffinate phase are carried out rectification
Method and condition be known to the skilled person, will not repeat at this.
Additionally, the present invention's mainly thes improvement is that providing a kind of new extractant takes off highly concentrated phenol wastewater
Phenol processes, and after removing aldehydes matter, also typically requires and described dephenolize waste water is carried out biochemical treatment, such as anaerobic bio-treated
And/or Aerobic biological process.Described anaerobic bio-treated and Aerobic biological process all can use and well known to a person skilled in the art
Method is carried out, and will not repeat at this.
The present invention mainly thes improvement is that methyl isopropyl ketone as the dephenolize extractant of phenol wastewater, and has
The extracting process of body can be same as the prior art or similar.Such as, described extraction is carried out in extraction tower, and the progression of extraction
It is preferably 2-8 level.The kind of extraction tower used and structure can be all the conventional selection of this area, and therefore not to repeat here.
According to the present invention, from being easy to the angle that describes, the rectifying column that described extraction phase carries out rectification is referred to as " the
One rectifying column ", the rectifying column that described raffinate phase carries out rectification is referred to as " Second distillation column ".The kind of described rectifying column and knot
Structure is known to the skilled person, and will not repeat at this.
The operating condition of described first rectifying column and Second distillation column is all not particularly limited by the present invention, such as, and institute
The operating condition stating the first rectifying column includes: bottom temperature can be 108-218 DEG C, be preferably 198-218 DEG C, and pressure can be
0.1-0.2MPa, preferably 0.1-0.15MPa, rectification theoretical stage can be 5-18 level, be preferably 8-18 level.Described second essence
The operating condition evaporating tower includes: bottom temperature can be 92-108 DEG C, be preferably 98-106 DEG C, and pressure can be 0.1-
0.2MPa, preferably 0.1-0.15MPa, rectification theoretical stage can be 5-22 level, be preferably 10-19 level.
In the present invention, described pressure refers both to absolute pressure.
Hereinafter will be described the present invention by embodiment.
In following example and comparative example, described highly concentrated phenol wastewater is the highly concentrated phenol wastewater of Coal Chemical Industry, described highly concentrated
The content of Phenol all uses gas chromatographic analysis.
Embodiment 1
The dephenolize extractant that this embodiment provides for the present invention is described application in processing highly concentrated phenol wastewater, specifically
Operate as follows:
By highly concentrated phenol wastewater (the total phenols 18000mg/L, volatile phenol 12000mg/L, polyphenol content 6000mg/ of pH=7
L, COD value is 46086mg/L), with dephenolize extractant (methyl isopropyl ketone) counter-current extraction in extraction tower, extraction theory level
Number is 8 grades, and extractant and wastewater volume than for 1:3, extraction temperature 40 DEG C, respectively obtain containing crude phenols and a large amount of dephenolize extractant
Extraction phase and containing a small amount of dephenolize extractant and the raffinate phase of a large amount of waste water.Extraction phase enters rectifying column i.e. phenol tower, and rectification is theoretical
Progression is 13 grades, and bottom temperature is 210-212 DEG C, and pressure is 0.105-0.11MPa, and tower top obtains dephenolize extractant circulation profit
With, tower reactor obtains crude phenols product.Raffinate phase enters rectifying column i.e. water tower, and rectifying column theoretical stage is 19 grades, and bottom temperature is 98-
101 DEG C, pressure is 0.10-0.11MPa, and tower top obtains the dephenolize extractant of residual, and tower reactor obtains dephenolize waste water.
After testing, in gained dephenolize waste water, total phenol content is 213mg/L, and unit phenol content is 44mg/L, polyphenol content
For 169mg/L, COD value is 1783mg/L.
Embodiment 2
The dephenolize extractant that this embodiment provides for the present invention is described application in processing highly concentrated phenol wastewater, specifically
Operate as follows:
By highly concentrated phenol wastewater (the total phenols 18000mg/L, volatile phenol 12000mg/L, polyphenol content 6000mg/ of pH=4
L, COD value is 46086mg/L), with dephenolize extractant (methyl isopropyl ketone) counter-current extraction in extraction tower, extraction theory level
Number is 8 grades, and extractant and wastewater volume than for 1:3, extraction temperature 40 DEG C, respectively obtain containing crude phenols and a large amount of dephenolize extractant
Extraction phase and containing a small amount of dephenolize extractant and the raffinate phase of a large amount of waste water.Extraction phase enters rectifying column i.e. phenol tower, and rectification is theoretical
Progression is 13 grades, and bottom temperature is 210-212 DEG C, and pressure is 0.105-0.11MPa, and tower top obtains dephenolize extractant circulation profit
With, tower reactor obtains crude phenols product.Raffinate phase enters rectifying column i.e. water tower, and rectifying column theoretical stage is 19 grades, and bottom temperature is 98-
101 DEG C, pressure is 0.10-0.11MPa, and tower top obtains the dephenolize extractant of residual, and tower reactor obtains dephenolize waste water.
After testing, in gained dephenolize waste water, total phenol content is 591mg/L, and unit phenol content is 137mg/L, polyphenol content
For 304mg/L, COD value is 3435mg/L.
Embodiment 3
The dephenolize extractant that this embodiment provides for the present invention is described application in processing highly concentrated phenol wastewater, specifically
Operate as follows:
By highly concentrated phenol wastewater (the total phenols 12000mg/L, volatile phenol 8000mg/L, polyphenol content 4000mg/ of pH=9
L, COD value is 30724mg/L), with dephenolize extractant (methyl isopropyl ketone) counter-current extraction in extraction tower, extraction theory level
Number is 2 grades, and extractant and wastewater volume than for 1:3, extraction temperature 40 DEG C, respectively obtain containing crude phenols and a large amount of dephenolize extractant
Extraction phase and containing a small amount of dephenolize extractant and the raffinate phase of a large amount of waste water.Extraction phase enters rectifying column i.e. phenol tower, and rectification is theoretical
Progression is 15 grades, and bottom temperature is 211-213 DEG C, and pressure is 0.105-0.11MPa, and tower top obtains dephenolize extractant circulation profit
With, tower reactor obtains crude phenols product.Raffinate phase enters rectifying column i.e. water tower, and rectifying column theoretical stage is 10 grades, and bottom temperature is
100-1103 DEG C, pressure is 0.1-0.11MPa, and tower top obtains the dephenolize extractant of residual, and tower reactor obtains dephenolize waste water.
After testing, in gained dephenolize waste water, total phenol content is 713mg/L, and unit phenol content is 232mg/L, polyphenol content
For 481mg/L, COD value is 2454mg/L.
Embodiment 4
The dephenolize extractant that this embodiment provides for the present invention is described application in processing highly concentrated phenol wastewater, specifically
Operate as follows:
By highly concentrated phenol wastewater (the total phenols 18000mg/L, volatile phenol 12000mg/L, polyphenol content 6000mg/ of pH=7
L, COD value is 46086mg/L), with dephenolize extractant (methyl isopropyl ketone) counter-current extraction in extraction tower, extraction theory level
Number is 8 grades, and extractant and wastewater volume than for 1:1, extraction temperature 40 DEG C, respectively obtain containing crude phenols and a large amount of dephenolize extractant
Extraction phase and containing a small amount of dephenolize extractant and the raffinate phase of a large amount of waste water.Extraction phase enters rectifying column i.e. phenol tower, and rectification is theoretical
Progression is 13 grades, and bottom temperature is 210-212 DEG C, and pressure is 0.105-0.11MPa, and tower top obtains dephenolize extractant circulation profit
With, tower reactor obtains crude phenols product.Raffinate phase enters rectifying column i.e. water tower, and rectifying column theoretical stage is 19 grades, and bottom temperature is 98-
101 DEG C, pressure is 0.10-0.11MPa, and tower top obtains the dephenolize extractant of residual, and tower reactor obtains dephenolize waste water.
After testing, in gained dephenolize waste water, total phenol content is 100mg/L, and unit phenol content is 27mg/L, polyphenol content
For 73mg/L, COD value is 3843mg/L.
Embodiment 5
The dephenolize extractant that this embodiment provides for the present invention is described application in processing highly concentrated phenol wastewater, specifically
Operate as follows:
By highly concentrated phenol wastewater (the total phenols 18000mg/L, volatile phenol 12000mg/L, polyphenol content 6000mg/ of pH=7
L, COD value is 46086mg/L), with dephenolize extractant (methyl isopropyl ketone) counter-current extraction in extraction tower, extraction theory level
Number is 8 grades, and extractant and wastewater volume, than for 1:10, extraction temperature 40 DEG C, respectively obtain containing crude phenols and a large amount of dephenolize extractant
Extraction phase and containing a small amount of dephenolize extractant and the raffinate phase of a large amount of waste water.Extraction phase enters rectifying column i.e. phenol tower, and rectification is managed
Opinion progression is 18 grades, and bottom temperature is 210-212 DEG C, and pressure is 0.105-0.11MPa, and tower top obtains dephenolize extractant circulation profit
With, tower reactor obtains crude phenols product.Raffinate phase enters rectifying column i.e. water tower, and rectifying column theoretical stage is 19 grades, and bottom temperature is 98-
101 DEG C, pressure is 0.10-0.11MPa, and tower top obtains the dephenolize extractant of residual, and tower reactor obtains dephenolize waste water.
After testing, in gained dephenolize waste water, total phenol content is 459mg/L, and unit phenol content is 38mg/L, polyphenol content
For 421mg/L, COD value is 3501mg/L.
Embodiment 6
The dephenolize extractant that this embodiment provides for the present invention is described application in processing highly concentrated phenol wastewater, specifically
Operate as follows:
By highly concentrated phenol wastewater (the total phenols 18000mg/L, volatile phenol 12000mg/L, polyphenol content 6000mg/ of pH=7
L, COD value is 46086mg/L), with dephenolize extractant (methyl isopropyl ketone) counter-current extraction in extraction tower, extraction theory level
Number is 5 grades, and extractant and wastewater volume than for 1:3, extraction temperature 60 DEG C, respectively obtain containing crude phenols and a large amount of dephenolize extractant
Extraction phase and containing a small amount of dephenolize extractant and the raffinate phase of a large amount of waste water.Extraction phase enters rectifying column i.e. phenol tower, and rectification is theoretical
Progression is 18 grades, and bottom temperature is 210-212 DEG C, and pressure is 0.15-0.11MPa, and tower top obtains dephenolize extractant and recycles,
Tower reactor obtains crude phenols product.Raffinate phase enters rectifying column i.e. water tower, and rectifying column theoretical stage is 15 grades, and bottom temperature is 98-101
DEG C, pressure is 0.10-0.11MPa, and tower top obtains the dephenolize extractant of residual, and tower reactor obtains dephenolize waste water.
After testing, in gained dephenolize waste water, total phenol content is 317mg/L, and unit phenol content is 54mg/L, polyphenol content
For 263mg/L, COD value is 2461mg/L.
Embodiment 7
The dephenolize extractant that this embodiment provides for the present invention is described application in processing highly concentrated phenol wastewater, specifically
Operate as follows:
By highly concentrated phenol wastewater (the total phenols 18000mg/L, volatile phenol 12000mg/L, polyphenol content 6000mg/ of pH=7
L, COD value is 46086mg/L), with dephenolize extractant (methyl isopropyl ketone) counter-current extraction in extraction tower, extraction theory level
Number is 5 grades, and extractant and wastewater volume than for 1:3, extraction temperature 70 DEG C, respectively obtain containing crude phenols and a large amount of dephenolize extractant
Extraction phase and containing a small amount of dephenolize extractant and the raffinate phase of a large amount of waste water.Extraction phase enters rectifying column i.e. phenol tower, and rectification is theoretical
Progression is 10 grades, and bottom temperature is 216-218 DEG C, and pressure is 0.14-0.15MPa, and tower top obtains dephenolize extractant and recycles,
Tower reactor obtains crude phenols product.Raffinate phase enters rectifying column i.e. water tower, and rectifying column theoretical stage is 15 grades, and bottom temperature is 101-
106 DEG C, pressure is 0.14-0.15MPa, and tower top obtains the dephenolize extractant of residual, and tower reactor obtains dephenolize waste water.
After testing, in gained dephenolize waste water, total phenol content is 380mg/L, and unit phenol content is 78mg/L, polyphenol content
For 302mg/L, COD value is 2295mg/L.
Embodiment 8
The dephenolize extractant that this embodiment provides for the present invention is described application in processing highly concentrated phenol wastewater, specifically
Operate as follows:
According to the method for embodiment 1, highly concentrated phenol wastewater is processed, except for the difference that, by highly concentrated phenol wastewater (total phenols
18000mg/L, volatile phenol 12000mg/L, polyphenol content 6000mg/L, COD value is 46086mg/L) with the height of same volume
(total phenol content is 2000mg/L to dense phenol wastewater, and unit phenol content is 1000mg/L, and polyphenol content is 1000mg/L, COD value
Substitute for 12500mg/L.
After testing, from water tower tower reactor dephenolize waste water out, total phenol content is 87mg/L, and unit phenol content is 23mg/L,
Polyphenol content is 64mg/L, and COD value is 1324mg/L.
Embodiment 9
The dephenolize extractant that this embodiment provides for the present invention is described application in processing highly concentrated phenol wastewater, specifically
Operate as follows:
According to the method for embodiment 1, highly concentrated phenol wastewater is processed, except for the difference that, by highly concentrated phenol wastewater (total phenols
18000mg/L, volatile phenol 12000mg/L, polyphenol content 6000mg/L, COD value is 46086mg/L) with the height of same volume
(total phenol content is 25000mg/L to dense phenol wastewater, and unit phenol content is 9000mg/L, and polyphenol content is 16000mg/L, COD
It is worth and substitutes for 65000mg/L.
After testing, from water tower tower reactor dephenolize waste water out, total phenol content is 653mg/L, and unit phenol content is 141mg/
L, polyphenol content is 512mg/L, and COD value is 3987mg/L.
Comparative example 1
This comparative example is for illustrating the reference processing method of highly concentrated phenol wastewater.
According to the method for embodiment 3, highly concentrated phenol wastewater is processed, except for the difference that, by methyl isopropyl ketone phase
The methyl-tert .-butyl ketone of same volume substitutes.After testing, from water tower tower reactor dephenolize waste water out, total phenol content is 829mg/
L, unit phenol content is 297mg/L, and polyphenol content is 532mg/L, and COD value is 2917mg/L.
From the contrast of embodiment 3 and comparative example 1 it can be seen that extraction conditions as, embodiment 3 uses methyl different
Propyl ketone is 12000mg/L as dephenolize extractant to total phenol content, unit phenol content is 8000mg/L, polyhydric phenols
4000mg/L, COD value are that the highly concentrated phenol wastewater of 30724mg/L processes, and result shows, from the dephenolize out of water tower tower reactor
In waste water, total phenol content is 713mg/L, and unit phenol content is 232mg/L, and polyphenol content is 481mg/L, and COD value is
2454mg/L.Visible, methyl isopropyl ketone shows different from methyl-tert .-butyl ketone in the extraction of aldehydes matter
Performance, methyl isopropyl ketone is above methyl-tert .-butyl ketone to the partition coefficient of unit phenol and polyhydric phenols, shows excellent
Effect of extracting in methyl-tert .-butyl ketone.
Comparative example 2
This comparative example is for illustrating the reference processing method of highly concentrated phenol wastewater.
Processing highly concentrated phenol wastewater according to the method for embodiment 3, except for the difference that, methyl isopropyl ketone is with identical
The hexone of volume substitutes.From water tower tower reactor dephenolize waste water out, total phenol content is 1339mg/L, unit phenol
Content is 301mg/L, and polyphenol content is 1038mg/L, and COD value is 3784mg/L.Visible, methyl isopropyl ketone and methyl
Isobutyl ketone shows different performances in the extraction of aldehydes matter, and methyl isopropyl ketone is to unit phenol and polyhydric phenols
Partition coefficient be above hexone, show the effect of extracting being better than hexone.
Comparative example 3
This comparative example is for illustrating the reference processing method of highly concentrated phenol wastewater.
Processing highly concentrated phenol wastewater according to the method for embodiment 3, except for the difference that, methyl isopropyl ketone is with identical
The diisopropyl ether of volume substitutes.From water tower tower reactor dephenolize waste water out, total phenol content is 2258mg/L, and unit phenol content is
334mg/L, polyphenol content is 1924mg/L, and COD value is 10680mg/L.Visible, methyl isopropyl ketone and diisopropyl ether exist
Showing different performances in the extraction of aldehydes matter, methyl isopropyl ketone is equal to the partition coefficient of unit phenol and polyhydric phenols
Higher than diisopropyl ether, show the effect of extracting being better than diisopropyl ether.
From the result of above example it can be seen that the dephenolize extractant using the present invention to provide can give up containing phenol to highly concentrated
Water effectively processes.From the contrast of embodiment 3 and comparative example 1-3 it can be seen that methyl isopropyl ketone is to unit
The partition coefficient of phenol and polyhydric phenols is above methyl-tert .-butyl ketone, hexone and Di Iso Propyl Ether, shows
It is substantially better than the effect of extracting of methyl-tert .-butyl ketone, hexone and Di Iso Propyl Ether, great prospects for commercial application.
Above-described embodiment is the present invention preferably embodiment, but embodiments of the present invention are not by above-described embodiment
Limit, the change made under other any spirit without departing from the present invention and principle, modify, substitute, combine, simplify,
All should be the substitute mode of equivalence, within being included in protection scope of the present invention.
Claims (10)
1. methyl isopropyl ketone application in processing highly concentrated phenol wastewater.
The methyl isopropyl ketone the most according to claim 1 application in processing highly concentrated phenol wastewater, it is characterised in that
Described application concrete steps include: extracted at 40-75 DEG C by described highly concentrated phenol wastewater methyl isopropyl ketone, obtain
Extraction phase and raffinate phase；Wherein said highly concentrated phenol wastewater is (1-10) with the volume ratio of dephenolize extractant: 1.
The methyl isopropyl ketone the most according to claim 2 application in processing highly concentrated phenol wastewater, it is characterised in that
Described extraction is carried out in the extraction tower that extraction progression is 2-8 level.
The methyl isopropyl ketone the most according to claim 2 application in processing highly concentrated phenol wastewater, it is characterised in that
The concrete steps of described application also include: described extraction phase carries out in the first rectifying column rectification, obtains isopropyl methyl first
Ketone and crude phenols product, gained methyl isopropyl ketone is cycled to used in the highly concentrated phenol wastewater of extraction；By described raffinate phase in the second essence
Evaporate and tower carries out rectification, obtain methyl isopropyl ketone and the dephenolize waste water of residual.
The methyl isopropyl ketone the most according to claim 4 application in processing highly concentrated phenol wastewater, it is characterised in that
The operating condition of described first rectifying column includes: bottom temperature is 108-218 DEG C, and pressure is 0.1-0.2MPa, rectification theoretical stage
Number is 5-18 level；The operating condition of described Second distillation column includes: bottom temperature is 92-108 DEG C, and pressure is 0.1-0.2MPa,
Rectification theoretical stage is 5-22 level.
The methyl isopropyl ketone the most according to claim 4 application in processing highly concentrated phenol wastewater, it is characterised in that
The operating condition of described first rectifying column includes: bottom temperature is 198-218 DEG C, and pressure is 0.1-0.15MPa, rectification theoretical stage
Number is 8-18 level；The operating condition of described Second distillation column includes: bottom temperature can be 98-106 DEG C, and pressure is 0.1-
0.15MPa, rectification theoretical stage is 10-19 level.
The methyl isopropyl ketone the most according to claim 1 application in processing highly concentrated phenol wastewater, it is characterised in that
In described highly concentrated phenol wastewater, total phenol content is not less than 2000mg/L.
The methyl isopropyl ketone the most according to claim 1 application in processing highly concentrated phenol wastewater, it is characterised in that
In described highly concentrated phenol wastewater, the content of total phenols is 2000-25000mg/L, and COD value is 10000-65000mg/L, pH value be 9 with
Under.
The methyl isopropyl ketone the most according to claim 8 application in processing highly concentrated phenol wastewater, it is characterised in that
Described total phenols includes unit phenol and polyhydric phenols, and the content of described polyhydric phenols is 1000-16000mg/L, and the content of unit phenol is
1000-9000mg/L。
The methyl isopropyl ketone the most according to claim 1 application in processing highly concentrated phenol wastewater, its feature exists
In, described highly concentrated phenol wastewater is the highly concentrated phenol wastewater of Coal Chemical Industry.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107739299A (en) * | 2017-11-23 | 2018-02-27 | 魏艳娟 | The refining spearation combined dehydration method and device of mixed phenol |
| CN111547913A (en) * | 2019-12-16 | 2020-08-18 | 昆山美淼环保科技有限公司 | Method for recovering phenol from phenol-containing wastewater |
| CN115196810A (en) * | 2022-08-16 | 2022-10-18 | 华电水务工程有限公司 | Method for extracting and dephenolizing phenolic wastewater |
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| CN1919818A (en) * | 2006-09-18 | 2007-02-28 | 清华大学 | Method of recovery phenol from waste water and system thereof |
| CN105712427A (en) * | 2016-04-05 | 2016-06-29 | 华南理工大学 | Extracting agent with high partition coefficient for polyphenol in phenol wastewater and extracting method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1919818A (en) * | 2006-09-18 | 2007-02-28 | 清华大学 | Method of recovery phenol from waste water and system thereof |
| CN105712427A (en) * | 2016-04-05 | 2016-06-29 | 华南理工大学 | Extracting agent with high partition coefficient for polyphenol in phenol wastewater and extracting method |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107739299A (en) * | 2017-11-23 | 2018-02-27 | 魏艳娟 | The refining spearation combined dehydration method and device of mixed phenol |
| CN111547913A (en) * | 2019-12-16 | 2020-08-18 | 昆山美淼环保科技有限公司 | Method for recovering phenol from phenol-containing wastewater |
| CN115196810A (en) * | 2022-08-16 | 2022-10-18 | 华电水务工程有限公司 | Method for extracting and dephenolizing phenolic wastewater |
| CN115196810B (en) * | 2022-08-16 | 2024-02-13 | 华电水务工程有限公司 | Method for extracting and dephenolizing phenol-containing wastewater |
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