CN106186146A - Methyl propyl ketone application in processing the highly concentrated phenol wastewater of Coal Chemical Industry - Google Patents
Methyl propyl ketone application in processing the highly concentrated phenol wastewater of Coal Chemical Industry Download PDFInfo
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- CN106186146A CN106186146A CN201610552057.1A CN201610552057A CN106186146A CN 106186146 A CN106186146 A CN 106186146A CN 201610552057 A CN201610552057 A CN 201610552057A CN 106186146 A CN106186146 A CN 106186146A
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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
- 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
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
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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
- C02F2303/18—Removal of treatment agents after treatment
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Abstract
The invention discloses methyl propyl ketone application in processing the highly concentrated phenol wastewater of Coal Chemical Industry.The concrete operations of described application are: extracted at 40 85 DEG C by highly concentrated to Coal Chemical Industry for methyl propyl ketone phenol wastewater, are extracted mutually and raffinate phase；The highly concentrated phenol wastewater of wherein said Coal Chemical Industry is (1 10) with the volume ratio of methyl propyl ketone: 1.Dephenolize extractant methyl propyl ketone of the present invention, it also is able to obtain the partition coefficient higher to unit phenol and polyhydric phenols under higher extraction temperature, it is thus possible to slow down the blocking of heat exchanger between deacidification deammoniation tower and extraction tower and reduce the consumption of recirculated cooling water, great prospects for commercial application.
Description
Technical field
The invention belongs to sewage treatment area, be specifically related to methyl propyl ketone in processing the highly concentrated phenol wastewater of Coal Chemical Industry
Application.
Background technology
Rich coal resources in China, reserves are big, it is achieved efficiently utilizing of coal resources is to solve current energy source shortage problem
Effective way.But during the multipath trans-utilization of coal, such as, coal gasification (very gasify in Shandong and BGL gasifies) is low
Temperature dry distilling, coking, direct or indirect liquefaction etc., it is required to use substantial amounts of washings and cooling water, then with the form of waste water
Discharge process system.Feature in the coal chemical industrial waste water produced during these is big containing substantial amounts of toxicity and the phenol of difficult degradation
Class material, including unit phenol and polyhydric phenols.
At present, the conventional process technique of Coal Chemical Industry phenol wastewater dephenolize is to utilize solvent-extracted method extraction removing waste water
Most aldehydes matters contained by.In solvent extraction process, owing to aldehydes matter dissolubility in extractant is long-range
Dissolubility in Yu Shui, thus aldehydes matter by waste water enter organic solvent mutually in, and remain in the aldehydes matter in waste water
Content is the lowest, it is possible to meet the highest phenol concentration requirement that subsequent biochemical processes.And extractant mutually in extractant and phenols
Material is then separated by rectification, obtains the extractant of crude phenols product and reusable edible.
Dephenolize extractant currently for Coal Chemical Industry phenol wastewater mainly has Di Iso Propyl Ether and hexone, this
Two kinds of extractants are the most conventional.But these extractants there is also significantly defect.If Di Iso Propyl Ether is to phenol
Class material, the especially extracting power of polyatomic phenol material are more weak；Hexone compares other extractions such as Di Iso Propyl Ether
Take agent, higher to the extraction partition coefficient of unit phenol, but its boiling point (118 DEG C) is higher, thus use this kind of extractant to process
During Coal Chemical Industry phenol wastewater, higher in the energy consumption of solvent recovery stage.Therefore, it is badly in need of a kind of low cost at present and dephenolize efficiency is high
Coal Chemical Industry phenol wastewater dephenolize extractant.
Summary of the invention
For solving the shortcoming that in prior art, dephenolize extractant energy consumption is high, the primary and foremost purpose of the present invention is to provide a kind of coal
Chemical industry highly concentrated phenol wastewater 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 Coal Chemical Industry highly concentrated phenol wastewater dephenolize extractant, methyl propyl ketone (2 pentanone), boiling point relatively low (102
DEG C), and unit phenol (phenol etc.) and polyhydric phenols (hydroquinone etc.) are all had higher removing ability, therefore select methyl-propyl
Ketone can the content of very effective reduction described Phenol for Waste Water class material as dephenolize extractant.
Methyl propyl ketone application in processing the highly concentrated phenol wastewater of Coal Chemical Industry.
Preferably, the concrete operations of described application are: by highly concentrated to Coal Chemical Industry for methyl propyl ketone phenol wastewater at 40-85
DEG C extract, be extracted mutually and raffinate phase；The highly concentrated phenol wastewater of wherein said Coal Chemical Industry and the volume of methyl propyl ketone
Than being (1-10): 1.
It is furthermore preferred that the volume ratio of the highly concentrated phenol wastewater of described Coal Chemical Industry and methyl propyl ketone is (3-10): 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 operations of described application also include: described extraction phase to be carried out in the first rectifying column rectification,
Obtaining methyl propyl ketone and crude phenols product, described methyl propyl ketone is cycled to used in the extraction highly concentrated phenol wastewater of Coal Chemical Industry；Will
Described raffinate phase carries out rectification in Second distillation column, obtains methyl propyl ketone and the dephenolize waste water of residual.
Being more highly preferred to, the operating condition of described first rectifying column includes: bottom temperature is 110-220 DEG C, and pressure is
0.1-0.2MPa, rectification theoretical stage is 5-20 level；The operating condition of described Second distillation column includes: bottom temperature is 95-110
DEG C, pressure is 0.1-0.2MPa, and rectification theoretical stage is 5-25 level.
Preferably, in the highly concentrated phenol wastewater of described Coal Chemical Industry, 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 the highly concentrated phenol wastewater of described Coal Chemical Industry is 4-8.
Preferably, 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, the highly concentrated phenol wastewater of described Coal Chemical Industry is coal gasification waste water.
Compared with prior art, the present invention has the following advantages and beneficial effect:
(1) the dephenolize extractant that the present invention provides is higher to the partition coefficient of the aldehydes matter in phenol wastewater, thus energy
Enough more efficiently remove aldehydes matter.
(2) the dephenolize extractant that the present invention provides, also is able to obtain unit phenol and polyhydric phenols under higher extraction temperature
Higher partition coefficient such that it is able to slow down the blockage problem of heat exchanger between deacidification deammoniation tower and extraction tower, reduces circulation cold
But the consumption of water, has good prospects for commercial application.
(3) the dephenolize extractant process dephenolize waste water that the present invention provides can effectively reduce energy consumption.Compared to methyl tert-butyl
Base ketone, methyl propyl ketone has lower boiling point, it means that can save more energy consumption at extractant recovery stage.
(4) as a rule, phenol wastewater, before using dephenolize extractant to extract, needs first at 105-165 DEG C
Carry out deacidification at a temperature of higher and deamination processes.And when using Di Iso Propyl Ether as dephenolize extractant, the temperature of extraction is led to
Often needing to be down to less than 50 DEG C, therefore, the cooling extent entering extraction tower needs from deacidification deammoniation tower is very big, the most not only needs
Want substantial amounts of recirculated cooling water, but also the blocking of heat exchanger between deacidification deammoniation tower and extraction tower can be aggravated.But, use this
The dephenolize extractant containing methyl propyl ketone of invention, the temperature of extraction is down to 80 DEG C and is obtained with unit phenol and polynary
The partition coefficient that phenol is higher, therefore, is possible not only to reduce the consumption of recirculated cooling water, it is also possible to slow down deacidification deammoniation tower and extraction
The blocking of heat exchanger between tower, great prospects for commercial application.
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 a kind of dephenolize extractant based on methyl propyl ketone.
Present invention also offers the application of above-mentioned dephenolize extractant: by phenol wastewater with described based on methyl propyl ketone
The dephenolize extractant of body extracts, and is extracted mutually and raffinate phase.
In the present invention, described " extraction " is to instigate the aldehydes matter in described phenol wastewater to be dissolved in dephenolize extractant, directly
Basically reaching balance to dissolving.
Dephenolize extractant of the present invention is based on methyl propyl ketone.
The application process of the dephenolize extractant that the present invention provides is applicable to the process to all phenol wastewater, such as, described
In 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 the hydrogen atom in aromatic compound on phenyl ring
Being optionally substituted by a hydroxyl group generated compound, it includes polyhydric phenols and unit phenol, i.e. containing polyhydric phenols and list in described phenol wastewater
Unit's 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
The phenolic compound of a phenolic hydroxyl group only it is bonded on phenyl ring.The example of described polyhydric phenols includes but not limited to: hydroquinone,
Benzodiazepines, catechol, 2-methyl hydroquinone, 2-methylresorcinol, 3-methyl pyrocatechol, 2,6-dimethyl are to benzene two
One or more in phenol, 2,5-dimethyl resorcinol etc..The example of described unit phenol includes but not limited to: 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, p-methyl phenol, a methylbenzene
One or more in phenol and alpha-Naphthol etc..Preferably, in described phenol wastewater, the content of described polyhydric phenols is 1000-
16000mg/L, the content of unit phenol is 1000-9000mg/L.It is highly preferred that described phenol wastewater is coal gasification waste water.
According to the present invention, the amount of the phenol wastewater that the consumption of described dephenolize extractant should process as required is fitted
Working as selection, as a rule, described phenol wastewater can be 1-10:1, preferably 3-10:1 with the volume ratio of dephenolize extractant.This
Outward, the temperature of described extraction can be 40-85 DEG C.
According to the present invention, the pH value of the phenol wastewater contacted with described dephenolize extractant is preferably smaller than 9, more preferably 4-8,
So can significantly more reduce polyhydric phenols and the content of polyhydric phenols in dephenolize waste water.But, as a rule, pending containing phenol
The pH value of waste water is usually 6-7.5, therefore, so that regulated by the pH value of the phenol wastewater contacted with described dephenolize extractant
To above-mentioned target zone, phenol wastewater that can be the most pending adds acidic materials or alkaline matter, specially ability
Known in field technique personnel, therefore not to repeat here.
The present invention mainly thes improvement is that methyl propyl ketone as the dephenolize extractant of phenol wastewater, and concrete
Extracting process can be same as the prior art or similar.Such as, described extraction is carried out in extraction tower, and the progression of extraction is excellent
Elect 2-8 level as.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, 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 application process of the dephenolize extractant that the present invention provides further preferably includes described extraction
Taking and carry out rectification in the first rectifying column, obtain dephenolize extractant and crude phenols product, described dephenolize extractant is cycled to used in extraction
Take phenol wastewater, so can utilize dephenolize extractant fully, reduce processing cost.Further, what the present invention provided is de-
The application process of phenol extraction agent further preferably includes carrying out described raffinate phase in Second distillation column rectification, obtains the dephenolize of residual
Extractant and dephenolize waste water, the dephenolize waste water so enabled to is directly used in next step biochemical treatment.
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 110-220 DEG C, be preferably 200-220 DEG C, and pressure can be
0.1-0.2MPa, preferably 0.1-0.15MPa, rectification theoretical stage can be 5-20 level, be preferably 8-20 level.Described second essence
The operating condition evaporating tower includes: bottom temperature can be 95-110 DEG C, be preferably 100-110 DEG C, and pressure can be 0.1-
0.2MPa, preferably 0.1-0.15MPa, rectification theoretical stage can be 5-25 level, be preferably 10-20 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 phenol wastewater is coal gasification waste water, total phenols in described phenol wastewater
Content is measured according to the bromination volumetric method (not carrying out the step of pre-distillation) of regulation in HJ 502-2009；Single
The content of unit's phenol is measured according to bromination volumetric method after the pre-distillation of regulation in HJ 502-2009；The content of polyhydric phenols is total
The content of phenol deducts the content of unit phenol；COD value uses the method for regulation in HJT399-2007 to be measured.
Embodiment 1
The dephenolize extractant that this embodiment provides for the present invention is described application in Phenol-Containing Wastewater Treatment, concrete operations
As follows:
By the phenol wastewater of pH=6.5, (total phenol content is 12000mg/L, and unit phenol content is 8000mg/L, and polyhydric phenols contains
Amount is 4000mg/L, and COD value is 30724mg/L), with dephenolize extractant methyl propyl ketone counter-current extraction in extraction tower, extraction
Taking theoretical stage 3 grades, dephenolize extractant is 1:6 with the volume ratio of phenol wastewater, and extraction temperature is 40 DEG C, respectively obtains containing crude phenols
With the extraction phase of a large amount of dephenolize extractants and containing a small amount of dephenolize extractant and the raffinate phase of a large amount of waste water.Extraction phase enters rectification
Tower i.e. phenol tower, rectification theoretical stage is 10 grades, and bottom temperature is 198-200 DEG C, and pressure is 0.105-0.11MPa, and tower top obtains
Dephenolize extractant recycles, and tower reactor obtains crude phenols product.Raffinate phase enters rectifying column i.e. water tower, and rectifying column theoretical stage is 15
Level, bottom temperature is 100-103 DEG C, and pressure is 0.10-0.11MPa, and tower top obtains the dephenolize extractant of residual, and tower reactor is taken off
Phenol waste water.
After testing, in gained dephenolize waste water, total phenol content is 151mg/L, and unit phenol content is 7mg/L, and polyphenol content is
144mg/L, COD value is 1639mg/L.
Embodiment 2
The dephenolize extractant that this embodiment provides for the present invention is described application in Phenol-Containing Wastewater Treatment, concrete operations
As follows:
By the phenol wastewater of pH=8, (total phenol content is 12000mg/L, and unit phenol content is 8000mg/L, polyphenol content
For 4000mg/L, COD value is 30724mg/L), and with dephenolize extractant methyl propyl ketone counter-current extraction in extraction tower, extraction
Taking theoretical stage is 8 grades, and dephenolize extractant is 1:5 with the volume of phenol wastewater, and extraction temperature is 85 DEG C, respectively obtains containing crude phenols
With the extraction phase of a large amount of dephenolize extractants and containing a small amount of dephenolize extractant and the raffinate phase of a large amount of waste water.Extraction phase enters rectification
Tower i.e. phenol tower, rectification theoretical stage is 5 grades, and bottom temperature is 210-212 DEG C, and pressure is 0.14-0.15MPa, and tower top is taken off
Phenol extraction agent recycles, and tower reactor obtains crude phenols product.Raffinate phase enters rectifying column i.e. water tower, and rectifying column theoretical stage is 25
Level, bottom temperature is 105-110 DEG C, and pressure is 0.14-0.15MPa, and tower top obtains the dephenolize extractant of residual, and tower reactor is taken off
Phenol waste water.
After testing, total phenol content 279mg/L in gained dephenolize waste water, unit phenol content is 11mg/L, the content of polyhydric phenols
For 268mg/L, COD value is 2537mg/L.
Embodiment 3
The dephenolize extractant that this embodiment provides for the present invention is described application in Phenol-Containing Wastewater Treatment, concrete operations
As follows:
By the phenol wastewater of pH=9, (total phenol content is 12000mg/L, and single content is 4000mg/L, and COD value is
30724mg/L), and with dephenolize extractant methyl propyl ketone counter-current extraction in extraction tower, extraction theory progression is 2 grades, de-
The volume of phenol extraction agent and phenol wastewater is 1:3, and extraction temperature is 40 DEG C, respectively obtains 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 198-200 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
100-103 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 411mg/L, and unit phenol content is 16mg/L, polyphenol content
For 395mg/L, COD value is 3269mg/L.
Embodiment 4
The dephenolize extractant that this embodiment provides for the present invention is described application in Phenol-Containing Wastewater Treatment, concrete operations
As follows:
By phenol wastewater, (total phenol content is 12000mg/L, and unit phenol content is 8000mg/L, and polyphenol content is
4000mg/L, COD value is 30724mg/L) pH to regulation to 6.5, and with dephenolize extractant methyl propyl ketone at extraction tower
Middle counter-current extraction, extraction theory progression is 8 grades, and dephenolize extractant is 1:8 with the volume of phenol wastewater, and extraction temperature is 60 DEG C,
Respectively obtain containing crude phenols and the extraction phase of a large amount of dephenolize extractant and contain 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 theoretical stage is 10 grades, and bottom temperature is 198-200 DEG C, and pressure is 0.105-
0.11MPa, tower top obtains dephenolize extractant and recycles, and tower reactor obtains crude phenols product.Raffinate phase enters rectifying column i.e. water tower, essence
Evaporating tower theoretical stage is 20 grades, and bottom temperature is 100-103 DEG C, and pressure is 0.10-0.11MPa, and tower top obtains the dephenolize of residual
Extractant, tower reactor obtains dephenolize waste water.
After testing, in gained dephenolize waste water, total phenol content is 166mg/L, and unit phenol content is 9mg/L, and polyphenol content is
157mg/L, COD value is 1762mg/L.
Embodiment 5
The dephenolize extractant that this embodiment provides for the present invention is described application in Phenol-Containing Wastewater Treatment, concrete operations
As follows:
By phenol wastewater, (total phenol content is 12000mg/L, and unit phenol content is 8000mg/L, and polyphenol content is
4000mg/L, COD value is 30724mg/L) pH to regulation to 6.5, and with dephenolize extractant methyl propyl ketone at extraction tower
Middle counter-current extraction, extraction theory progression is 8 grades, and dephenolize extractant is 1:8 with the volume of phenol wastewater, and extraction temperature is 70 DEG C,
Respectively obtain containing crude phenols and the extraction phase of a large amount of dephenolize extractant and contain 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 theoretical stage is 10 grades, and bottom temperature is 198-200 DEG C, and pressure is 0.105-
0.11MPa, tower top obtains dephenolize extractant and recycles, and tower reactor obtains crude phenols product.Raffinate phase enters rectifying column i.e. water tower, essence
Evaporating tower theoretical stage is 20 grades, and bottom temperature is 100-103 DEG C, and pressure is 0.10-0.11MPa, and tower top obtains the dephenolize of residual
Extractant, tower reactor obtains dephenolize waste water.
After testing, in gained dephenolize waste water, total phenol content is 268mg/L, and unit phenol content is 13mg/L, polyphenol content
For 255mg/L, COD value is 2303mg/L.
Embodiment 6
The dephenolize extractant that this embodiment provides for the present invention is described application in Phenol-Containing Wastewater Treatment, concrete operations
As follows:
Processing phenol wastewater according to the method for embodiment 1, except for the difference that, by phenol wastewater, (total phenol content is
12000mg/L, unit phenol content is 8000mg/L, and polyphenol content is 4000mg/L, and COD value is 30724mg/L) use same volume
(total phenol content is 2000mg/L to long-pending phenol wastewater, and unit phenol content is 1000mg/L, and polyphenol content is 1000mg/L, COD
It is worth and substitutes for 12500mg/L.
After testing, from water tower tower reactor dephenolize waste water out, total phenol content is 38mg/L, and unit phenol content is 1mg/L,
Polyphenol content is 37mg/L, and COD value is 385mg/L.
Embodiment 7
The dephenolize extractant that this embodiment provides for the present invention is described application in Phenol-Containing Wastewater Treatment, concrete operations
As follows:
Processing phenol wastewater according to the method for embodiment 1, except for the difference that, by phenol wastewater, (total phenol content is
12000mg/L, unit phenol content is 8000mg/L, and polyphenol content is 4000mg/L, and COD value is 30724mg/L) use same volume
Long-pending phenol wastewater (total phenol content is 25000mg/L, and unit phenol content is 9000mg/L, and polyphenol content is 16000mg/L,
COD value is 65000mg/L) substitute.
After testing, from water tower tower reactor dephenolize waste water out, total phenol content is 440mg/L, and unit phenol content is 19mg/
L, polyphenol content is 421mg/L, and COD value is 3431mg/L.
Embodiment 8
The dephenolize extractant that this embodiment provides for the present invention is described application in Phenol-Containing Wastewater Treatment, concrete operations
As follows:
According to the method for embodiment 1, described phenol wastewater is processed, except for the difference that, dephenolize extractant and phenol wastewater
Volume be 1:10.
After testing, from water tower tower reactor dephenolize waste water out, total phenol content is 281mg/L, and unit phenol content is 10mg/
L, polyphenol content is 271mg/L, and COD value is 2699mg/L.
Embodiment 9
The dephenolize extractant that this embodiment provides for the present invention is described application in Phenol-Containing Wastewater Treatment, concrete operations
As follows:
According to the method for embodiment 1, described phenol wastewater is processed, except for the difference that, by the pH value of described phenol wastewater
It is adjusted to 10.
After testing, from water tower tower reactor dephenolize waste water out, total phenol content is 851mg/L, and unit phenol content is 49mg/
L, polyphenol content is 802mg/L, and COD value is 4601mg/L.
Comparative example 1
This comparative example is for illustrating the reference processing method of phenol wastewater.
According to the method for embodiment 3, phenol wastewater is processed, except for the difference that, by methyl propyl ketone same volume
Hexone substitute.After testing, 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.
From the contrast of embodiment 3 and comparative example 1 it can be seen that extraction conditions as, embodiment 3 uses methyl-prop
Base 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 phenol wastewater of 30724mg/L processes, and result shows, total phenols from water tower tower reactor dephenolize waste water out
Content is 411mg/L, and unit phenol content is 16mg/L, and polyphenol content is 395mg/L, and COD value is 3269mg/L.And comparative example
1 uses hexone to process identical phenol wastewater as dephenolize extractant, and result shows, from water tower tower reactor
In dephenolize waste water out, total phenol content is 1339mg/L, and unit phenol content is 301mg/L, and polyphenol content is 1038mg/L,
COD value is 3784mg/L.
Visible, methyl propyl ketone shows different property in the extraction of aldehydes matter from hexone
Can, methyl propyl ketone is above hexone to the partition coefficient of unit phenol and polyhydric phenols, shows and be better than first
The effect of extracting of base isobutyl ketone.
Comparative example 2
This comparative example is for illustrating the reference processing method of phenol wastewater.
According to the method for embodiment 3, phenol wastewater is processed, except for the difference that, methyl propyl ketone same volume
Di Iso Propyl Ether 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.
Comparative example 3
This comparative example is for illustrating the reference processing method of phenol wastewater.
According to the method for embodiment 3, phenol wastewater is processed, except for the difference that, methyl propyl ketone same volume
Methyl-tert .-butyl ketone substitutes.From water tower tower reactor dephenolize waste water out, total phenol content is 829mg/L, and unit phenol content is
297mg/L, polyphenol content is 532mg/L, and COD value is 2917mg/L.
From the result of above example it can be seen that phenol wastewater can be carried out very by the method using the present invention to provide
Effectively process.From the contrast of embodiment 3 and comparative example 1-3 it can be seen that methyl propyl ketone is to unit phenol and polyhydric phenols
Partition coefficient is above hexone, Di Iso Propyl Ether and methyl-tert .-butyl ketone, shows and is substantially better than first
The effect of extracting of base isobutyl ketone, Di Iso Propyl Ether and methyl-tert .-butyl ketone, great prospects for commercial application.Additionally, from reality
Execute the contrast of example 1 and embodiment 9 it can be seen that when the pH value of described phenol wastewater is 4-8, it is possible to significantly more reduce described
Unit phenol and the content of polyhydric phenols in phenol wastewater.
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 propyl ketone application in processing the highly concentrated phenol wastewater of Coal Chemical Industry.
The methyl propyl ketone the most according to claim 1 application in processing the highly concentrated phenol wastewater of Coal Chemical Industry, its feature
Being, the concrete operations of described application are: extracted at 40-85 DEG C by highly concentrated to Coal Chemical Industry for methyl propyl ketone phenol wastewater
Take, be extracted mutually and raffinate phase；The highly concentrated phenol wastewater of wherein said Coal Chemical Industry is (1-with the volume ratio of methyl propyl ketone
10):1。
The methyl propyl ketone the most according to claim 2 application in processing the highly concentrated phenol wastewater of Coal Chemical Industry, its feature
Being, the highly concentrated phenol wastewater of described Coal Chemical Industry is (3-10) with the volume ratio of methyl propyl ketone: 1.
The methyl propyl ketone the most according to claim 2 application in processing the highly concentrated phenol wastewater of Coal Chemical Industry, its feature
Being, described extraction is carried out in the extraction tower that extraction progression is 2-8 level.
The methyl propyl ketone the most according to claim 2 application in processing the highly concentrated phenol wastewater of Coal Chemical Industry, its feature
Being, the concrete operations of described application also include: described extraction phase carries out in the first rectifying column rectification, obtains methyl-propyl
Ketone and crude phenols product, gained methyl propyl ketone is cycled to used in the extraction highly concentrated phenol wastewater of Coal Chemical Industry；Described raffinate phase is existed
Second distillation column carries out rectification, obtains methyl propyl ketone and the dephenolize waste water of residual.
The methyl propyl ketone the most according to claim 5 application in processing the highly concentrated phenol wastewater of Coal Chemical Industry, its feature
Being, the operating condition of described first rectifying column includes: bottom temperature is 110-220 DEG C, and pressure is 0.1-0.2MPa, and rectification is managed
Opinion progression is 5-20 level；The operating condition of described Second distillation column includes: bottom temperature is 95-110 DEG C, and pressure is 0.1-
0.2MPa, rectification theoretical stage is 5-25 level.
The methyl propyl ketone the most according to claim 1 application in processing the highly concentrated phenol wastewater of Coal Chemical Industry, its feature
Being, in the highly concentrated phenol wastewater of described Coal Chemical Industry, the content of total phenols is 2000-25000mg/L, and COD value is 10000-65000mg/
L, pH value is less than 9.
The methyl propyl ketone the most according to claim 7 application in processing the highly concentrated phenol wastewater of Coal Chemical Industry, its feature
Being, described total phenols includes unit phenol and polyhydric phenols, and the content of described polyhydric phenols is 1000-16000mg/L, containing of unit phenol
Amount is 1000-9000mg/L.
The methyl propyl ketone the most according to claim 1 application in processing the highly concentrated phenol wastewater of Coal Chemical Industry, its feature
Being, the pH value of the highly concentrated phenol wastewater of described Coal Chemical Industry is 4-8.
The methyl propyl ketone the most according to claim 1 application in processing the highly concentrated phenol wastewater of Coal Chemical Industry, its feature
Being, the highly concentrated phenol wastewater of described Coal Chemical Industry is coal gasification waste water.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107585820A (en) * | 2017-09-08 | 2018-01-16 | 华南理工大学 | A kind of extractant and extracting process to polyhydric phenols in phenol wastewater with high distribution coefficient |
| CN107739299A (en) * | 2017-11-23 | 2018-02-27 | 魏艳娟 | The refining spearation combined dehydration method and device of mixed phenol |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103420442A (en) * | 2013-08-09 | 2013-12-04 | 华南理工大学 | Method for extracting high-concentration phenol-containing coal chemical industry wastewater at high temperature by using methyl isobuthyl ketone |
| CN104327227A (en) * | 2014-11-18 | 2015-02-04 | 西安元创化工科技股份有限公司 | Method for synthesizing phenolic resin |
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2016
- 2016-07-12 CN CN201610552057.1A patent/CN106186146A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103420442A (en) * | 2013-08-09 | 2013-12-04 | 华南理工大学 | Method for extracting high-concentration phenol-containing coal chemical industry wastewater at high temperature by using methyl isobuthyl ketone |
| CN104327227A (en) * | 2014-11-18 | 2015-02-04 | 西安元创化工科技股份有限公司 | Method for synthesizing phenolic resin |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107585820A (en) * | 2017-09-08 | 2018-01-16 | 华南理工大学 | A kind of extractant and extracting process to polyhydric phenols in phenol wastewater with high distribution coefficient |
| CN107739299A (en) * | 2017-11-23 | 2018-02-27 | 魏艳娟 | The refining spearation combined dehydration method and device of mixed phenol |
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Application publication date: 20161207 |