CN104556539B - A kind of nitrile rubber produces the processing method of waste water - Google Patents
A kind of nitrile rubber produces the processing method of waste water 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
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
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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
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
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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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
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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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
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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
- C02F2101/38—Organic compounds containing nitrogen
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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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/38—Polymers
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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
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
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Abstract
The invention discloses a kind of nitrile rubber and produce the processing method of waste water, the method comprises the following steps: a, nitrile rubber produces waste water mix with sulphite, so that the material of the difficult volatilization of acrylonitrile conversion in nitrile rubber production waste water；B, make to carry out advanced oxidation solid-liquid separation with the mixed waste water of sulphite；C, by step b separate obtain liquid phase mix with activated sludge.In water after being processed by the inventive method, acrylonitrile content is low, < < 5mg/L, effluent quality is higher, obvious processing effect for 50mg/L and ammonia-nitrogen content for COD value.And, the inventive method can be effectively prevented acrylonitrile and be overflowed by waste water in processing procedure, it is to avoid its pollution to air.
Description
Technical field
The invention belongs to field of industrial waste water treatment, relate to a kind of nitrile rubber and produce the processing method of waste water.
Background technology
Due to function admirable, being widely used, the demand of nitrile rubber and volume of production constantly rise in recent years, and the thing followed is the process problem producing waste water in a large number.Acrylonitrile (AN) is the important monomer that nitrile rubber produces, although through MONOMER RECOVERY, but produces in waste water at nitrile rubber and still have residual.Acrylonitrile is organic cyanogen of a kind of colourless, Semen Armeniacae Amarum taste, is number four, has high toxicity and potential genetoxic in the toxic chemical list of the 52 kinds of priority acccess control determined in China, is one of noxious pollutant important in environment.Additionally, acrylonitrile is also easy to volatilization, U.S. EPA specify acrylonitrile in the Organic substance list of priority acccess control be listed in can the Organic substance of stripping, it is easily caused air pollution by effusion in waste water in wastewater treatment process.But existing nitrile rubber produces in the treatment technology of waste water and does not all take any prophylactico-therapeutic measures for the stripping of acrylonitrile.
CN102874913A discloses the processing method of a kind of high-concentration acrylonitrile wastewater, adopts reduction liquid medicine that the acrylonitrile in high-concentration acrylonitrile wastewater carries out reduction and removes, and its reduction medicament adopts sodium sulfite.But, sodium sulfite with the carbon-carbon double bond generation additive reaction in acrylonitrile, can only can not destroy cyano group, simply makes acrylonitrile to be detected, and can not really change its toxicity, and waste water is not really processed.
Additionally, nitrile rubber produces in waste water possibly together with big weight oligomers and various auxiliary agent, complicated component and be difficult to degrade.Mostly existing processing method is that also having some technology is process certain composition in this waste water targetedly by itself and other waste water mixed processing.There is presently no and nitrile rubber can be produced the waste water individual processing a whole set of technology to qualified discharge.
Summary of the invention
It is an object of the invention to overcome the deficiencies in the prior art, it is provided that the nitrile rubber of a kind of acrylonitrile content, COD value and ammonia-nitrogen content that can effectively reduce in nitrile rubber production waste water produces the processing method of waste water.
To achieve these goals, the present invention provides a kind of nitrile rubber to produce the processing method of waste water, and wherein, the method comprises the following steps:
A, nitrile rubber is produced waste water mix with sulphite, so that nitrile rubber produces the material of the difficult volatilization of acrylonitrile conversion in waste water；
B, make to carry out advanced oxidation solid-liquid separation with the mixed waste water of sulphite；
C, by step b separate obtain liquid phase mix with activated sludge.
In water after being processed by the inventive method substantially without acrylonitrile residue, COD value < 50mg/L(oligomer is low) and ammonia-nitrogen content < 5mg/L, effluent quality is higher, obvious processing effect.And, the inventive method can be effectively prevented acrylonitrile and be overflowed by waste water in processing procedure, it is to avoid its pollution to air.
Other features and advantages of the present invention will be described in detail in detailed description of the invention part subsequently.
Detailed description of the invention
Hereinafter the specific embodiment of the present invention is described in detail.It should be appreciated that detailed description of the invention described herein is merely to illustrate and explains the present invention, it is not limited to the present invention.
In the present invention, when not making contrary explanation, the amount of the activated sludge related in the present invention is all in the butt of activated sludge.
Nitrile rubber provided by the invention produces the processing method of waste water and comprises the following steps:
A, nitrile rubber is produced waste water mix with sulphite, so that nitrile rubber produces the material of the difficult volatilization of acrylonitrile conversion in waste water；
B, make to carry out advanced oxidation solid-liquid separation with the mixed waste water of sulphite；
C, by step b separate obtain liquid phase mix with activated sludge.
According to the present invention, kind and the not special requirement of consumption to described sulphite, as long as nitrile rubber can be made to produce the material of the difficult volatilization of acrylonitrile conversion in waste water, under preferable case, it is 1-5:1 that the weight of the sulphite of use and nitrile rubber produce the ratio of the weight of acrylonitrile in waste water.
Preferably, described sulphite is the salt that can make α in acrylonitrile, β-unsaturated bond generation additive reaction, thus promoting the material (material that namely dissolubility strengthens in water) of the difficult volatilization of acrylonitrile conversion.Therefore, described sulphite is preferably the alkali metal salt (include normal salt and acid salt, and can also be able to be anhydride for hydrate) of sulfurous acid, more preferably at least one in sodium sulfite, potassium sulfite, sodium sulfite and Potassium acid sulfite.
According to the present invention, in step a, the condition of the material of the difficult volatilization of acrylonitrile conversion is made to preferably include: the time of mixing is 10-30min.Step a can carry out under conventional wastewater processing temperatures, for instance, the temperature of mixing can be 0-80 DEG C.
According to the present invention, advanced oxidation refers to the process that the pollutant in sewage are undertaken oxidative degradation by producing hydroxyl radical free radical.Make with the mixed waste water of sulphite carry out advanced oxidation method can be various routines advanced oxidization method.
Preferably, the method for described advanced oxidation is Fenton oxidation method.The weight of the reagent that Fenton oxidation uses and nitrile rubber produce the ratio of the weight of acrylonitrile in waste water and are preferably 0.5-3:1.
The reagent that Fenton oxidation uses can be hydrogen peroxide and ferrous sulfate.Wherein, hydrogen peroxide and the weight ratio of ferrous sulfate can be conventional selection, it is preferable that in situation, the weight ratio of hydrogen peroxide and ferrous sulfate is 2-6:1, and the weight of ferrous sulfate is in iron ion.
In preferred embodiment of the invention mode, the condition of Fenton oxidation in step b do not had special restriction, it is preferable that the condition of Fenton oxidation includes: the time is 30-120min.
According to the present invention, in step b, the mode of described solid-liquid separation can be separate mode commonly used in the art, for instance, the mode of described solid-liquid separation can be stand.In order to obtain better separating effect, the time of standing is preferably 10-40min.
In preferred embodiment of the invention mode, in order to remove the ferrous ion in waste water, and the flocculating sedimentation of (when particularly standing) pollutant when promoting solid-liquid separation further, it is also possible to before solid-liquid separation, the pH value of waste water is regulated to neutral (such as 6-8).
According to the present invention, in step c, in order to obtain better treatment effect, the consumption of described activated sludge is preferably 2500-3500mg/L nitrile rubber and produces waste water.
According to the present invention, to the sludge loading of described activated sludge, there is no particular limitation, it is possible to use various common activated sludge, it is preferable that in situation, the sludge loading of described activated sludge is 0.2-0.5kgCOD/(kg mud d).
According to the present invention, in order to further ensure that effluent quality, it is also preferred that contain activated carbon in the mixed system of step c.
Preferably, described activated carbon is 0.05-0.2:1 with the weight ratio of activated sludge.
Described activated carbon is pore structure prosperity, the big (1500m of specific surface area2/ more than g), the charcoal of high adsorption capacity, be with raw materials such as coal, timber and shells, obtain through carbonization, activation and post processing.Powdered activated carbon, granular active carbon, pressed active carbon and NACF can be divided into by face shaping.
In the present invention, described activated carbon can be commercially available various powdered activated carbons.The granularity of described activated carbon is preferably particle diameter below 100 μm.
According to the present invention, step b separates the liquid phase obtained and mixes with activated sludge and can carry out conventional when, under preferable case, it is 2-4mg/L that the condition that the liquid phase that step b separation obtains mixes with activated sludge includes dissolved oxygen, temperature is 10-40 DEG C, pH value is 6-9, and hydraulic detention time is 8-20h.Well known to a person skilled in the art and be, the operation utilizing active sludge treatment waste water generally carries out in the reactor, and hydraulic detention time refers to pending waste water mean residence time in reactor, namely waste water and the average reaction time of microbial action in reactor.Therefore, if the dischargeable capacity of reactor is V(m3), water velocity is Q(m3/ h), then: hydraulic detention time (HRT)=V/Q, namely hydraulic detention time is equal to the ratio of reactor dischargeable capacity with water velocity.
The method of the present invention can significantly reduce various nitrile rubber and produce the acrylonitrile content in waste water, COD value and ammonia-nitrogen content.In the present invention, it can be 400-700mg/L that pending nitrile rubber produces the content of acrylonitrile in waste water.It can be 1200-1700mg/L that pending nitrile rubber produces the COD value of waste water.It can be 15-25mg/L that pending nitrile rubber produces the turbidity of waste water.It can be 2-4 that pending nitrile rubber produces the pH value of waste water.
Hereinafter will be described the present invention by embodiment.In following example, the Powdered Activated Carbon of use is purchased from Kai Bi source, Beijing trade Co., Ltd；In waste water, the assay method of acrylonitrile content is liquid chromatography, and the INSTRUMENT MODEL of employing is Agilent1100LC；The assay method of COD value is dichromate titration (GB11914-89), COD value can the oligomer in reaction waste to a certain extent, COD value is more little, illustrates that the oligomer in waste water is more low；The assay method of ammonia-nitrogen content is Berthelot spectrophotometry (HJ535-2009)；The assay method of total nitrogen content is that alkaline chitinase clears up ultraviolet spectrophotometry (HJ636-2012)；The assay method of turbidity is referring to GB13200-91；In gas, the assay method of AN content is gas chromatography (HJ/T37-1999).
The water quality of the waste water processed in embodiment is as shown in table 1.
Table 1
| Waste water | AN(mg/L) | COD(mg/L) | Turbidity (mg/L) | pH |
| 1 | 459 | 1263 | 16.3 | 2.3 |
| 2 | 545 | 1370 | 17.3 | 3.2 |
| 3 | 625 | 1540 | 19.7 | 3.8 |
| 4 | 683 | 1652 | 20.4 | 2.6 |
Embodiment 1
Adding seven hydration sodium sulfite in waste water 1, the dosage in 1L waste water is 2160mg.After 10min, above-mentioned waste water enters Fenton oxidation unit, i.e. add H in waste water2O2With ferrous sulfate (with Fe2+Meter), respectively 689mg and the 150mg of the dosage in 1L waste water, the response time is 70min, regulates pH value to neutral after having reacted, and the standing sedimentation time is 20min.Supernatant enters active sludge treatment unit, namely, Powdered Activated Carbon (weight ratio of Powdered Activated Carbon and activated sludge is 0.12:1) is added in activated sludge, sludge loading is 0.23kgCOD/(kg mud d), the consumption of activated sludge is 3200mg/L waste water, and the dissolved oxygen controlling system for handling is 2mg/L, and temperature is 35 DEG C, pH value is 6.5, and hydraulic detention time is 14h.Result is in Table 2.
Embodiment 2
Adding anhydrous sodium sulfite in waste water 2, the dosage in 1L waste water is 1289mg.After 30min, above-mentioned waste water enters Fenton oxidation unit, i.e. add H in waste water2O2With ferrous sulfate (with Fe2+Meter), respectively 981mg and the 258mg of the dosage in 1L waste water, the response time is 90min, regulates pH value to neutral after having reacted, and the standing sedimentation time is 30min.Supernatant enters active sludge treatment unit, namely, Powdered Activated Carbon (weight ratio of Powdered Activated Carbon and activated sludge is 0.17:1) is added in activated sludge, sludge loading is 0.24kgCOD/(kg mud d), the consumption of activated sludge is 2800mg/L waste water, and the dissolved oxygen controlling system for handling is 4mg/L, and temperature is 25 DEG C, pH value is 7.5, and hydraulic detention time is 16h.Result is in Table 2.
Embodiment 3
Adding anhydrous potassium sulfite in waste water 3, the dosage in 1L waste water is 1835mg.After 20min, above-mentioned waste water enters Fenton oxidation unit, i.e. add H in waste water2O2With ferrous sulfate (with Fe2+Meter), respectively 1250mg and the 298mg of the dosage in 1L waste water, the response time is 110min, regulates pH value to neutral after having reacted, and the standing sedimentation time is 35min.Supernatant enters active sludge treatment unit, namely, Powdered Activated Carbon (weight ratio of Powdered Activated Carbon and activated sludge is 0.15:1) is added in activated sludge, sludge loading is 0.33kgCOD/(kg mud d), the consumption of activated sludge is 3000mg/L waste water, and the dissolved oxygen controlling system for handling is 3mg/L, and temperature is 30 DEG C, pH value is 7.0, and hydraulic detention time is 12h.Result is in Table 2.
Embodiment 4
Adding sodium sulfite in waste water 4, the dosage in 1L waste water is 1257mg.After 28min, above-mentioned waste water enters Fenton oxidation unit, i.e. add H in waste water2O2With ferrous sulfate (with Fe2+Meter), respectively 1708mg and the 534mg of the dosage in 1L waste water, the response time is 120min, regulates pH value to neutral after having reacted, and the standing sedimentation time is 25min.Supernatant enters active sludge treatment unit, namely, Powdered Activated Carbon (weight ratio of Powdered Activated Carbon and activated sludge is 0.1:1) is added in activated sludge, sludge loading is 0.50kgCOD/(kg mud d), the consumption of activated sludge is 3500mg/L waste water, and the dissolved oxygen controlling system for handling is 4mg/L, and temperature is 15 DEG C, pH value is 8.0, and hydraulic detention time is 8h.Result is in Table 2.
Embodiment 5
Adding anhydrous sodium sulfite in waste water 2, the dosage in 1L waste water is 1260mg.After 25min, above-mentioned waste water enters Fenton oxidation unit, i.e. add H in waste water2O2With ferrous sulfate (with Fe2+Meter), respectively 273mg and the 118mg of the dosage in 1L waste water, the response time is 30min, regulates pH value to neutral after having reacted, and the standing sedimentation time is 10min.Supernatant enters active sludge treatment unit, namely, Powdered Activated Carbon (weight ratio of Powdered Activated Carbon and activated sludge is 0.08:1) is added in activated sludge, sludge loading is 0.23kgCOD/(kg mud d), the consumption of activated sludge is 2800mg/L waste water, and the dissolved oxygen controlling system for handling is 2mg/L, and temperature is 10 DEG C, pH value is 9.0, and hydraulic detention time is 20h.Result is in Table 2.
Embodiment 6
Adding Potassium acid sulfite in waste water 3, the dosage in 1L waste water is 1350mg.After 22min, above-mentioned waste water enters Fenton oxidation unit, i.e. add H in waste water2O2With ferrous sulfate (with Fe2+Meter), respectively 625mg and the 120mg of the dosage in 1L waste water, the response time is 60min, regulates pH value to neutral after having reacted, and the standing sedimentation time is 40min.Supernatant enters active sludge treatment unit, namely, Powdered Activated Carbon (weight ratio of Powdered Activated Carbon and activated sludge is 0.05:1) is added in activated sludge, sludge loading is 0.42kgCOD/(kg mud d), the consumption of activated sludge is 3200mg/L waste water, and the dissolved oxygen controlling system for handling is 3mg/L, and temperature is 20 DEG C, pH value is 6.0, and hydraulic detention time is 10h.Result is in Table 2.
Embodiment 7
Adding two hydration potassium sulfites in waste water 1, the dosage in 1L waste water is 1594mg.After 15min, above-mentioned waste water enters Fenton oxidation unit, i.e. add H in waste water2O2With ferrous sulfate (with Fe2+Meter), respectively 551mg and the 95mg of the dosage in 1L waste water, the response time is 50min, regulates pH value to neutral after having reacted, and the standing sedimentation time is 15min.Supernatant enters active sludge treatment unit, namely, Powdered Activated Carbon (weight ratio of Powdered Activated Carbon and activated sludge is 0.2:1) is added in activated sludge, sludge loading is 0.26kgCOD/(kg mud d), the consumption of activated sludge is 2500mg/L waste water, and the dissolved oxygen controlling system for handling is 2mg/L, and temperature is 40 DEG C, pH value is 8.5, and hydraulic detention time is 18h.Result is in Table 2.
Embodiment 8
Waste water is processed according to the mode of embodiment 1, the difference is that, the weight ratio of Powdered Activated Carbon and activated sludge is 0.03:1, and result is in Table 2.
Comparative example 1
Waste water 3 is directly entered Fenton oxidation unit, i.e. add H in waste water2O2With ferrous sulfate (with Fe2+Meter), respectively 1250mg and the 298mg of the dosage in 1L waste water, the response time is 110min, regulates pH value to neutral after having reacted, and the sedimentation time is 35min.Result is in Table 2.
Comparative example 2
Adding seven hydration sodium sulfite in waste water 1, the dosage in 1L waste water is 2130mg.After 10min, above-mentioned waste water enters active sludge treatment unit, namely, adding Powdered Activated Carbon (weight ratio of Powdered Activated Carbon and activated sludge is 0.12:1) in activated sludge, sludge loading is 0.68kgCOD/(kg mud d), and the consumption of activated sludge is 3200mg/L waste water, the dissolved oxygen controlling system for handling is 2mg/L, temperature is 35 DEG C, and pH value is 6.5, and hydraulic detention time is 14h.Result is in Table 2.
Table 2
The equal water white transparency of water outlet after nitrile rubber production wastewater treatment in embodiment 1-8, is represented by table 2("/" and is not measured) it can be seen that water outlet all can reach without acrylonitrile residue, COD < 50mg/L, < 5mg/L has good treatment effect to ammonia nitrogen.Through comparing it can be seen that COD is less than embodiment 3 in comparative example 1 Fenton oxidation water outlet, but in its Fenton device exit gas, AN content reaches 31mg/m3, more than embodiment 3(0mg/m3), illustrate not add anhydrous sodium sulfite, Fenton oxidation processing procedure has acrylonitrile and is overflowed by waste water, present invention environmental hazard caused it can be avoided that acrylonitrile is overflowed in processing procedure, nitrile rubber is produced waste water there is good treatment effect.In comparative example 2 bio-chemical effluent, acrylonitrile has residual, COD value to be much higher than embodiment 1, possibly together with a large amount of total nitrogens, illustrates not carry out Fenton oxidation process, and noxious substance and hard-degraded substance in waste water can not be removed by biochemical treatment unit completely.Mutually work in coordination with between each step of the present invention and play a role, indispensable.
Especially, the result of embodiment 1 is compared with the result of embodiment 8 it can be seen that adopt the weight ratio of the activated carbon in preferable range of the present invention and activated sludge to be obtained in that treatment effect more preferably.
The preferred embodiment of the present invention described in detail above; but, the present invention is not limited to the detail in above-mentioned embodiment, in the technology concept of the present invention; technical scheme can being carried out multiple simple variant, these simple variant belong to protection scope of the present invention.
It is further to note that, each concrete technical characteristic described in above-mentioned detailed description of the invention, in reconcilable situation, it is possible to be combined by any suitable mode, in order to avoid unnecessary repetition, various possible compound modes are no longer illustrated by the present invention separately.
Additionally, can also carry out combination in any between the various different embodiment of the present invention, as long as it is without prejudice to the thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (14)
1. the processing method of a nitrile rubber production waste water, it is characterised in that the method comprises the following steps:
A, nitrile rubber produces waste water mixing with sulphite, so that nitrile rubber produces the material of the difficult volatilization of acrylonitrile conversion in waste water, wherein, it is 400-700mg/L that nitrile rubber produces the content of acrylonitrile in waste water；
B, make to carry out advanced oxidation solid-liquid separation with the mixed waste water of sulphite；
C, by step b separate obtain liquid phase mix with activated sludge.
2. method according to claim 1, wherein, it is 1-5:1 that the weight of the sulphite of use and nitrile rubber produce the ratio of the weight of acrylonitrile in waste water.
3. method according to claim 1 and 2, wherein, described sulphite is the alkali metal salt of sulfurous acid.
4. method according to claim 1 and 2, wherein, described sulphite is at least one in sodium sulfite, potassium sulfite, sodium sulfite and Potassium acid sulfite.
5. method according to claim 1, wherein, in step a, makes the condition of the material of the difficult volatilization of acrylonitrile conversion include: the time of mixing is 10-30min.
6. method according to claim 1, wherein, the method for described advanced oxidation is Fenton oxidation method, and it is 0.5-3:1 that the weight of the reagent that Fenton oxidation uses and nitrile rubber produce the ratio of the weight of acrylonitrile in waste water.
7. method according to claim 6, wherein, the reagent that Fenton oxidation uses is hydrogen peroxide and ferrous sulfate, and the weight ratio of hydrogen peroxide and ferrous sulfate is 2-6:1, and the weight of ferrous sulfate is in iron ion.
8. the method according to claim 6 or 7, wherein, the condition of Fenton oxidation includes: the time is 30-120min.
9. method according to claim 1, wherein, the mode of described solid-liquid separation is for standing, and the time of standing is 10-40min.
10. method according to claim 1, wherein, the consumption of described activated sludge is that 2500-3500mg/L nitrile rubber produces waste water.
11. the method according to claim 1 or 10, wherein, the sludge loading of described activated sludge is 0.2-0.5kgCOD/ (kg mud d).
12. method according to claim 1, wherein, possibly together with activated carbon in the mixed system of step c, the weight ratio of described activated carbon and activated sludge is 0.05-0.2:1.
13. method according to claim 1, wherein, it is 2-4mg/L that the condition that the liquid phase that step b separation obtains mixes with activated sludge includes dissolved oxygen, and temperature is 10-40 DEG C, and pH value is 6-9, and hydraulic detention time is 8-20h.
14. method according to claim 1, wherein, it is 1200-1700mg/L that nitrile rubber produces COD value in waste water, and turbidity is 15-25mg/L, and pH value is 2-4.
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| CN105366749A (en) * | 2015-12-15 | 2016-03-02 | 河南师范大学 | Treatment method of high-salinity organic volatile waste water |
| CN106977052A (en) * | 2017-04-24 | 2017-07-25 | 上海洗霸科技股份有限公司 | The processing method of nitrile rubber waste water |
| CN109775903B (en) * | 2017-11-14 | 2022-10-11 | 中国石油化工股份有限公司 | Advanced treatment method of acrylic fiber wastewater |
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