CN113023972A - High-salt organic wastewater treatment method based on electrochemical coupling hydrogen peroxide - Google Patents
High-salt organic wastewater treatment method based on electrochemical coupling hydrogen peroxide Download PDFInfo
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- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 title claims abstract description 64
- 230000008878 coupling Effects 0.000 title claims abstract description 11
- 238000010168 coupling process Methods 0.000 title claims abstract description 11
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 11
- 238000004065 wastewater treatment Methods 0.000 title claims description 7
- 239000000460 chlorine Substances 0.000 claims abstract description 50
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 41
- 239000002351 wastewater Substances 0.000 claims abstract description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 40
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000000034 method Methods 0.000 claims abstract description 35
- 238000010521 absorption reaction Methods 0.000 claims abstract description 34
- 238000003487 electrochemical reaction Methods 0.000 claims abstract description 33
- 238000004062 sedimentation Methods 0.000 claims abstract description 32
- 238000005695 dehalogenation reaction Methods 0.000 claims abstract description 28
- 239000002253 acid Substances 0.000 claims abstract description 24
- 239000003595 mist Substances 0.000 claims abstract description 24
- 238000001179 sorption measurement Methods 0.000 claims abstract description 24
- 239000007788 liquid Substances 0.000 claims abstract description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 10
- 239000001301 oxygen Substances 0.000 claims abstract description 10
- 238000010979 pH adjustment Methods 0.000 claims abstract description 9
- 230000001105 regulatory effect Effects 0.000 claims abstract description 9
- 230000005855 radiation Effects 0.000 claims abstract description 7
- 239000013049 sediment Substances 0.000 claims abstract description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 19
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 229910052799 carbon Inorganic materials 0.000 claims description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 8
- -1 chlorine ions Chemical class 0.000 claims description 8
- 239000003575 carbonaceous material Substances 0.000 claims description 7
- 239000007769 metal material Substances 0.000 claims description 7
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 5
- 229910021536 Zeolite Inorganic materials 0.000 claims description 4
- 229910052782 aluminium Inorganic materials 0.000 claims description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 4
- 239000000440 bentonite Substances 0.000 claims description 4
- 229910000278 bentonite Inorganic materials 0.000 claims description 4
- SVPXDRXYRYOSEX-UHFFFAOYSA-N bentoquatam Chemical compound O.O=[Si]=O.O=[Al]O[Al]=O SVPXDRXYRYOSEX-UHFFFAOYSA-N 0.000 claims description 4
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 4
- 239000004744 fabric Substances 0.000 claims description 4
- 238000005188 flotation Methods 0.000 claims description 4
- 229910052742 iron Inorganic materials 0.000 claims description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical class C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 4
- 239000010457 zeolite Substances 0.000 claims description 4
- 239000002957 persistent organic pollutant Substances 0.000 abstract description 4
- 230000008569 process Effects 0.000 abstract description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 abstract description 3
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 3
- 208000028659 discharge Diseases 0.000 description 7
- 229910052736 halogen Inorganic materials 0.000 description 7
- 150000002367 halogens Chemical class 0.000 description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 230000014759 maintenance of location Effects 0.000 description 6
- 238000001784 detoxification Methods 0.000 description 5
- 239000003344 environmental pollutant Substances 0.000 description 5
- 239000012528 membrane Substances 0.000 description 5
- 231100000719 pollutant Toxicity 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 229910019142 PO4 Inorganic materials 0.000 description 4
- 239000000945 filler Substances 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 239000010452 phosphate Substances 0.000 description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000011033 desalting Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000002848 electrochemical method Methods 0.000 description 2
- 230000005518 electrochemistry Effects 0.000 description 2
- 239000007772 electrode material Substances 0.000 description 2
- 238000005868 electrolysis reaction Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 230000007935 neutral effect Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000011574 phosphorus Substances 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000000909 electrodialysis Methods 0.000 description 1
- 238000006056 electrooxidation reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
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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
-
- 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
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- 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
-
- 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
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
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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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
- C02F1/4674—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation with halogen or compound of halogens, e.g. chlorine, bromine
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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Abstract
Discloses a method for treating high-salt organic wastewater based on electrochemical coupling hydrogen peroxide, which comprises the following steps: inputting the high-salinity organic wastewater into an adjusting tank to adjust the water quality and the water quantity; inputting the effluent of the regulating reservoir into an electrochemical reaction tank and staying for a first preset time, generating free chlorine at an anode by chloride ions, reducing oxygen into hydrogen peroxide at a cathode, removing most of organic pollutants and ammonia nitrogen in the wastewater by active chlorine species and hydroxyl radicals generated by the free chlorine and the hydrogen peroxide under UV radiation, and absorbing chlorine generated in the electrochemical process by an acid mist absorption tower to form an absorption solution; the effluent of the electrochemical reaction tank enters a sedimentation tank and stays for a second preset time to remove suspended matters and sediments; the effluent of the sedimentation tank enters a dehalogenation tank, the pH value of the wastewater is adjusted to be alkaline, and hydrogen peroxide is added to keep a third preset time; the effluent of the dehalogenation tank enters a pH adjusting tank, the absorption liquid in the acid mist absorption tower is guided into the pH adjusting tank for pH adjustment, and the effluent of the pH adjusting tank enters an adsorption tank; and the effluent of the adsorption tank enters a clean water tank to finish treatment.
Description
Technical Field
The invention belongs to the technical field of high-salt organic wastewater, and particularly relates to a high-salt organic wastewater treatment method based on electrochemical coupling hydrogen peroxide.
Background
The high-salinity wastewater is directly discharged without being treated, which can destroy the ecological environment of soil and bring more pressure to the water environment. The treatment effect and efficiency of the high-salinity wastewater are very limited due to the limitations of treatment technology and cost. Aiming at the treatment of high-salt organic wastewater, the traditional method comprises desalting firstly and then performing biochemistry. Common desalting techniques mainly include membrane separation, evaporation, electrodialysis, etc.; however, the membrane separation method is easy to cause membrane blockage, and the use of the membrane separation method is limited because the membrane separation method is expensive; the evaporation method is the most widely used technology at present, but the evaporation cost is too high, so that the treatment of high-salt organic wastewater becomes an important bottleneck limiting the development of related industries; the electrochemical method is a technology for treating high-salinity organic wastewater, which is most likely to realize industrial application, but the large-scale industrial application of the electrochemical method is limited due to the problem caused by halogen organic matters.
The above information disclosed in this background section is only for enhancement of understanding of the background of the invention and therefore it may contain information that does not form the prior art that is already known in this country to a person of ordinary skill in the art.
Disclosure of Invention
Aiming at the defects in the prior art, the purpose of the present disclosure is to provide a method for treating high-salinity organic wastewater based on electrochemical coupling hydrogen peroxide, which overcomes the defects of the 'desalting and biochemical' treatment technology in the prior art and detoxifies halogen organic matters.
In order to achieve the above purpose, the present disclosure provides the following technical solutions:
a method for treating high-salt organic wastewater based on electrochemical coupling hydrogen peroxide comprises the following steps:
in the first step, high-salinity organic wastewater is input into an adjusting tank to adjust the water quality and the water quantity;
in the second step, the effluent of the regulating reservoir is input into an electrochemical reaction pool at a first preset time, an acid mist absorption tower for absorbing acid mist is arranged above the electrochemical reaction pool, a UV radiation unit is arranged below the water surface of the electrochemical reaction pool, free chlorine is generated at the anode through chlorine ions, oxygen is reduced to hydrogen peroxide at the cathode, the free chlorine and the hydrogen peroxide generate active chlorine species and hydroxyl radicals under UV radiation, and the acid mist absorption tower absorbs the free chlorine to generate absorption liquid;
in the third step, the effluent of the electrochemical reaction tank enters a sedimentation tank for a second preset time to remove suspended matters and sediments;
in the fourth step, the effluent of the sedimentation tank enters a dehalogenation tank, the pH value of the wastewater is adjusted to be alkaline, and hydrogen peroxide is added to keep a third preset time;
in the fifth step, the effluent of the dehalogenation tank enters a pH adjusting tank, the absorption liquid in the acid mist absorption tower is guided into the pH adjusting tank for pH adjustment, and the absorption liquid is adjusted and then enters an adsorption tank;
and in the sixth step, the effluent of the adsorption tank enters a clean water tank to finish treatment.
In the method, in the second step S2, the anode of the electrochemical reaction cell is made of metal material, the cathode is made of carbon material, and the current density is 10-30mA/cm2And the distance between the anode and the cathode is 1-3 cm.
In the method, the metal material comprises iron or aluminum, and the carbon material comprises activated carbon fiber, carbon cloth or carbon felt.
In the method, in the second step, the active chlorine species include Cl, Cl2Or ClO.
In the third step, the sedimentation tank comprises an air flotation sedimentation tank, an inclined tube sedimentation tank or a horizontal flow sedimentation tank.
In the method, in the fourth step, caustic soda flakes are put into a dehalogenation tank to keep the pH value between 11 and 14.
In the method, the acid mist absorption tower is communicated with the pH adjusting tank, the filler of the absorption tank can be one or a plurality of combinations of active carbon, bentonite, zeolite and the like, and the corresponding selection is made according to the properties of pollutants.
Compared with the prior art, the beneficial effect that this disclosure brought does:
the invention solves the problems of high energy consumption, high operation cost and easy blockage in the prior art by coupling electrochemical oxidation and hydrogen peroxide dehalogenation, and the effluent can reach the standard discharge.
Drawings
Various additional advantages and benefits of the present disclosure will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the disclosure. It is apparent that the drawings described below are only some embodiments of the disclosure, and that other drawings may be derived from those drawings by one of ordinary skill in the art without inventive effort. Also, like parts are designated by like reference numerals throughout the drawings.
In the drawings:
FIG. 1 is a schematic flow diagram of a method for treating high-salinity organic wastewater based on electrochemical coupling of hydrogen peroxide according to the invention;
fig. 2 is a schematic diagram of a corresponding system integration method of a high-salt organic wastewater treatment method based on electrochemical coupling hydrogen peroxide according to the invention.
The invention is further explained below with reference to the figures and examples.
Detailed Description
Specific embodiments of the present disclosure will be described in more detail below with reference to fig. 1 to 2. While specific embodiments of the disclosure are shown in the drawings, it should be understood that the disclosure may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the disclosure to those skilled in the art.
It should be noted that certain terms are used throughout the description and claims to refer to particular components. As one skilled in the art will appreciate, various names may be used to refer to a component. This specification and claims do not intend to distinguish between components that differ in name but not function. In the following description and in the claims, the terms "include" and "comprise" are used in an open-ended fashion, and thus should be interpreted to mean "include, but not limited to. The description which follows is a preferred embodiment of the disclosure, but is made for the purpose of illustrating the general principles of the disclosure and not for the purpose of limiting the scope of the disclosure. The scope of the present disclosure is to be determined by the terms of the appended claims.
For the purpose of facilitating an understanding of the disclosed embodiments, reference will now be made in detail to the embodiments illustrated in the accompanying drawings, which are not intended to limit the embodiments of the invention.
For better understanding, as shown in fig. 1 and fig. 2, a method for treating high-salt organic wastewater based on electrochemical coupling hydrogen peroxide comprises the following steps:
in the first step S1, high-salt organic wastewater is input into a regulating reservoir to regulate the quality of water quality and water quality;
in a second step S2, the effluent of the regulating reservoir is input into an electrochemical reaction tank at a first preset time, an acid mist absorption tower for absorbing acid mist is arranged above the electrochemical reaction tank, a UV radiation unit is arranged below the water surface of the electrochemical reaction tank, free chlorine is generated at the anode through chloride ions, oxygen is reduced to hydrogen peroxide at the cathode, the free chlorine and the hydrogen peroxide generate active chlorine species and hydroxyl radicals under UV radiation, and the acid mist absorption tower absorbs the free chlorine to generate absorption liquid;
in a third step S3, the effluent of the electrochemical reaction tank enters a sedimentation tank for a second predetermined time to remove suspended matters and sediments;
in a fourth step S4, the effluent of the sedimentation tank enters a dehalogenation tank, the pH value of the wastewater is adjusted to be alkaline, and hydrogen peroxide is added to keep a third preset time;
in a fifth step S5, the effluent of the dehalogenation tank enters a pH adjusting tank, and the absorption liquid in the acid mist absorption tower is guided into the pH adjusting tank for pH adjustment and then enters an adsorption tank after the pH adjustment;
in the sixth step S6, the effluent from the adsorption tank enters a clean water tank to complete the treatment.
In a preferred embodiment of the method, in a first step S1, the predetermined salinity is measured based on sodium chloride in the conditioning tank effluent.
In a preferred embodiment of the method, in the second step S2, the anode of the electrochemical reaction cell is made of a metal material, the cathode is made of a carbon material, and the current density is 10 to 30mA/cm2And the distance between the anode and the cathode is 1-3 cm.
In a preferred embodiment of the method, the metal material comprises iron or aluminum, and the carbon material comprises activated carbon fiber, carbon cloth, or carbon felt.
In a preferred embodiment of the method, in the second step S2, the active chlorine species include Cl, Cl2Or ClO.
In a preferred embodiment of the method, in the third step S3, the sedimentation tank includes an air flotation sedimentation tank, an inclined tube sedimentation tank or a horizontal flow sedimentation tank.
In a preferred embodiment of the method, in the fourth step S4, the dehalogenation cell is maintained at a pH between 11 and 14.
In a preferred embodiment of the method, in the fourth step S4, caustic soda flakes are fed into the dehalogenation tank to maintain the pH at 12.
In a preferred embodiment of the method, the acid mist absorption tower is communicated with the pH adjusting tank, and the adsorption tank can be one or a combination of more of activated carbon, bentonite or zeolite, and is selected correspondingly according to the properties of pollutants.
In one embodiment, the method includes the steps of,
1. wastewater firstly enters an adjusting tank to adjust the water quality and the water quantity;
2. the effluent of the regulating reservoir enters an electrochemical system, and the pollutants are effectively degraded by controlling the pH, the distance between electrodes and the current density according to the attributes of the pollutants;
3. the electrochemical system discharges water, the wastewater enters a sedimentation tank, and suspended matters and sediments are removed in the sedimentation tank;
4. the effluent of the sedimentation tank enters a dehalogenation tank, and halogen organic matters are detoxified by adjusting the pH value of the wastewater to be alkaline and adding hydrogen peroxide in the dehalogenation tank;
5. the effluent of the dehalogenation tank enters a pH adjusting tank, and the absorption liquid in the acid mist tower is guided into the pH adjusting tank for pH adjustment;
6, enabling the effluent of the pH adjusting tank to enter an adsorption tank, and completing the deep removal of pollutants in the adsorption tank;
7. and the effluent of the adsorption tank enters a clean water tank, and the effluent is discharged after reaching the standard.
Further specifically, in the step 2, the electrochemical system is a closed system and comprises an electrochemical reaction tank and an acid mist absorption tower; the electrochemical reaction zone comprises a direct current power supply, an electrode and an ultraviolet lamp, the anode is mainly made of metal materials such as iron and aluminum, the cathode is mainly made of carbon materials such as activated carbon fiber, carbon cloth and carbon felt, and the current density is 10-30mA/cm2The distance between the electrodes is 1-3cm, the electrodes can be flat electrodes, mesh electrodes, three-dimensional electrodes and the like, and the electrodes are immersed in the water body under an ultraviolet lamp; the acid mist absorption tower is positioned at the top of the electrochemical reaction area, and chlorine generated in the electrochemical process is conveyed to the acid mist spray tower through an exhaust fan and a pipeline; (ii) a In the electrochemical reaction pool, chlorine ions generate free chlorine at the anode, and the free chlorine generates active chlorine species with strong oxidation effect under the near-UV radiation
And oxygen active species (
O2-、1O2Etc.), nitrogen in the wastewater can be efficiently removed by active chlorine species, active oxygen species and active chlorine species can effectively degrade organic pollutants, and meanwhile, positive ions generated by the anode electrode material during electrolysis can form precipitates with phosphate in a water body to remove phosphorus in the water.
More specifically, in step 3, the sedimentation tank is mainly used for removing suspended matters and sediments in the wastewater after electrochemical treatment, and the sedimentation tank can be in the form of an air flotation sedimentation tank, an inclined tube sedimentation tank, a horizontal flow sedimentation tank and the like.
More specifically, in step 4, the pH value in the detoxification pool is kept between 11 and 14, and a certain amount of hydrogen peroxide is added.
In step 5, the solution in the acid mist absorption tower is introduced into a pH adjusting tank to adjust the pH, and hydrochloric acid is added when the solution is insufficient;
specifically, in step 6, the filler of the adsorption tank is mainly activated carbon, bentonite, zeolite and the like, and is mainly used for further advanced treatment of halogen organic matters, so that the effluent water is ensured not to contain toxic halogenated organic pollutants.
Example 1
The wastewater in the embodiment is high-salt organic wastewater discharged by a pharmaceutical factory in Jiangsu, and the treatment scale is as follows: 20m3D; the treatment method comprises the following steps: an adjusting tank, an electrochemical reaction tank, a sedimentation tank, a dehalogenation tank, a pH adjusting tank and an adsorption tank.
Wastewater firstly enters an adjusting tank, water quality and water quantity are adjusted, then the wastewater enters an electrochemical system, firstly enters an electrochemical reaction tank, chlorine ions generate free chlorine at an anode by adjusting the voltage in the electrochemical reaction tank, oxygen is reduced to hydrogen peroxide at a cathode, and the free chlorine and the hydrogen peroxide generate active chlorine species (Cl & lt- & gt ) with strong oxidation effect under UC radiation2The hydraulic retention time of the hydroxyl free radicals in the electrochemical reaction tank is 6 hours, and the removal of organic matters and ammonia nitrogen is basically completed in the electrochemical reaction tank; the effluent after electrochemical treatment enters an inclined tube sedimentation tank, the hydraulic retention time is 0.5 hour, and phosphate in the water is removed through sludge discharge; the effluent of the battery settling enters a dehalogenation pool, the pH of a water body is maintained to be about 12 by adding caustic soda flakes into the dehalogenation pool, then hydrogen peroxide is added, the hydraulic retention time is 2 hours, and the detoxification of a small amount of halogen organic matters generated due to electrochemistry is completed in the dehalogenation pool; the effluent of the dehalogenation tank enters a pH adjusting tank, and the pH is adjusted to be neutral by using the absorption liquid in the acid mist absorption tower, so that the amount of the absorption liquid is sometimes adjustedWhen the pH value is not enough, extra hydrochloric acid is needed to be added for pH adjustment; the effluent of the pH adjusting tank enters an adsorption tank, and the filler of the adsorption tank is mainly activated carbon; and the adsorbed effluent enters a clean water tank, and the effluent reaches the sewage comprehensive secondary discharge standard.
Table 1 shows the control item change table (unit: mg/L, pH removal) in the high-salt organic wastewater before and after the treatment by the process technology of' regulating tank + electrochemical system + dehalogenation tank + adsorption tank
TABLE 1 comparison table before and after wastewater treatment
Example 2
The wastewater in the embodiment is high-salt organic wastewater discharged by a pharmaceutical factory in Jiangxi, and the treatment scale is as follows: 50m3D; the treatment method comprises the following steps: the method comprises a regulating tank, an electrochemical reaction tank, an electrochemical sedimentation tank, a dehalogenation tank and an adsorption tank.
Wastewater firstly enters an adjusting tank, water quality and water quantity are adjusted, then the wastewater enters an electrochemical system, firstly enters an electrochemical reaction tank, chloride ions generate free chlorine at an anode by adjusting voltage in the electrochemical reaction tank, oxygen is reduced to hydrogen peroxide at a cathode, and the free chlorine and the hydrogen peroxide generate active chlorine species (Cl & lt + & gt and Cl & lt + & gt) with strong oxidation effect under UV radiation2The water power retention time of the hydroxyl free radical in the electrochemical reaction tank is 10 hours, and the removal of organic matters and ammonia nitrogen is basically completed in the electrochemical reaction tank; the effluent after electrochemical treatment enters a sedimentation tank, the hydraulic retention time is 0.5 hour, and phosphate in the water is removed through sludge discharge; the effluent of the electrochemical precipitation cell enters a dehalogenation pool, the pH of a water body is maintained to be about 12 by adding caustic soda flakes into the dehalogenation pool, then hydrogen peroxide is added, the hydraulic retention time is 2.5 hours, and the detoxification of a small amount of halogen organic matters generated by electrochemistry is completed in the dehalogenation pool; the effluent of the dehalogenation tank enters a pH adjusting tank, the pH is adjusted to be neutral by using absorption liquid in an acid mist absorption tower, and hydrochloric acid is additionally added for pH adjustment when the amount of the absorption liquid is insufficient; the effluent of the pH adjusting tank enters an adsorption tankThe filler of the adsorption tank is mainly activated carbon; and the adsorbed effluent enters a clean water tank, and the effluent reaches the sewage comprehensive secondary discharge standard.
Table 2 shows the control item change table (unit: mg/L, pH removal) in the high-salt organic wastewater before and after the treatment by the "adjusting tank + electrochemical system + dehalogenation tank + adsorption tank" process technology of the invention
TABLE 2 comparison table before and after wastewater treatment
The wastewater enters an adjusting tank, the water quality and the water quantity are adjusted, and then the wastewater enters an electrochemical reaction tank; in the electrochemical reaction pool, chlorine ions generate free chlorine at the anode, and the free chlorine generates active chlorine species with strong oxidation effect under the near-UV radiation
And oxygen active species (
O2 -、1O2And the like), nitrogen in the wastewater can be efficiently removed by active chlorine species, active oxygen species and active chlorine species can effectively degrade organic pollutants, and meanwhile, positive ions generated by the anode electrode material during electrolysis can form precipitates with phosphate in a water body to remove phosphorus in the water; after electrochemical treatment, the wastewater enters a detoxification pool, and halogen organic matters are detoxified by adjusting the pH of the wastewater to be alkaline and adding hydrogen peroxide in the detoxification pool; the detoxified wastewater enters a pH adjusting tank, the pH is adjusted and then enters an adsorption tank, and deep purification is further carried out in the adsorption tank; after being adsorbed, the effluent enters a clean water tank, and the effluent can reach the comprehensive secondary sewage discharge standard.
Although the embodiments of the present invention have been described above with reference to the accompanying drawings, the present invention is not limited to the above-described embodiments and application fields, and the above-described embodiments are illustrative, instructive, and not restrictive. Those skilled in the art, having the benefit of this disclosure, may effect numerous modifications thereto without departing from the scope of the invention as defined by the appended claims.
Claims (7)
1. A high-salt organic wastewater treatment method based on electrochemical coupling hydrogen peroxide comprises the following steps:
in a first step S1, inputting high-salinity organic wastewater into a regulating reservoir to regulate water quality and water quantity;
in a second step S2, inputting the effluent of the regulating reservoir into an electrochemical reaction tank to stay for a first preset time, arranging an acid mist absorption tower above the electrochemical reaction tank for absorbing acid mist, arranging a UV radiation unit below the water surface of the electrochemical reaction tank, generating free chlorine at an anode through chlorine ions, reducing oxygen to hydrogen peroxide at a cathode, generating active chlorine species and hydroxyl radicals from the free chlorine and the hydrogen peroxide under UV radiation, and absorbing the free chlorine by the acid mist absorption tower to generate an absorption liquid;
in a third step S3, the effluent of the electrochemical reaction tank enters a sedimentation tank and stays for a second preset time to remove suspended matters and sediments;
in a fourth step S4, the effluent of the sedimentation tank enters a dehalogenation tank, the pH value of the wastewater is adjusted to be alkaline, and hydrogen peroxide is added to keep a third preset time;
in a fifth step S5, the effluent of the dehalogenation tank enters a pH adjusting tank, and the absorption liquid in the acid mist absorption tower is guided into the pH adjusting tank for pH adjustment and then enters an adsorption tank after the pH adjustment;
in the sixth step S6, the effluent from the adsorption tank enters a clean water tank to complete the treatment.
2. The method according to claim 1, wherein in the second step S2, the anode of the electrochemical reaction cell is made of metal material, the cathode is made of carbon material, and the current density is 10-30mA/cm2And the distance between the anode and the cathode is 1-3 cm.
3. The method of claim 2, wherein the metallic material comprises iron or aluminum and the carbon material comprises activated carbon fiber, carbon cloth, carbon felt.
4. The method of claim 1, wherein in the second step S2, the active chlorine species comprises Cl, Cl2Or ClO.
5. The method according to claim 1, wherein in the third step S3, the sedimentation tank further comprises an air flotation sedimentation tank, an inclined tube sedimentation tank or a horizontal flow sedimentation tank.
6. The method of claim 1, wherein in a fourth step S4, the pH of the dehalogenation tank is maintained at 11-14 by feeding caustic soda flakes.
7. The method of claim 1, wherein the acid mist absorption tower is communicated with the pH adjusting tank, and the adsorption tank is filled with activated carbon, bentonite or zeolite.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114835210A (en) * | 2022-04-28 | 2022-08-02 | 南昌航空大学 | Novel method for treating cyanide through electrocatalysis coupling ultraviolet light auxiliary advanced oxidation |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102153220A (en) * | 2011-02-21 | 2011-08-17 | 中国科学院生态环境研究中心 | Method for treating and recycling polishing waste water of plated part in electroplating industry |
| CN102874961A (en) * | 2012-09-25 | 2013-01-16 | 科迈化工股份有限公司 | Method for treating wastewater of rubber vulcanization accelerator N-cyclohexyl-2-benzothiazolylsulfenamide (CBS) |
| CN103922524A (en) * | 2014-05-14 | 2014-07-16 | 山东盛阳集团有限公司 | Advanced treatment method for coking wastewater |
| CN106698764A (en) * | 2017-03-16 | 2017-05-24 | 深圳市世清环保科技有限公司 | Method for removing phosphorus and nickel in electroless nickel-plating wastewater and treatment system |
| CN110759437A (en) * | 2019-10-12 | 2020-02-07 | 清华苏州环境创新研究院 | Method for electrochemical-UV composite treatment of refractory organic matters |
-
2021
- 2021-03-12 CN CN202110273771.8A patent/CN113023972A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102153220A (en) * | 2011-02-21 | 2011-08-17 | 中国科学院生态环境研究中心 | Method for treating and recycling polishing waste water of plated part in electroplating industry |
| CN102874961A (en) * | 2012-09-25 | 2013-01-16 | 科迈化工股份有限公司 | Method for treating wastewater of rubber vulcanization accelerator N-cyclohexyl-2-benzothiazolylsulfenamide (CBS) |
| CN103922524A (en) * | 2014-05-14 | 2014-07-16 | 山东盛阳集团有限公司 | Advanced treatment method for coking wastewater |
| CN106698764A (en) * | 2017-03-16 | 2017-05-24 | 深圳市世清环保科技有限公司 | Method for removing phosphorus and nickel in electroless nickel-plating wastewater and treatment system |
| CN110759437A (en) * | 2019-10-12 | 2020-02-07 | 清华苏州环境创新研究院 | Method for electrochemical-UV composite treatment of refractory organic matters |
Non-Patent Citations (3)
| Title |
|---|
| 吴向阳 等主编: "《水污染控制工程及设备》", 31 August 2015, 中国环境出版社, pages: 67 - 69 * |
| 施悦 等主编: "《环境氧化还原处理技术原理与应用》", 31 August 2013, 哈尔滨工业大学出版社, pages: 189 - 190 * |
| 杨铭鼎 主编: "《中国医学百科全书 公共卫生工程学》", 31 October 1986, 上海科学技术出版社, pages: 91 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114835210A (en) * | 2022-04-28 | 2022-08-02 | 南昌航空大学 | Novel method for treating cyanide through electrocatalysis coupling ultraviolet light auxiliary advanced oxidation |
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