CN109824194A - A kind of processing method of high COD organic wastewater with high salt - Google Patents
A kind of processing method of high COD organic wastewater with high salt Download PDFInfo
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- CN109824194A CN109824194A CN201910160612.XA CN201910160612A CN109824194A CN 109824194 A CN109824194 A CN 109824194A CN 201910160612 A CN201910160612 A CN 201910160612A CN 109824194 A CN109824194 A CN 109824194A
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Abstract
The invention discloses a kind of processing methods of high COD organic wastewater with high salt, it is evaporated through ultrafiltration membrance filter, COD remover oxidation processes and multiple-effect or MVR, effectively high COD organic wastewater with high salt can be handled, the removal rate of salt and COD have reached 97% or more in high-salt wastewater, it can continuous processing, continuous productive process, treating capacity is big, is suitable for promoting the use of.
Description
Technical field
The invention belongs to technical field for the treatment of of organic waste, and in particular to a kind of processing side of high COD organic wastewater with high salt
Method.
Background technique
Since the 1990s, with the fast development of China's textile industry, dyeing scale is expanded rapidly, dye
The production of material and usage amount are increasing.A large amount of high COD, high chroma, high toxicity, high salinity, the dye of low B/C are generated as a result,
Expect waste water.According to statistics, it is total to account for textile waste up to 24.3 hundred million tons for waste water from dyestuff total amount caused by dyeing in 2009
80 parts or more of discharge amount.The characteristics of " four high one is low " that this kind of waste water from dyestuff has, and it is related with the type of dyestuff is used.
At the same time, in DYE PRODUCTION, the enrichment of salt is mainly made by the addition of production technology and process auxiliaries in waste discharge
At.For example, only villaumite mass fraction is as high as 60g/L in the comprehensive wastewater of Jiangsu dyestuff factory.As it can be seen that how efficiently to locate
The dyeing waste water of high salinity, high pollution degree is managed, separation of the villaumite from water up to standard is realized, meets recycling for freshwater resources and want
It asks, it has also become the problem for the treatment of of dyeing wastewater.
In Chemical Manufacture, pesticide producing process can also generate a large amount of high-salt wastewater.According to statistics, national pesticide producing factory
Up to 1600 or so, pesticide annual output is up to 47.6 ten thousand tons.Wherein, the production of organophosphorus pesticide account for 50 parts of pesticide industry with
On.The characteristics of this kind of agricultural chemicals waste water is: organic concentration is high, pollutant component is complicated, toxicity is big, difficult to degrade, water quality is unstable etc..
For example, it is useless that concentrated mother liquor process can generate dense phosphate and sodium chloride in the production process of herbicide glyphosate
Water, COD are 50000mg/L or so, and the content of salt is up to 150g/L.For such high COD, agricultural chemicals waste water with high salt, it is necessary to
The measure of being effectively treated is taken to be handled.Otherwise, serious environmental pollution will be caused.
In addition to this, in other chemical production process, high-salt wastewater generation is also had.For example, ammonia-soda process prepares soda ash
In production, the soluble-salt content of system waste discharge is generally 15 parts~20 parts reachable after ammonia still process processing, and wherein most is
CaCl2,NaCl.In coal chemical industry, brine waste is after thermal concentration technique, and the concentration waste water salt content of outlet is up to 20
Part or more.For the high-salt wastewater generated in chemical process, due to deriving from different chemical products and production technology, high-salt wastewater
Property it is also different.Therefore, for the various high-salt wastewaters directly generated in Chemical Manufacture, the difference according to high-salt wastewater is needed
Source, property are classified and optimum process are selected to handle.
The traditional processing method of high COD organic wastewater with high salt has following two:
One, located again through bioanalysis, chemical oxidization method and physical treatment process etc. after high COD organic wastewater dilution with high salt
Reason, this method are generally only applicable to the situation that salt content is lower and COD content is relatively low, and otherwise processing cost can be very high.
Two, preliminary treatment is first carried out to high COD organic wastewater with high salt using Fenton chemical oxidization method, be then then sent through useless
Water treatment plant carries out secondary treatment.Fenton chemical oxidization method is using hydrogen peroxide as oxidant, to having under ferrous ion effect
Machine object carry out oxidative degradation a kind of method, its advantage is that operating condition is milder, but its disadvantage is also obvious: 1) by
There is very strong catalyticing decomposition action to hydrogen peroxide in ferrous ion, cause the utilization rate of hydrogen peroxide not high, processing cost is high；2)
Fenton chemical oxidization method needs the first pH adjusting proximity neutrality by waste water, thus can consume soda acid, while can introduce other kinds
The inorganic salts of class；3) Fenton chemical oxidization method mainly converts hardly degraded organic substance to and is relatively easy to the organic of biochemical degradation
Object, generally cannot degradable organic matter, thus can only partially remove COD, the subsequent biochemical treatment apparatus that also to enter carries out two
Secondary degradation, therefore this method is typically only capable to the preprocess method as organic wastewater with difficult degradation thereby；4) for high-salt wastewater, warp
After the processing of Fenton chemical oxidization method, inorganic salt content is not reduced, and also just be can be carried out biochemical degradation by dilution, otherwise be given birth to
The bacterium changed in degradation process can not adapt to high content of salt；5) not applicable through Fenton chemical oxidization method treated high-salt wastewater
In direct high-efficiency evaporating desalination because Fenton method can not thorough degradation of organic substances, these remaining organic matters easily enter nothing
In machine salt, the inorganic salts after leading to removing become solid hazardous waste.
Since this kind of liquid waste concentration is high, often complex treatment process, used device are more, reagent cost is high, make at waste liquid
The cost of reason is too high, and general company is difficult to bear, and all using the waste liquid of high COD content with high salt as dangerous waste, high price is handed over for most companies
It is handled by specialized company, but some enterprises are made a desperate move by cost pressure, the illegal row of stealing is directly discharged into urban pipe network and enters sewage
Treatment plant has seriously affected the normal operation of municipal sewage plant.Therefore, seek new high-efficiency environment friendly in high COD with high salt
The remover of organic wastewater has important practical significance.
Summary of the invention
The purpose of the present invention is to provide a kind of processing method of high COD organic wastewater with high salt, addition is made with ferrate
For host agent, compounding with organic flocculant and metal salt be subject to auxiliary material compound COD removal and, can be effectively reduced high COD with high salt
COD content in organic wastewater.
To realize above-mentioned target, the technical solution adopted by the present invention is that:
A kind of processing method of high COD organic wastewater with high salt, includes the following steps:
S1, high COD organic wastewater with high salt is imported into pretreatment pool filtering and impurity removing, its floaters on surface is carried out at salvaging
Reason；
The waste water that S2, pretreatment pool are discharged imports in reaction tank, and the COD remover of certain mass is added into reaction tank,
The mass ratio of high COD organic wastewater with high salt and COD remover is 1:0.02~1:0.08, at normal temperature stirring a period of time, will
Organic matter is converted into carbon dioxide and water, mineralized nitrogen and enters atmosphere at nitrogen, and the organic phosphorus phosphate radical that is converted into is removed；
S3, reaction tank discharge liquor is imported into active carbon filtering ponds, settles solids through filtering and removing；
S4, it active carbon filtering ponds discharge liquor is exported to carries out flash distillation desalination in evaporator, the condensed water after desalination reaches
Discharge standard.
Further, the content of the inorganic salts in the high COD organic wastewater with high salt is 1.0~25.0wt.%, COD
Content be 2000~100000mg/L.
Further, filter uses ultrafiltration membrane in step S1, it is preferred to use the hollow fibre of external-compression type that aperture is 1~10 μm
Tie up film；
Through a step, in step S2, the time of stirring is 1~100 hour, preferably 10~50 hours, most preferably 20~40
Hour.
Further, in step S3, replacement in active carbon 3~5 days is primary in active carbon filtering ponds.
Further, evaporator is multiple-effect or MVR evaporator in step S4.
The mass fraction of each component in the COD remover are as follows: 10 parts~55 parts of ferrate, magnesium chloride 0.1 part~5
Part, 0 part~25 parts of inorganic flocculating agent, 0 part~15 parts of organic flocculant, 0.1 part~15 parts, 0.1 part of sodium nitrite of sodium sulfite
~5 parts, 1 part~2.5 parts of sodium pyrosulfite, 10 parts~55 parts of calcium oxide, 10 parts~25 parts of adsorbent, the above pulvis component is equal
It is even to be mixed into intermixture.
Further, the ferrate is Na2Fe04 or potassium ferrate
Further, the organic flocculant is diallyl dimethyl ammoniumchloride.
Further, the inorganic flocculant is as cation and nitrate anion or sulfate radical with aluminium or iron as yin
The inorganic salts of ion.Wherein the inorganic flocculant is selected from: ferric sulfate (III), bodied ferric sulfate, ferric nitrate (III), nitric acid
Aluminium, aluminum sulfate and any combination thereof.
Further, the adsorbent is active carbon or molecular sieve or macroporous absorbent resin.The adsorbent is preferred
For active carbon, wherein 300 mesh of average particle size particle size~400 mesh of the active carbon.
Ferro element is positive sexavalence in ferrate (sodium, potassium), has very strong oxidisability, at the same time, itself is reduced
At the Fe (OH) 3 of nascent state, this is a kind of inorganic flocculating agent best in quality, can efficiently remove the fine suspended matter in water.
It is demonstrated experimentally that due to its strong oxidation and flocculation collective effect, the disinfection of ferrate and scavenging effect, comprehensively better than containing chlorine
Disinfectant and permanganate；More importantly it in the purification process entirely to water, does not generate any be harmful to the human body
Substance.
Exothermic heat of reaction polymer-inorganic and organic wadding are generated using the oxidation reaction of the thermal response and Na2Fe04 of CaO and water
The solidifying obtained composite flocculation agent of agent, generates a large amount of polynuclear complex with organic matter positively charged in water after hydrolysis,
The effects of under faintly acid to neutrallty condition by adsorbing, building bridge, be crosslinked, keep the colloidal particles in water agglomerated together, reaches high
The effect of effect removal COD.
The present invention compared to the prior art, beneficial effects of the present invention: the processing of high COD organic wastewater with high salt of the invention
Method is evaporated through ultrafiltration membrance filter, COD remover oxidation processes and multiple-effect or MVR, can be effectively organic to high COD with high salt
Waste water is handled, and the removal rate of salt and COD have reached 97% or more in high-salt wastewater, can continuous processing, continuous productive process, processing
Amount is big, is suitable for promoting the use of.
Specific embodiment
The following is a clear and complete description of the technical scheme in the embodiments of the invention, it is clear that described embodiment
Only a part of the embodiment of the present invention, instead of all the embodiments.Based on the embodiments of the present invention, the common skill in this field
Art personnel every other embodiment obtained without making creative work belongs to the model that the present invention protects
It encloses.
[embodiment 1]
A kind of COD remover, the mass fraction of each component are as follows: 35 parts of ferrate, 0.1 part of magnesium chloride, aluminum nitrate 3
Part, 12 parts of diallyl dimethyl ammoniumchloride, 3 parts of sodium sulfite, 3 parts of sodium nitrite, 1 part of sodium pyrosulfite, calcium oxide 12
Part, 22 parts of active carbon, the above pulvis component is uniformly mixed into as intermixture.
[embodiment 2]
A kind of COD remover, the mass fraction of each component are as follows: 55 parts of ferrate, 0.1 part of magnesium chloride, aluminum sulfate 12
Part, 11 parts of diallyl dimethyl ammoniumchloride, 0.1 part of sodium sulfite, 2 parts of sodium nitrite, 2.5 parts of sodium pyrosulfite, oxidation
23 parts of calcium, 12 parts of active carbon, the above pulvis component is uniformly mixed into as intermixture.
[embodiment 3]
A kind of COD remover, the mass fraction of each component are as follows: 40 parts of ferrate, 0.2 part of magnesium chloride, iron chloride 1
Part, 3 parts of diallyl dimethyl ammoniumchloride, 6.5 parts of sodium sulfite, 2 parts of sodium nitrite, 1.5 parts of sodium pyrosulfite, calcium oxide
25 parts, 105 parts of molecular sieve, the above pulvis component is uniformly mixed into as intermixture.
[embodiment 4]
A kind of COD remover, the mass fraction of each component are as follows: 35 parts of ferrate, 2 parts of magnesium chloride, 20 parts of iron chloride,
15 parts of diallyl dimethyl ammoniumchloride, 3 parts of sodium sulfite, 5 parts of sodium nitrite, 1 part of part of sodium pyrosulfite, calcium oxide 35
10 parts of part, active carbon parts, the above pulvis component is uniformly mixed into as intermixture.
[embodiment 5]
S1, by high COD organic wastewater with high salt, (content of inorganic salts is 1.0wt.%, and the content of COD is 100000mg/L)
Import pretreatment pool filtering and impurity removing, filter uses aperture for 10 μm of external pressing type hollow fibrous membrane, to its floaters on surface into
Row salvaging processing；
The waste water that S2, pretreatment pool are discharged imports in reaction tank, prepared by the embodiment 1 that certain mass is added into reaction tank
COD remover, the mass ratio of high COD organic wastewater with high salt and COD remover is 1:0.08, stir 50 hours at normal temperature,
Carbon dioxide and water, mineralized nitrogen are converted by organic matter and enters atmosphere at nitrogen, and the organic phosphorus phosphate radical that is converted into is removed；
S3, reaction tank discharge liquor is imported into active carbon filtering ponds, settles solids through filtering and removing, replaces within active carbon 3 days
Once；
S4, it active carbon filtering ponds discharge liquor is exported to carries out flash distillation desalination in MVR evaporator, the condensed water after desalination is straight
Run in and puts, through detecting, the removal rate of treated organic wastewater COD is 98.25%, and the rate of recovery of inorganic salts is 99.3%,
[embodiment 6]
S1, high COD organic wastewater (content of inorganic salts is 25wt.%, and the content of COD is 9000mg/L) with high salt is imported
Pretreatment pool filtering and impurity removing, filter use aperture for 10 μm of external pressing type hollow fibrous membrane, beat its floaters on surface
Fishing processing；
The waste water that S2, pretreatment pool are discharged imports in reaction tank, prepared by the embodiment 2 that certain mass is added into reaction tank
COD remover, the mass ratio of high COD organic wastewater with high salt and COD remover is 1:0.02, stir 10 hours at normal temperature,
Carbon dioxide and water, mineralized nitrogen are converted by organic matter and enters atmosphere at nitrogen, and the organic phosphorus phosphate radical that is converted into is removed；
S3, reaction tank discharge liquor is imported into active carbon filtering ponds, settles solids through filtering and removing, replaces within active carbon 5 days
Once；
S4, it active carbon filtering ponds discharge liquor is exported to carries out flash distillation desalination in MVR evaporator, the condensed water after desalination is straight
Run in and puts, through detecting, the removal rate of treated organic wastewater COD is 97.35%, and the rate of recovery of inorganic salts is 99.0%,
[embodiment 7]
S1, high COD organic wastewater (content of inorganic salts is 13wt.%, and the content of COD is 80000mg/L) with high salt is led
Enter pretreatment pool filtering and impurity removing, filter uses aperture for 3 μm of external pressing type hollow fibrous membrane, beats its floaters on surface
Fishing processing；
The waste water that S2, pretreatment pool are discharged imports in reaction tank, prepared by the embodiment 3 that certain mass is added into reaction tank
COD remover, the mass ratio of high COD organic wastewater with high salt and COD remover is 1:0.05, stir 40 hours at normal temperature,
Carbon dioxide and water, mineralized nitrogen are converted by organic matter and enters atmosphere at nitrogen, and the organic phosphorus phosphate radical that is converted into is removed；
S3, reaction tank discharge liquor is imported into active carbon filtering ponds, settles solids through filtering and removing, replaces within active carbon 3 days
Once；
S4, it active carbon filtering ponds discharge liquor is exported to carries out flash distillation desalination in multi-effect evaporator, the condensed water after desalination
Direct emission, through detecting, the removal rate of treated organic wastewater COD is 98.15%, and the rate of recovery of inorganic salts is 96.1%,
[embodiment 8]
S1, high COD organic wastewater (content of inorganic salts is 12wt.%, and the content of COD is 30000mg/L) with high salt is led
Enter pretreatment pool filtering and impurity removing, filter uses aperture for 2 μm of external pressing type hollow fibrous membrane, to its floaters on surface into
Row salvaging processing；
The waste water that S2, pretreatment pool are discharged imports in reaction tank, and the embodiment 4 that certain mass is added into reaction tank is made
The mass ratio of standby COD remover, high COD organic wastewater with high salt and COD remover is 1:0.02, and it is small to stir 30 at normal temperature
When, carbon dioxide and water, mineralized nitrogen are converted by organic matter and enters atmosphere at nitrogen, and the organic phosphorus phosphate radical that is converted into is gone
It removes；
S3, reaction tank discharge liquor is imported into active carbon filtering ponds, settles solids through filtering and removing, replaces within active carbon 3 days
Once；
S4, it active carbon filtering ponds discharge liquor is exported in multiple-effect or MVR evaporator carries out flash distillation desalination, it is cold after desalination
Condensate direct emission, through detecting, the removal rate of treated organic wastewater COD is 97.25%, and the rate of recovery of inorganic salts is
99.2%,
Above description sufficiently discloses a specific embodiment of the invention.It should be pointed out that being familiar with the field
Range of any change that technical staff does a specific embodiment of the invention all without departing from claims of the present invention.
Correspondingly, the scope of the claims of the invention is also not limited only to previous embodiment.
Claims (10)
1. a kind of processing method of high COD organic wastewater with high salt, includes the following steps:
S1, high COD organic wastewater with high salt is imported into pretreatment pool filtering and impurity removing, salvaging processing is carried out to its floaters on surface；
The waste water that S2, pretreatment pool are discharged imports in reaction tank, and the COD remover of certain mass is added into reaction tank, with high salt
The mass ratio of high COD organic wastewater and COD remover is 1:0.02~1:0.08, at normal temperature stirring a period of time, will be organic
Object is converted into carbon dioxide and water, mineralized nitrogen and enters atmosphere at nitrogen, and the organic phosphorus phosphate radical that is converted into is removed；
S3, reaction tank discharge liquor is imported into active carbon filtering ponds, settles solids through filtering and removing；
S4, it active carbon filtering ponds discharge liquor is exported to carries out flash distillation desalination in evaporator, the condensed water after desalination reaches discharge
Standard.
2. the processing method of high COD organic wastewater with high salt according to claim 1, it is characterised in that: further, described
High COD organic wastewater with high salt in the contents of inorganic salts be 1.0~25.0wt.%, the content of COD is 2000~
100000mg/L。
3. the processing method of high COD organic wastewater with high salt according to claim 1, which is characterized in that further, step
Filter uses ultrafiltration membrane in S1, it is preferred to use the external pressing type hollow fibrous membrane that aperture is 1~10 μm.
4. the processing method of high COD organic wastewater with high salt according to claim 1, which is characterized in that through a step, step
In S2, the time of stirring is 1~100 hour, preferably 10~50 hours, most preferably 20~40 hours.
5. the processing method of high COD organic wastewater with high salt according to claim 4, which is characterized in that further, step
In S3, replacement in active carbon 3~5 days is primary in active carbon filtering ponds.
6. the processing method of high COD organic wastewater with high salt according to claim 1, which is characterized in that further, step
Evaporator is multiple-effect or MVR evaporator in S4.
7. the processing method of high COD organic wastewater with high salt according to claim 1-6, which is characterized in that described
COD remover in each component mass fraction are as follows: 10 parts~55 parts of ferrate, 0.1 part~5 parts of magnesium chloride, inorganic flocculation
0 part~25 parts of agent, 0 part~15 parts of organic flocculant, 0.1 part~15 parts of sodium sulfite, 0.1 part~5 parts of sodium nitrite, burnt sulfurous
1 part~2.5 parts of sour sodium, 10 parts~55 parts of calcium oxide, 10 parts~25 parts of adsorbent, it is mixed that the above pulvis component, which is uniformly mixed into,
Mixture.
8. the processing method of high COD organic wastewater with high salt according to claim 7, it is characterised in that: the ferric acid
Salt is Na2Fe04 or potassium ferrate；The organic flocculant is diallyl dimethyl ammoniumchloride；The inorganic cohesion
Agent is the inorganic salts with aluminium or iron as cation and nitrate anion or sulfate radical as anion；Ferric sulfate (III), polymerization
Ferric sulfate, ferric nitrate (III), aluminum nitrate, aluminum sulfate and any combination thereof.
9. the processing method of high COD organic wastewater with high salt according to claim 7, further, the adsorbent is
Active carbon or molecular sieve or macroporous absorbent resin.
10. the processing method of high COD organic wastewater with high salt according to claim 7, it is characterised in that: the adsorbent
Preferably active carbon, wherein 300 mesh of average particle size particle size~400 mesh of the active carbon.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111624062A (en) * | 2020-04-13 | 2020-09-04 | 南京曼蕊生物科技有限公司 | Chemical wastewater anti-interference detection pretreatment and COD detection kit |
| CN113087296A (en) * | 2021-04-07 | 2021-07-09 | 江苏瑞恒新材料科技有限公司 | Method for treating nitrochlorobenzene wastewater |
| CN116947266A (en) * | 2023-09-20 | 2023-10-27 | 广东绿日环境科技有限公司 | Treatment process for comprehensive sewage and high-salt wastewater |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102126806A (en) * | 2011-01-17 | 2011-07-20 | 无锡德宝水务投资有限公司 | Method for completely recycling wastewater containing fluorine and ammonia nitrogen in electronic industry |
| CN102295335A (en) * | 2011-08-04 | 2011-12-28 | 安徽师范大学 | Flocculating-agent composition |
| CN105174641A (en) * | 2015-10-10 | 2015-12-23 | 博瑞德（南京）净化技术有限公司 | Treating technology for chemical RO concentrated water |
| CN105600911A (en) * | 2016-02-22 | 2016-05-25 | 同济大学 | Method for quickly removing organic pollutants in water based on intermediate-state iron |
| CN106517622A (en) * | 2016-09-23 | 2017-03-22 | 江苏新宇天成环保工程集团有限公司 | Separation and reuse method of sodium sulfate from high salinity wastewater |
| CN108975420A (en) * | 2017-06-05 | 2018-12-11 | 艺康美国股份有限公司 | COD (COD) removes mixture of powders |
| CN108996808A (en) * | 2018-07-02 | 2018-12-14 | 山西太钢不锈钢股份有限公司 | The biochemical combined treatment process and equipment of steel and iron industry concentrated water difficult to degrade |
-
2019
- 2019-03-04 CN CN201910160612.XA patent/CN109824194A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102126806A (en) * | 2011-01-17 | 2011-07-20 | 无锡德宝水务投资有限公司 | Method for completely recycling wastewater containing fluorine and ammonia nitrogen in electronic industry |
| CN102295335A (en) * | 2011-08-04 | 2011-12-28 | 安徽师范大学 | Flocculating-agent composition |
| CN105174641A (en) * | 2015-10-10 | 2015-12-23 | 博瑞德（南京）净化技术有限公司 | Treating technology for chemical RO concentrated water |
| CN105600911A (en) * | 2016-02-22 | 2016-05-25 | 同济大学 | Method for quickly removing organic pollutants in water based on intermediate-state iron |
| CN106517622A (en) * | 2016-09-23 | 2017-03-22 | 江苏新宇天成环保工程集团有限公司 | Separation and reuse method of sodium sulfate from high salinity wastewater |
| CN108975420A (en) * | 2017-06-05 | 2018-12-11 | 艺康美国股份有限公司 | COD (COD) removes mixture of powders |
| CN108996808A (en) * | 2018-07-02 | 2018-12-14 | 山西太钢不锈钢股份有限公司 | The biochemical combined treatment process and equipment of steel and iron industry concentrated water difficult to degrade |
Non-Patent Citations (3)
| Title |
|---|
| KYRIAKOS MANOLI 等: "Enhanced oxidative transformation of organic contaminants by activation of ferrate(VI):Possible involvement of FeV/FeIV species", 《CHEMICAL ENGINEERING JOURNAL》 * |
| SHAOFANG SUN 等: "The combination of ferrate(VI) and sulfite as a novel advanced oxidation process for enhanced degradation of organic contaminants", 《CHEMICAL ENGINEERING JOURNAL》 * |
| 黄军磊: "高铁酸钾去除新兴有机污染物吲哚美辛的研究", 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑（月刊）》 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111624062A (en) * | 2020-04-13 | 2020-09-04 | 南京曼蕊生物科技有限公司 | Chemical wastewater anti-interference detection pretreatment and COD detection kit |
| CN113087296A (en) * | 2021-04-07 | 2021-07-09 | 江苏瑞恒新材料科技有限公司 | Method for treating nitrochlorobenzene wastewater |
| CN116947266A (en) * | 2023-09-20 | 2023-10-27 | 广东绿日环境科技有限公司 | Treatment process for comprehensive sewage and high-salt wastewater |
| CN116947266B (en) * | 2023-09-20 | 2023-11-24 | 广东绿日环境科技有限公司 | Treatment process for comprehensive sewage and high-salt wastewater |
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