CN116332395A - Efficient treatment process for industrial park sewage and chemical wastewater - Google Patents
Efficient treatment process for industrial park sewage and chemical wastewater Download PDFInfo
- Publication number
- CN116332395A CN116332395A CN202310141996.7A CN202310141996A CN116332395A CN 116332395 A CN116332395 A CN 116332395A CN 202310141996 A CN202310141996 A CN 202310141996A CN 116332395 A CN116332395 A CN 116332395A
- Authority
- CN
- China
- Prior art keywords
- reactor
- efficient
- wastewater
- fenton
- reaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000002351 wastewater Substances 0.000 title claims abstract description 55
- 238000011282 treatment Methods 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims abstract description 41
- 230000008569 process Effects 0.000 title claims abstract description 40
- 239000010865 sewage Substances 0.000 title claims abstract description 24
- 239000000126 substance Substances 0.000 title claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 238000004062 sedimentation Methods 0.000 claims abstract description 40
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 36
- 230000020477 pH reduction Effects 0.000 claims abstract description 35
- 238000006243 chemical reaction Methods 0.000 claims abstract description 34
- 230000007062 hydrolysis Effects 0.000 claims abstract description 27
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 27
- 239000007800 oxidant agent Substances 0.000 claims abstract description 23
- 230000001590 oxidative effect Effects 0.000 claims abstract description 21
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 claims abstract description 17
- 230000001105 regulatory effect Effects 0.000 claims abstract description 14
- 239000003513 alkali Substances 0.000 claims abstract description 11
- 239000003054 catalyst Substances 0.000 claims abstract description 10
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 9
- 229910052742 iron Inorganic materials 0.000 claims abstract description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 42
- 238000003756 stirring Methods 0.000 claims description 28
- 239000003344 environmental pollutant Substances 0.000 claims description 20
- 231100000719 pollutant Toxicity 0.000 claims description 20
- 230000001112 coagulating effect Effects 0.000 claims description 18
- 230000007246 mechanism Effects 0.000 claims description 16
- 238000001179 sorption measurement Methods 0.000 claims description 15
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 12
- 230000003301 hydrolyzing effect Effects 0.000 claims description 9
- 238000007254 oxidation reaction Methods 0.000 claims description 9
- 230000003647 oxidation Effects 0.000 claims description 8
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 6
- OSVXSBDYLRYLIG-UHFFFAOYSA-N dioxidochlorine(.) Chemical compound O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 claims description 6
- 238000005273 aeration Methods 0.000 claims description 5
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 4
- 239000002957 persistent organic pollutant Substances 0.000 claims description 4
- 239000004155 Chlorine dioxide Substances 0.000 claims description 3
- 239000001569 carbon dioxide Substances 0.000 claims description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 3
- 235000019398 chlorine dioxide Nutrition 0.000 claims description 3
- 239000008394 flocculating agent Substances 0.000 claims description 3
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 claims description 3
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 claims description 3
- 229910006540 α-FeOOH Inorganic materials 0.000 claims description 3
- 229910006299 γ-FeOOH Inorganic materials 0.000 claims description 3
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 2
- 238000006065 biodegradation reaction Methods 0.000 claims description 2
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 19
- 239000002253 acid Substances 0.000 abstract description 9
- 238000000354 decomposition reaction Methods 0.000 abstract description 4
- 150000003839 salts Chemical class 0.000 abstract description 4
- 230000009286 beneficial effect Effects 0.000 abstract description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 18
- 230000000630 rising effect Effects 0.000 description 17
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 16
- 230000009471 action Effects 0.000 description 15
- 229910052799 carbon Inorganic materials 0.000 description 13
- 244000005700 microbiome Species 0.000 description 13
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 12
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 239000000203 mixture Substances 0.000 description 7
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 229910000859 α-Fe Inorganic materials 0.000 description 5
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 4
- 238000007664 blowing Methods 0.000 description 4
- 238000010992 reflux Methods 0.000 description 4
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 3
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 3
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- WQZGKKKJIJFFOK-VFUOTHLCSA-N beta-D-glucose Chemical compound OC[C@H]1O[C@@H](O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-VFUOTHLCSA-N 0.000 description 3
- 239000008103 glucose Substances 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 230000007935 neutral effect Effects 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000001632 sodium acetate Substances 0.000 description 3
- 235000017281 sodium acetate Nutrition 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 238000009423 ventilation Methods 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- 230000000844 anti-bacterial effect Effects 0.000 description 2
- 239000003899 bactericide agent Substances 0.000 description 2
- 230000003851 biochemical process Effects 0.000 description 2
- 239000000701 coagulant Substances 0.000 description 2
- 230000015271 coagulation Effects 0.000 description 2
- 238000005345 coagulation Methods 0.000 description 2
- 239000000356 contaminant Substances 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002071 nanotube Substances 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 239000003929 acidic solution Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 238000009303 advanced oxidation process reaction Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000986 disperse dye Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000003411 electrode reaction Methods 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229910001448 ferrous ion Inorganic materials 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- TUJKJAMUKRIRHC-UHFFFAOYSA-N hydroxyl Chemical compound [OH] TUJKJAMUKRIRHC-UHFFFAOYSA-N 0.000 description 1
- -1 iron ions Chemical class 0.000 description 1
- 238000011369 optimal treatment Methods 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- 239000000985 reactive dye Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000012163 sequencing technique Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Images
Classifications
-
- 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
- C02F3/30—Aerobic and anaerobic processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F33/00—Other mixers; Mixing plants; Combinations of mixers
- B01F33/40—Mixers using gas or liquid agitation, e.g. with air supply tubes
- B01F33/4094—Plants
-
- 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
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
- C02F2101/163—Nitrates
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention discloses a high-efficiency treatment process of industrial park sewage and chemical wastewater, which is characterized in that the pH value of the wastewater is regulated to 3-5 by a pH regulating tank; delivering the wastewater with the pH value regulated to a Fenton reactor; adding an oxidant and a catalyst containing iron into the Fenton reactor; fenton (or Fenton-like) reaction is carried out on the wastewater; conveying the water body after Fenton reaction to an iron-carbon reactor for internal electrolysis reaction; adding a small amount of alkali liquor into the effluent of the internal electrolysis reaction to adjust the pH to 8.5-9.0, and adding a small amount of flocculant PAM; and (3) delivering the effluent of the primary sedimentation tank into a biochemical system consisting of an ultra-efficient hydrolysis acidification reactor, an efficient SBR reactor and the like for decomposition. Compared with the prior art, the pretreatment process adopted by the invention has the advantages that the acid adding and alkali adding amount is greatly reduced, so that the salt brought into the wastewater by the acid adding and alkali adding is also greatly reduced, the influence of the salt on subsequent biochemistry is greatly reduced, and the biochemical system is beneficial to exerting the optimal removal effect.
Description
Technical Field
The invention relates to the technical field of water treatment, in particular to an efficient treatment process for industrial park sewage or chemical wastewater, which can also be used for pretreatment before partial reclaimed water recycling project membrane and other water suitable for treatment by the process.
Background
The existing industrial park sewage treatment plants and chemical wastewater treatment stations generally adopt: regulating tank, pretreatment, primary sedimentation tank, hydrolytic acidification, A/OA/O, secondary sedimentation tank, post-treatment and discharge.
The pretreatment generally adopts coagulating sedimentation or iron carbon and Fenton, and the post-treatment generally adopts coagulating sedimentation (or air floatation), ozone catalytic oxidation, a biological filter (or activated carbon adsorption regeneration), a filter and the like.
Wastewater received by industrial park sewage treatment plants is generally subjected to biochemical treatment of various factories in the park, most of pollutants which are easy to be biodegraded are removed, and most of wastewater discharged to industrial park sewage treatment plants is poor in biodegradability. The sewage treatment plants in the early industrial parks are mainly biochemical treatment, so that most of the sewage treatment plants can not reach the emission standard regulated by the environmental protection department. Improvements are now made, such as: pretreatment and post-treatment are added. The pretreatment generally adopts coagulating sedimentation or iron carbon + Fenton. Because coagulating sedimentation only can remove part of SS (suspended solids), the molecular structure of pollutants cannot be changed fundamentally, and refractory organic matters cannot be converted into easily degradable organic matters, so that the pretreatment effect is poor. Although the effect of the pretreatment process of iron carbon + Fenton + precipitation is improved compared with that of the simple coagulation precipitation pretreatment, the pH of the wastewater is required to be adjusted to 3-5 before the wastewater enters the iron carbon, the pH of the wastewater can be increased to 5-7.5 after the iron carbon is reacted, the wastewater enters a Fenton reactor and is required to be adjusted to 3-5 by adding acid for the second time (if the pH is not adjusted, the treatment efficiency is low), the pH is rarely increased after the Fenton reaction, and more alkali is required to be added to adjust the pH to alkalescence (8.5-9), so that divalent iron ions can be completely precipitated, and the influence on subsequent biochemistry is avoided. The whole process needs to add acid twice and more alkali, so that the operation cost is high, the salinity of the wastewater is increased more, and the subsequent biochemical or discharged water recycling is adversely affected. Meanwhile, more oxidant (commonly used hydrogen peroxide) is needed to be added in Fenton reaction, and sometimes the reaction and decomposition are not completed. The oxidant which is not completely reacted and decomposed is also a bactericide, directly enters a biochemical system in the prior art, is very unfavorable for subsequent biochemical treatment, kills partial microorganisms in a biochemical pond and reduces biochemical efficiency. The existing biochemical treatment process generally adopts a hydrolysis acidification-A/OA/O-secondary sedimentation tank process, the original degradation efficiency of waste water with poor biodegradability is low, and the overall removal efficiency is lower due to the double effects of pretreatment salinity and oxidant, so that the COD index of biochemical effluent is often higher, and the subsequent treatment is under great pressure. Therefore, the improvement is made by us, and an efficient treatment process for sewage in an industrial park is provided.
Chemical wastewater is produced by a chemical production process, and the biodegradability of the wastewater is not high, and the biochemical removal rate is not high. And even cannot be directly biochemically treated. The treatment process generally used is similar to that of industrial park sewage.
Disclosure of Invention
In order to solve the technical problems, the invention provides the following technical scheme: comprises the steps of,
the invention relates to a high-efficiency treatment process for industrial park sewage and chemical wastewater,
step 5, sending supernatant fluid from the primary sedimentation tank into a biochemical system consisting of an ultra-efficient hydrolysis acidification reactor, an efficient SBR (sequencing batch reactor) or an efficient A/O or A/O coupling MBR reactor for decomposition;
and 6, if the treatment of the high-efficiency biochemical system cannot completely reach the discharge standard, the post treatment of the biochemical tail water can be performed. The post-treatment adopts coagulating sedimentation and activated carbon adsorption.
As a preferable technical scheme of the invention, the oxidant is one or more of hydrogen peroxide, ozone, sodium hypochlorite, chlorine dioxide and the like.
As a preferable technical scheme of the invention, the catalyst is Fe 0 Magnetite, gamma-FeOOH, alpha-FeOOH, fe 5 HO 8 One or more of the following.
As a preferable technical scheme of the invention, the ultra-efficient hydrolysis acidification reactor comprises a reactor main body, wherein a high-efficient buoyancy stirring mechanism is arranged in the reactor main body and comprises a vent pipe, a large bubble generator and a fan, the vent pipe is arranged in the reactor main body, and the air outlet end of the fan is connected with the air inlet end of the vent pipe through the air pipe.
As a preferred embodiment of the present invention, the vent pipe extends into the reactor body.
As a preferable technical scheme of the invention, the bottom of the ventilation pipe is provided with a large bubble generator.
As an optimal technical scheme of the invention, the high-efficiency buoyancy stirring mechanisms (2) can be flexibly arranged into a plurality of high-efficiency buoyancy stirring mechanisms according to the size of the tank volume.
As a preferable technical scheme of the invention, the air pipe is provided with a control valve.
The beneficial effects of the invention are as follows:
1. the pretreatment process adopted by the industrial park sewage high-efficiency treatment process comprises the following steps: fenton+iron carbon+precipitation, only the PH is required to be adjusted to 3-5 times, and the addition amount of acid is reduced by 50%. Meanwhile, the PH naturally rises to be neutral or close to neutral after the iron and carbon are processed, and the alkali solution amount required for adjusting the PH to be 8.5-9.0 is reduced by 30-70% compared with the prior art. Therefore, the cost of adding the medicament is greatly reduced.
2. Compared with the prior art, the pretreatment process adopted by the industrial park sewage high-efficiency treatment process has the advantages that the acid adding and alkali adding amount is greatly reduced, so that the salt brought into the sewage by the acid adding and alkali adding is also greatly reduced, the influence of the salt on subsequent biochemistry is greatly reduced, and the biochemical system is beneficial to exerting the optimal treatment effect.
3. The industrial park sewage high-efficiency treatment process can further generate Fenton-like reaction on ferrous iron generated by the reaction of oxidizing agents such as hydrogen peroxide and the like which are not fully reacted in the Fenton stage, zero-valent iron in an iron-carbon reactor (reaction tank) and iron-carbon in the iron-carbon stage, and is equivalent to the Fenton-like advanced oxidation reaction which is generated more than the prior art. Therefore, the pretreatment efficiency is higher than that of the prior art with the same addition amount of the oxidant. Meanwhile, as the oxidizing agents such as hydrogen peroxide and the like which are not completely reacted in the Fenton stage further react and decompose in the iron-carbon stage, the amount of the oxidizing agents contained in the wastewater entering the biochemical stage can be ensured to be minimized, so that the influence of the oxidizing agents on the biochemistry is minimized, and the maximum efficiency of a biochemical system, particularly a first unit (such as a hydrolytic acidification tank or an anoxic tank) of the biochemistry is ensured to be exerted.
4. In the industrial park sewage high-efficiency treatment process, a specific super-efficient hydrolysis acidification reactor is arranged, the density of air is far smaller than that of water, and large buoyancy is generated in the water, but viscous force exists around bubbles, the smaller the bubbles are, the larger the corresponding surface area is, the larger the viscous force is, and the rising speed is slow. The larger the bubble, the smaller the corresponding surface area, the smaller the viscous force, and the faster the rising speed, thereby driving the surrounding liquid to rise rapidly. And as long as the bubble is bulged from high-efficient agitating unit, the subsequent rising process of bubble need not additionally to provide energy, and the bubble can rely on self buoyancy to rise fast, therefore very energy-conserving. The high-efficiency buoyancy stirring mechanism adopted by the ultra-efficient hydrolysis acidification reactor provided by the invention is used for stirring by utilizing the large bubbles, and the rapid rising of the large bubbles drives the mud-water mixture around the bubbles to rapidly rise from the bottom of the tank to the top of the tank; and simultaneously, an appropriate amount of oxygen is transferred into the water of the reactor to control the ORP of the reactor to operate in a better range, so that the hydrolysis acidification reactor operates at higher reaction efficiency. Meanwhile, the design can avoid the anaerobic state of the reactor by blowing air into the reactor with a proper amount, thereby avoiding the generation of methane and eliminating the potential safety hazard caused by the methane.
Drawings
The accompanying drawings are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate the invention and together with the embodiments of the invention, serve to explain the invention. In the drawings:
FIG. 1 is a schematic flow chart of an efficient industrial park sewage treatment process according to the invention;
FIG. 2 is a schematic structural diagram of an ultra-efficient hydrolytic acidification reactor according to the present invention.
In the figure: 1. a reactor body; 2. a high-efficiency buoyancy stirring mechanism; 3. a vent pipe; 4. a blower; 5. an air duct; 6. a large bubble generator; 7. and a control valve.
Detailed Description
The preferred embodiments of the present invention will be described below with reference to the accompanying drawings, it being understood that the preferred embodiments described herein are for illustration and explanation of the present invention only, and are not intended to limit the present invention.
Examples: as shown in fig. 1, the invention relates to a high-efficiency treatment process for industrial park sewage, which comprises the following steps,
wherein the Fenton/Fenton-like effluent PH is still weak acid, and can directly enter an iron-carbon reactor (pool) to carry out internal electrolytic reaction. Iron forms a tiny galvanic cell with carbon in an electrolyte-containing solution, and the following electrode reactions occur:
anode (Fe) 2Fe 2 + +4e
Cathode (C) 4H + +4e→4[H]→2H 2 (acidic solution)
O 2 +2H 2 O+4e→4OH- (alkaline and neutral solution)
Removal of organic contaminants can be accomplished by O 2 Enhancing galvanic corrosion to produce a large amount of Fe 2+ 、Fe 3+ 、Fe(OH) 2 、Fe(OH) 3 . Nascent F e 2+ 、[H]Reducing the oxidizing groups in the organic material (e.g. -NO 2 ) To convert it into readily biodegradable groups (e.g. -NH. Sub. 2 ) The pollutant is Fe (OH) 2 、Fe(OH) 3 Adsorbed, forming flocs. At the same time, the iron-carbon potential difference causes colloidal contaminants to be rapidly electrodeposited. Dissolved Fe 3+ H 2 O and O 2 A series of extremely complex chemical reactions are carried out to produce a variety of ferrites. Some ferrite will envelop pollutant molecules during the formation process, and some ferrite pairs in nascent stateThe colloidal pollutant has good flocculation effect, and the ferrite is an excellent adsorbent to adsorb and remove pollutant molecules in water. The invention can further generate Fenton-like reaction on the oxidizing agent such as hydrogen peroxide which is not completely reacted in the Fenton stage, ferrous iron generated by the reaction of zero-valent iron and iron carbon in the iron-carbon reactor, ferrite and the like, and is equivalent to the Fenton-like reaction which is generated once more than the prior art, so that the pretreatment efficiency is higher than the prior art.
and step 5, delivering the effluent of the primary sedimentation tank into a high-efficiency biochemical system for decomposition.
The design high-efficiency biochemical system adopts an ultra-efficient hydrolysis acidification reactor and an efficient A/O (or an efficient SBR or A/O coupling MBR) and a secondary sedimentation tank process (SBR and MBR do not need a secondary sedimentation tank) combined process. Because the oxidant added in the pretreatment stage is fully decomposed, the influence of redundant oxidant (also a bactericide) is avoided in the biochemical treatment stage, and the normal function can be realized. The wastewater enters an ultra-efficient hydrolysis acidification reactor from a primary sedimentation tank, under the action of hydrolysis acidification microorganisms and an efficient stirring device, the pollutants undergo hydrolysis and acidification reactions, macromolecular organic matters and nondegradable organic matters are converted into micromolecular easily-degradable organic matters, and part of organic matters are converted into organic acids which are extremely easy to biochemically produce. The ultra-efficient hydrolysis acidification reactor has excellent mass transfer effect, and the pollutant removal rate is greatly improved compared with the existing hydrolysis acidification reactor, and the removal rate can be generally improved to 1.5-10 times by taking COD as an example. The water discharged from the hydrolysis acidification reactor enters a denitrification reactor A, and denitrification reaction is carried out under the action of denitrification microorganisms and carbon sources (degradable organic matters in wastewater or easily degradable organic matters added independently) to obtain NO 3 -、NO 2 Conversion to N 2 Realizes complete denitrification and reduces TN (total nitrogen) index. The wastewater then enters an aerobic reactor, and the pollutants are further degraded under the action of aerobic microorganisms and are converted into CO 2 And water to mineralize and transform ammonia nitrogen intoNO 3 - And NO 2 - . Thereby realizing the reduction of indexes such as COD, BOD, ammonia nitrogen and the like. The secondary sedimentation tank is provided with a reflux pump which can generate NO 3 - And NO 2 - Biological denitrification is carried out under the action of denitrifying bacteria by refluxing to the denitrification reactor, and TN (total nitrogen) index is reduced. If SBR technology is adopted, NO generated in the SBR aerobic aeration stage 3 - And NO 2 - Then enters an anoxic denitrification stage, and organic matters in the inlet water can be used as carbon sources, or organic matters which are easy to be utilized by microorganisms (such as domestic sewage, glucose, methanol, sodium acetate and the like) are independently added as carbon sources, and denitrification reaction is carried out under the action of denitrifying microorganisms and the carbon sources to obtain NO 3 - 、NO 2 - Conversion to N 2 Realizes complete denitrification and reduces TN (total nitrogen) index.
After biochemical treatment, various pollutant indexes of the wastewater are greatly reduced, most indexes can reach the emission standard, but if the residual part of organic matters which are difficult to degrade (or can not degrade) cause COD indexes to exceed the emission standard, the wastewater needs to be subjected to post-treatment. Because the invention adopts the high-efficiency pretreatment and high-efficiency biochemical process, even if the COD of biochemical effluent exceeds the discharge standard, the COD value is greatly reduced compared with the biochemical effluent index of the traditional process, thus the post-treatment process is simplified compared with the prior art, the investment and the operation cost are lower, generally, only the coagulation sedimentation and the activated carbon adsorption (or advanced oxidation) +the filter (or filter tank) are adopted, the consumption of the activated carbon or the oxidant is greatly reduced compared with the prior art, the equipment specification can be reduced by 1-2 grades, and the operation cost and the investment cost are greatly reduced. Post-treatment process: the biochemical effluent enters a coagulating sedimentation tank after being precipitated in a secondary sedimentation tank, and the concentration of organic pollutants in the wastewater is further reduced through the actions of electric neutralization, adsorption, bridging and the like by adding coagulant and flocculant, so that the COD value is reduced. If the coagulating sedimentation effluent does not reach the standard yet, the coagulating sedimentation effluent enters an activated carbon adsorption tank, and organic matters in the wastewater are further removed through the adsorption action of activated carbon, so that the COD is ensured to reach the standard for emission. For a few wastewater with poor activated carbon adsorption effect, an advanced oxidation reactor can be adopted after coagulating sedimentation, and organic matters are further oxidized and decomposed under the action of an oxidant and a catalyst, so that the COD is ensured to reach the emission standard.
The ultra-efficient hydrolytic acidification reactor as shown in fig. 2 comprises a reactor main body 1, wherein a high-efficiency buoyancy stirring mechanism 2 is arranged in the reactor main body 1, and comprises a vent pipe 3 and a large bubble generator 6. And the ventilation pipe 3 is arranged in the reactor main body 1, and the air outlet end of the fan 4 is connected with the air inlet end of the ventilation pipe 3 through an air pipe 5. The setting of the high-efficiency buoyancy stirring mechanism can greatly improve the stirring effect and the mass transfer effect of the hydrolysis acidification reactor. The invention uses the density of air to be far less than that of water, and generates great buoyancy in water, but the viscous force exists around the bubbles, the finer the bubbles are, the larger the corresponding specific surface area is, the larger the viscous force is, and the lower the rising speed is. The larger the bubble is, the smaller the corresponding specific surface area is, the smaller the viscous force is, and the faster the rising speed is, so that the surrounding liquid is driven to rise rapidly. And, as long as the bubble bulges, the subsequent rising process of the bubble does not need to provide extra energy, and the bubble can quickly rise by depending on own buoyancy, so that the energy is saved. The high-efficiency buoyancy stirring mechanism 2 of the invention utilizes the large bubbles to stir, the rapid rising of the large bubbles drives the mud-water mixture around the bubbles, namely the mixture of microorganisms and water, to rapidly rise from the bottom of the tank to the top of the tank, the boundary water flow speed can reach 5-20 times of that of a submersible stirrer and a mechanical stirrer, the stirring mass transfer effect is excellent, the pollutant removal efficiency is greatly increased, and the general COD removal rate can be increased to 1.5-10 times. The arrows in fig. 2 indicate the direction in which the slurry-water mixture flows.
The ORP value of the reactor has a certain influence on the efficiency of the hydrolysis acidification reactor, and when bubbles are blown into the reactor to stir, oxygen can be properly transferred into the water of the reactor to control the ORP of the reactor to operate in a better range, so that the hydrolysis acidification reactor operates at higher reaction efficiency. Meanwhile, the design can avoid the anaerobic state of the reactor by blowing air into the reactor with a proper amount, thereby avoiding the generation of methane and eliminating the potential safety hazard caused by the methane.
The vent pipe 3 extends into the reactor body 1.
The bottom of the vent pipe 3 is provided with a large bubble generator 6. The large bubble generator 6 has large bubble specification, high rising flow rate and large boundary flow rate, thereby having good stirring and mass transfer effects.
The ventilating pipe 3 can be provided with a plurality of ventilating pipes for stirring in multiple directions and multiple areas.
The air pipe 5 is provided with a control valve 7 which is easy to control the air inflow.
The invention designs a high-efficiency, green and low-carbon stirring device, which can greatly improve the stirring effect and the mass transfer effect of a hydrolysis acidification reactor, and is high-efficiency and energy-saving. The stirring device designed by the invention only consumes 1/2 to 1/20 of the power consumption of the submersible stirrer and the mechanical stirrer.
The hydrolysis acidification reactor designed by the invention can avoid the anaerobic state of the reactor, avoid the generation of methane and eliminate the potential safety hazard caused by the methane by blowing air in a proper amount.
The hydrolysis acidification reactor designed by the invention has excellent mass transfer effect, so that the pollutant removal efficiency is greatly improved, and the COD removal rate can be generally improved to 1.5-10 times under the same conditions. Taking a mixed wastewater of a disperse dye and a reactive dye as an example, the removal rate of hydrolytic acidification COD can reach 60 percent (the vast majority of the existing hydrolytic acidification reactors only have 5 to 10 percent). The fan can adopt: roots blower, centrifugal blower, rotary blower, ring blower, air compressor, etc., and one of them is selected. According to the specific wastewater property, the high-efficiency biological carrier, the high-efficiency microorganism or the biological enzyme can be added into the high-efficiency hydrolysis acidification reactor, so that the efficiency of the hydrolysis acidification reactor is further improved.
Working principle: the density of air is far less than that of water, so that a large buoyancy force is generated in the water, but the viscous force exists around the bubbles, the smaller the bubbles are, the larger the corresponding specific surface area is, the larger the viscous force is, and the rising speed is slow. The larger the bubble is, the smaller the corresponding specific surface area is, the smaller the viscous force is, and the faster the rising speed is, so that the surrounding liquid is driven to rise rapidly. And, as long as the bubble bulges, the subsequent rising process of the bubble does not need to provide extra energy, and the bubble can quickly rise by depending on own buoyancy, so that the energy is saved. The rapid rising of the air bubbles drives the mud-water mixture around the air bubbles, namely the mixture of microorganisms and water, to rapidly rise from the bottom of the tank to the top of the tank, the boundary water flow speed can reach 5-20 times that of a submersible mixer and a mechanical mixer, the stirring mass transfer effect is excellent, the pollutant removal efficiency is greatly improved, and the general COD removal rate can be improved to 1.5-10 times.
The high-efficiency buoyancy stirring mechanisms can be flexibly arranged into a plurality of high-efficiency buoyancy stirring mechanisms according to the size of the tank volume. .
The reactor works in such a way that air is supplied to the high-efficiency buoyancy stirring mechanism 2 through the air pipe 5 by the fan 4, and large bubbles are generated through the large bubble generator of the high-efficiency buoyancy stirring mechanism. The method comprises the steps of carrying out a first treatment on the surface of the The density of air is far less than that of water, so that a great buoyancy force is generated in the water, but the viscous force exists around the bubbles, the finer the bubbles are, the larger the corresponding surface area is, the larger the viscous force is, and the rising speed is slow. The larger the bubble, the smaller the corresponding surface area, the smaller the viscous force, and the faster the rising speed, thereby driving the surrounding liquid to rise rapidly. And as long as the bubble is bulged from high-efficient agitating unit, the subsequent rising process of bubble need not additionally to provide energy, and the bubble can rely on self buoyancy to rise fast, therefore very energy-conserving. The rapid rising of the bubbles drives the mud-water mixture around the bubbles to rapidly rise from the bottom of the tank to the top of the tank; and simultaneously, an appropriate amount of oxygen is transferred into the water of the reactor to control the ORP of the reactor to operate in a better range, so that the hydrolysis acidification reactor operates at higher reaction efficiency. Meanwhile, the design can avoid the anaerobic state of the reactor by blowing air into the reactor with a proper amount, thereby avoiding the generation of methane and eliminating the potential safety hazard caused by the methane.
The water discharged from the ultra-efficient hydrolysis acidification reactor enters the high-efficient denitrification reactor A or the SBR reactor, and the high-efficient SBR reactor and the high-efficient denitrification reactor are respectively provided with a high-efficiency buoyancy stirring mechanism, so that the mass transfer effect is excellent. The anoxic water inlet stage of the high-efficiency denitrification reactor A or the SBR reactor is utilized to carry out high efficiencyBiological denitrification reaction is carried out under the action of denitrifying microorganism and carbon source (degradable organic matters in wastewater or independently adding easily degradable organic matters), and NO is generated 3 - 、NO 2 - Conversion to N 2 Realizes complete denitrification and reduces TN (total nitrogen) index.
After denitrification reaction is completed, the wastewater enters an aerobic aeration stage of an aerobic tank O or SBR, and pollutants are further degraded under the action of aerobic microorganisms and converted into CO 2 And water to mineralize and convert ammonia nitrogen into NO 3 - And NO 2 - . Thereby realizing the reduction of indexes such as COD, BOD, ammonia nitrogen and the like.
The aerobic tank O or the secondary sedimentation tank is provided with a reflux pump to generate NO in the section O 3 - And NO 2 - Biological denitrification is carried out under the action of denitrifying bacteria by refluxing to the A-stage high-efficiency denitrification reactor, and TN (total nitrogen) index is reduced. If SBR technology is adopted, NO generated in the SBR aerobic aeration stage 3 - And NO 2 - Then enters an anoxic denitrification stage, residual organic matters in water can be used as a carbon source, organic matters which are easy to be utilized by microorganisms (such as methanol, ethanol, glucose, methanol, sodium acetate and the like) can be additionally added into the carbon source, and denitrification reaction is carried out under the action of denitrifying microorganisms and the carbon source, so that NO is obtained 3 - 、NO 2 - Conversion to N 2 Realizes complete denitrification and reduces TN (total nitrogen) index.
If the total nitrogen index of the aerobic O effluent can not reach the standard, a section of denitrification reactor A can be connected behind the aerobic reactor 2 And adding an easily degradable organic substance as a carbon source (such as methanol, ethanol, sodium acetate, glucose and the like), further removing total nitrogen, and ensuring that the total nitrogen reaches the standard.
If all the indexes of the effluent of the aerobic reactor or the SBR reactor reach the standards, the effluent can be directly discharged.
After biochemical treatment, various pollutant indexes of the wastewater are greatly reduced, most indexes can reach the emission standard, and still part of organic matters which cannot be biodegraded can be remained. If the COD index exceeds the emission standard due to the residual undegradable organic matters, the post-treatment is needed. Because the invention adopts the high-efficiency pretreatment and high-efficiency biochemical process, even if the COD of biochemical effluent exceeds the discharge standard, the COD value is greatly reduced compared with the biochemical effluent index of the traditional process, thus the post-treatment process can be simplified compared with the prior art, the investment and the operation cost are lower, generally only the coagulating sedimentation and the activated carbon adsorption (or the advanced oxidation) are adopted, the consumption of the activated carbon or the oxidant is greatly reduced compared with the prior art, the equipment specification can be reduced by 1-2 grades, and the operation cost and the investment cost are greatly reduced.
Post-treatment process: the biochemical effluent is precipitated in a secondary sedimentation tank and then enters a coagulating sedimentation tank, and the concentration of pollutants in the wastewater is further reduced through the actions of electric neutralization, adsorption, bridging and the like by adding coagulant and flocculant, so that the indexes such as COD value and the like are reduced. If the coagulating sedimentation effluent does not reach the standard yet, the coagulating sedimentation effluent enters an activated carbon adsorption tank, various pollutants in the water are further removed through the adsorption action of activated carbon, and the COD is ensured to reach the standard for emission. For a few wastewater with poor activated carbon adsorption effect, an advanced oxidation process can be adopted after coagulating sedimentation, and organic matters are further oxidized and decomposed under the action of an oxidant and a catalyst, so that the COD is ensured to reach the emission standard. And (3) allowing the wastewater after activated carbon adsorption (or advanced oxidation) to enter a filter (or a filter tank) to further remove indexes such as suspended matters.
The water after biochemical treatment can ensure that various indexes are discharged up to standard or enter a membrane treatment system for recycling.
The treatment process is also suitable for treating toxic, harmful and nondegradable chemical wastewater, can remove the toxicity of pollutants by pretreatment Fenton+ internal electrolysis, improves the biodegradability of the wastewater, and then enters a high-efficiency biochemical system for biodegradation. If the biochemical effluent reaches the standard, the biochemical effluent can be directly discharged or the nano tube can be subjected to biochemical post-treatment if the biochemical effluent does not reach the standard. The biochemical post-treatment can adopt coagulating sedimentation, or coagulating sedimentation and activated carbon adsorption, or coagulating sedimentation and advanced oxidation, so that the standard discharge of wastewater or a nano tube can be ensured.
Finally, it should be noted that: the above is only a preferred embodiment of the present invention, and the present invention is not limited thereto, but it is to be understood that the present invention is described in detail with reference to the foregoing embodiments, and modifications and equivalents of some of the technical features described in the foregoing embodiments may be made by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. An efficient treatment process for industrial park sewage and chemical wastewater is characterized by comprising the following steps of: comprises the steps of,
step 1, regulating the pH value of the wastewater by a pH regulating tank to 3-5;
step 2, conveying the wastewater with the pH value regulated to a Fenton reactor; adding an oxidant and a catalyst containing iron into the Fenton reactor; the wastewater is subjected to Fenton (or Fenton-like) reaction, so that organic pollutants are decomposed into micromolecular organic matters or are partially mineralized into carbon dioxide and water;
step 3, conveying the water after Fenton reaction to an iron-carbon reactor for internal electrolysis reaction; and a large amount of Fe is produced 2+ Reducing the oxidizing groups in the wastewater, and simultaneously, enabling pollutants to be subjected to Fe (OH) 2 、Fe(OH) 3 Adsorbing to form flocs;
step 4, adding a small amount of alkali liquor into the effluent of the internal electrolysis reaction to adjust the pH to 8.5-9.0, adding a flocculating agent PAM, and sending the flocs and suspended matters in the wastewater into a primary sedimentation tank together for sedimentation and removal;
step 5, delivering the effluent of the primary sedimentation tank into a biochemical treatment system consisting of an ultra-efficient hydrolysis acidification reactor and a high-efficient SBR reactor (or a high-efficient A/O reactor and a secondary sedimentation tank or a high-efficient A/O and MBR) for biodegradation;
and step 6, if the treated biochemical effluent can not completely reach the discharge standard, the biochemical effluent can be subjected to post-treatment, and the post-treatment adopts coagulating sedimentation and activated carbon adsorption (or advanced oxidation).
2. The efficient treatment process for industrial park sewage and chemical wastewater according to claim 1, wherein the oxidant is one or more of hydrogen peroxide, ozone, sodium hypochlorite and chlorine dioxide.
3. The efficient industrial park sewage treatment process according to claim 1, wherein the catalyst is Fe 2+ 、Fe 3+ 、Fe 0 Magnetite, gamma-FeOOH, alpha-FeOOH, fe 5 HO 8 One or more of the following.
4. The efficient industrial park sewage treatment process according to claim 1, wherein the ultra-efficient hydrolysis acidification reactor comprises a reactor main body (1), a high-efficiency buoyancy stirring mechanism (2) is arranged in the reactor main body (1), the high-efficiency buoyancy stirring mechanism (2) comprises a vent pipe (3), a large bubble generator (6) and a fan (4), the vent pipe (3) and the large bubble generator (6) are arranged in the reactor main body (1), and an air outlet end of the fan (4) is connected with an air inlet end of the vent pipe (3) through an air pipe (5).
5. An ultra efficient hydrolytic acidification reactor as claimed in claim 4, characterised in that said aeration pipe (3) extends into the interior of the reactor body (1).
6. An ultra-efficient hydrolytic acidification reactor as claimed in claim 4, characterised in that the bottom of said aeration pipe (3) is provided with a large bubble generator (6).
7. An ultra-efficient hydrolysis acidification reactor according to claim 4, wherein said high-efficient buoyancy stirring mechanism (2) is flexibly arranged in a plurality according to the size of the tank volume.
8. An ultra-efficient hydrolytic acidification reactor as claimed in claim 4, characterised in that a control valve (7) is arranged on said air duct (5).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310067434 | 2023-02-06 | ||
| CN2023100674342 | 2023-02-06 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116332395A true CN116332395A (en) | 2023-06-27 |
Family
ID=86884876
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310141979.3A Pending CN116639804A (en) | 2023-02-06 | 2023-02-20 | High-efficiency denitrification reactor |
| CN202310141996.7A Pending CN116332395A (en) | 2023-02-06 | 2023-02-20 | Efficient treatment process for industrial park sewage and chemical wastewater |
Family Applications Before (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310141979.3A Pending CN116639804A (en) | 2023-02-06 | 2023-02-20 | High-efficiency denitrification reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (2) | CN116639804A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2024164503A1 (en) * | 2023-02-06 | 2024-08-15 | 上海天誉环境科技工程有限公司 | Ultra-efficient hydrolytic acidification reactor and high-performance buoyancy stirring mechanism thereof |
-
2023
- 2023-02-20 CN CN202310141979.3A patent/CN116639804A/en active Pending
- 2023-02-20 CN CN202310141996.7A patent/CN116332395A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2024164503A1 (en) * | 2023-02-06 | 2024-08-15 | 上海天誉环境科技工程有限公司 | Ultra-efficient hydrolytic acidification reactor and high-performance buoyancy stirring mechanism thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN116639804A (en) | 2023-08-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104609658B (en) | A kind of catalyzed internal electrocatalysis-improvement BAF processes the method for reverse osmosis concentrated water | |
| CN109205954A (en) | Light electrolysis catalysis oxidation, biochemical treatment high-concentration waste hydraulic art | |
| CN105174632A (en) | Device and method for treating ship sewage through ultrasonic strengthening internal electrolysis coupling biological method | |
| CN111268872A (en) | Pesticide wastewater treatment process and treatment device thereof | |
| CN112551744A (en) | Method for treating wastewater by utilizing acidic coagulated Fenton oxidation | |
| CN103787544B (en) | Process the system of DCP waste water | |
| CN111747600A (en) | Ozone oxidation-biochemical coupling water treatment method | |
| CN116332395A (en) | Efficient treatment process for industrial park sewage and chemical wastewater | |
| CN113955899A (en) | Efficient paint production wastewater treatment system and process | |
| CN212222737U (en) | Pesticide effluent treatment plant | |
| CN111410376B (en) | Catalytic hydrolysis pretreatment method for industrial park wastewater | |
| CN117142685A (en) | Landfill leachate treatment process | |
| CN103787545B (en) | The method processing DCP waste water | |
| CN216005557U (en) | Integrated treatment system for high-ammonia-nitrogen wastewater difficult to biodegrade | |
| CN113184972B (en) | Method for removing organic pollutants in wastewater by sequencing batch reaction | |
| CN214244099U (en) | High concentration organic wastewater treatment system | |
| CN112759196B (en) | Treatment process of esterification wastewater | |
| CN116119888A (en) | Combined treatment system and treatment method for post-concentration liquid of landfill leachate membrane | |
| CN214004362U (en) | Quick purification treatment system of waste water | |
| CN212403799U (en) | LAS effluent disposal system to high concentration high salt | |
| CN212222726U (en) | Landfill leachate treatment system | |
| CN203187488U (en) | System for treating DCP (dicalcium phosphate) wastewater | |
| CN220098801U (en) | Treatment system of refractory industrial wastewater | |
| CN215403702U (en) | Ozone coupling device for treating high-organic-matter high-ammonia-nitrogen wastewater | |
| CN112408707A (en) | Medical intermediate wastewater treatment process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |