CN105923855A - Treatment process and system of chromium plating wastewater and application of treatment process and system - Google Patents
Treatment process and system of chromium plating wastewater and application of treatment process and system Download PDFInfo
- Publication number
- CN105923855A CN105923855A CN201610441197.1A CN201610441197A CN105923855A CN 105923855 A CN105923855 A CN 105923855A CN 201610441197 A CN201610441197 A CN 201610441197A CN 105923855 A CN105923855 A CN 105923855A
- Authority
- CN
- China
- Prior art keywords
- outlet
- flocculation
- water outlet
- micro
- coagulation
- 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
Classifications
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
-
- 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
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention discloses treatment process of chromium plating wastewater. The treatment process is characterized in that the wastewater is regulated to be acid, microsphere absorption deoiling is performed, then the wastewater is fed into a Fe-C microelectrolysis reactor to reduce Cr<6+> into Cr<3+>, coagulation reaction is performed on the discharged water to remove surfactant, flocculation precipitation is performed on the water discharged after the coagulation, the pH of the discharged water is regulated to be alkaline, further flocculation precipitation is performed, and the supernate which is obtained finally and meets the standards is discharged. The treatment process has the advantages that the problem that the wastewater containing chromium and especially the complex chromium plating wastewater containing oil and the surfactant are hard to treat is solved, and the whole treatment system is low in energy consumption, low in operation cost, low in sludge amount and suitable for being popularized; microsphere absorption resin can be regenerated thoroughly, and generated Fe3+ can be utilized to remove the surfactant in the wastewater through coagulation while the Cr<6+> is reduced into the Cr<3+>.
Description
Technical field
The invention belongs to Sewage advanced treatment field, particularly relate to process technique, processing system and the application thereof of a kind of chromium plating wastewater.
Background technology
Chromium plating wastewater is acidity, chromium ion is mainly presented in Cr (VI), Cr (VI) toxicity is bigger, there is after being not only absorbed by the body the carcinogenic and danger of modificator gene sudden change, and chromium plating wastewater severe contamination water source, soil, destroying ecological environment, therefore GB8978 1996 " integrated wastewater discharge standard ", the highest permission concentration of emission strictly limiting Cr (VI) is 0.5 mg/L.
For the conventional treatment method of this type of waste water, mainly include ion exchange and electrolysis.Wherein, ion exchange can reach discharge standard, and effluent quality is preferable, typically can recycle.But the once investment of ion exchange processing waste water containing chrome is higher, operation management requires strict, is often not good at due to operation management and does not reaches expected effect in production run；For electrolytic reduction, although have that volume is little, take up an area less, power consumption is low, convenient management, the feature such as effective, but its iron plate consumption is more, is mixed with substantial amounts of hydrated ferric oxide. in mud, and value is low, need to deal carefully with.
It addition, electroplating wastewater is possibly together with oils and surfactant, such as stearic acid, dodecylbenzene sodium sulfonate etc. in actual production, it is mainly reflected in COD, needs to be removed before discharge.Minimizing technology for surfactant is more, but all defects of various degrees, as: foamet is applicable to the separation in the case of low concentration, but the COD clearance of foamet Surfactant waste water is the highest, needs to be used in combination with additive method；Membrane separation process efficiency is high, energy consumption is little, but film easily pollutes, and cleans difficulty, and operating cost is high；Although Coagulation Method processing cost is low, technical maturity, but its floor space is big, dosing is big, and produce a large amount of waste residue and mud, often processing method with other to be used in combination and can be only achieved the purpose removed completely, generally as the pretreatment of process concentrated surfactant waste water；Catalytic oxidation processing cost is high；Anaerobic digestion processes waste water can avoid producing substantial amounts of foam, but surfactant can produce a certain degree of suppression to anaerobic treatment process；Biological oxidation process can directly process the surface active agent wastewater of meta-alkalescence, assists other treatment technologies can obtain more preferable effect during process；Absorption method advantage is that speed is fast, good stability, equipment take up an area little, major defect be invest higher, adsorbent reactivation is difficult, pre-processing requirements is higher.
Therefore, for above-mentioned situation, inventor sums up forefathers' experience and considers practical problem, develops process technique and the processing system thereof of a kind of chromium plating wastewater, and this processing system can be widely applied to chromium plating wastewater process field, has a good application prospect.
Summary of the invention
For the problems referred to above, the invention provides process technique, processing system and the application of a kind of chromium plating wastewater, this technique contains the particularity of chromium, oil and surfactant according to chromium plating wastewater, comprehensive utilization microsphere absorption, Fe-C micro-electrolysis reaction and flocculent precipitation achieve the removal of chromium, oil and surfactant, the supernatant qualified discharge finally given, the adsorbent resin of native system is renewable thoroughly, and at reduction Cr6+For Cr3+While, it is also with the Fe generated3+Being removed by surfactant coagulation in waste water, whole system energy consumption is little, operating cost is low, sludge quantity is few, and suitable process is promoted.
For reaching this purpose, the present invention by the following technical solutions:
The process technique of a kind of chromium plating wastewater, is first adjusted to acidity by described waste water, enters Fe-C micro-electrolysis reactor by Cr after utilizing microsphere absorption removing oil6+It is reduced to Cr3+, then water outlet is carried out coagulating removal surfactant, water outlet pH is adjusted to alkalescence flocculation sediment, the supernatant qualified discharge finally given further by coagulation water outlet again after carrying out flocculation sediment.
First described wastewater pH is adjusted to 3 ~ 5, then enters microballoon adsorbing column removing oil, oil content ＜ 3mg/L in absorption water outlet with the flow velocity of 2 ~ 5BV/h.
Described Fe-C micro-electrolysis reactor is by Cr6+It is reduced to Cr3+Gas-liquid volume ratio be 3:1, Inlet and outlet water flow velocity is 1-2BV/h.
The Fe that described coagulating produces with Fe-C micro-electrolysis reaction3+Salt or Fe (OH)3For coagulant, the coagulating time is 1-3h.
Adding polymeric ferrous sulphate solution in coagulation water outlet and carry out flocculation sediment, the flocculation sediment time is 1-2 hour, obtains water outlet of flocculating.
Adding sodium hydroxide solution in flocculation water outlet and pH is adjusted to 8 ~ 9, carry out flocculation sediment with bodied ferric sulfate for flocculant, the response time of flocculation sediment is 1 ~ 2h, Cr < 0.01mg/L, COD < 50mg/L, qualified discharge in supernatant water outlet.
A kind of processing system realizing technique described in the claims, including the first pH regulator groove, microballoon adsorbing column, Fe-C micro-electrolysis reactor and precipitation unit；The outlet of described first pH regulator groove is connected with the entrance of described microballoon adsorbing column, and the outlet of described microballoon adsorbing column is connected with the entrance of described Fe-C micro-electrolysis reactor, and the outlet of described Fe-C micro-electrolysis reactor is connected with described precipitation unit.
Described precipitation unit also includes coagulation tank, the first flocculation tank, the second pH regulator groove and the second flocculation tank, the outlet of described coagulation tank is connected with described first flocculation tank entrance, the outlet of described first flocculation tank is connected with described second pH regulator groove entrance, and described second pH regulator groove is connected with described second flocculation tank.
The purposes of a kind of such as above-mentioned Waste Water Treatment, it is applied to chromium plating wastewater process field.
Compared with prior art, the method have the advantages that
1) the invention discloses the processing method of a kind of chromium plating wastewater, the method have effectively achieved the qualified discharge containing chromium, oil and surface active agent wastewater；
2) present system is widely portable to containing chromium, oil and surface active agent wastewater process field；
3) in present system, microballoon adsorbing column is renewable thoroughly, and at reduction Cr6+For Cr3+While, it is also with the Fe generated3+Being removed by surfactant coagulation in waste water, whole system energy consumption is little, operating cost is low, sludge quantity is few, and suitable process is promoted.
Accompanying drawing explanation
Fig. 1 is that the present invention contains the processing system of inorganic ammonium salt waste water and processes the flow chart of technique.
In figure: 1-the first pH regulator groove；2-microballoon adsorbing column；3-Fe-C micro-electrolysis reactor；4-coagulation tank；5-the first flocculation tank；6-the second pH regulator groove；7-the second flocculation tank.
Detailed description of the invention
For the present invention is better described, it is simple to understand technical scheme, the typical but non-limiting embodiment of the present invention is as follows:
As it is shown in figure 1, the processing system of a kind of chromium plating wastewater, including the first pH regulator groove 1, microballoon adsorbing column 2, Fe-C micro-electrolysis reactor 3 and precipitation unit；The outlet of pH regulator groove 1 is connected with the entrance of microballoon adsorbing column 2, and the outlet of resin absorbing column 2 is connected with the entrance of Fe-C micro-electrolysis reactor 3, and the outlet of Fe-C micro-electrolysis reactor 3 is connected with precipitation unit.
Precipitation unit also includes coagulation tank the 4, first flocculation tank the 5, second pH regulator groove 6 and the second flocculation tank 7, the outlet of described coagulation tank 4 is connected with the first coagulation tank 5 entrance, the outlet of described first coagulation tank 5 is connected with the second pH regulator groove 6 entrance, and described second pH regulator groove 6 is connected with the second flocculation tank 7.Native system can be widely applied to chromium plating wastewater process field.
A kind of process technique applying above-mentioned processing system to carry out chromium plating wastewater process, is first adjusted to acidity by waste water, enters Fe-C micro-electrolysis reactor by Cr after utilizing microsphere absorption removing oil6+It is reduced to Cr3+, then water outlet is carried out coagulating removing surfactant, coagulation water outlet first obtains, through a flocculation sediment, water outlet of flocculating, further flocculation sediment after flocculation water outlet pH is adjusted to alkalescence, the supernatant qualified discharge finally given.
Wherein, first wastewater pH is adjustable to 3 ~ 5, then enters microballoon adsorbing column removing oil, oil content ＜ 3mg/L in absorption water outlet with the flow velocity of 2 ~ 5BV/h；Fe-C micro-electrolysis reactor is by Cr6+It is reduced to Cr3+Gas-liquid volume ratio be preferably 3:1, Inlet and outlet water flow velocity is both preferably 1-2BV/h；The Fe that coagulating produces with Fe-C micro-electrolysis reaction3+Salt or Fe (OH)3For coagulant, the coagulating time is preferably 1-3h, obtains coagulation water outlet；In coagulation water outlet, add sodium hydroxide solution, carry out flocculation sediment with bodied ferric sulfate for flocculant after pH is adjusted to 8 ~ 9, Cr < 0.01mg/L, COD < 50mg/L, qualified discharge in supernatant water outlet；The response time of flocculation sediment is preferably 1 ~ 2h.
Embodiment 1: certain electroplating enterprise waste water, pH=6, containing Cr (VI) 100mg/L, COD900mg/L.
(1) taking the above-mentioned waste water of 100L, be initially charged sulphuric acid regulation pH=3, then waste water enters microballoon adsorbing column with the flow velocity of 2BV/h and removes oils, adsorbs water outlet oil ＜ 3mg/L；(2) step (1) water outlet enters Fe-C micro-electrolysis reactor by Cr6+It is reduced to Cr3+, produce Fe simultaneously3+, waste water Inlet and outlet water flow velocity is 1BV/h, and gas liquid ratio is 3:1, reacts pH=3；(3) step (2) water outlet pH=3, is introduced into coagulation reaction tank, utilizes the Fe (OH) generated3Coagulation removes surfactant, reacts pH=7, and the coagulating time is 1h.
(4) step (3) water outlet is introduced into the second pH regulator pond addition NaOH and regulates pH=8, and subsequently into flocculation sediment, bodied ferric sulfate addition is 60mg/L, and the flocculation sediment time is 1.Cr ＜ 0.01mg/L, COD ＜ 50mg/L in flocculation sedimentation tank supernatant, qualified discharge, mud carries out subsequent treatment.
Embodiment 2:
Certain electroplating enterprise waste water, pH=8, containing Cr (VI) 180mg/L, COD1000mg/L.(1) taking the above-mentioned waste water of 100L, be initially charged sulphuric acid regulation pH=4, then waste water enters microballoon adsorbing column with the flow velocity of 4BV/h and removes oils, adsorbs water outlet oil ＜ 3mg/L；(2) step (1) water outlet enters Fe-C micro-electrolysis reactor by Cr6+It is reduced to Cr3+, waste water Inlet and outlet water flow velocity is 1.5BV/h, and gas liquid ratio is 3:1, reacts pH=4；(3) step (2) water outlet pH=4, is introduced into coagulation reaction tank and removes surfactant, react pH=7, and the coagulating time is 2h.
(4) step (3) water outlet is introduced into the second pH regulator pond addition NaOH and regulates pH=9, and subsequently into flocculation sediment, bodied ferric sulfate addition is 80mg/L, and the flocculation sediment time is 2h.Cr ＜ 0.01mg/L, COD ＜ 50mg/L in flocculation sedimentation tank supernatant, qualified discharge, mud carries out subsequent treatment.
Embodiment 3:
Certain electroplating enterprise waste water, pH=9, containing Cr (VI) 200mg/L, COD1250mg/L.(1) taking the above-mentioned waste water of 100L, be initially charged sulphuric acid regulation pH=5, then waste water enters microballoon adsorbing column with the flow velocity of 5BV/h and removes oils, adsorbs water outlet oil ＜ 3mg/L；(2) step (1) water outlet enters Fe-C micro-electrolysis reactor by Cr6+It is reduced to Cr3+, waste water Inlet and outlet water flow velocity is 2BV/h, and gas liquid ratio is 3:1, reacts pH=5；(3) step (2) water outlet pH=5, is introduced into coagulation reaction tank and removes surfactant, react pH=6-8, and the coagulating time is 3h.
(4) step (3) water outlet is introduced into the second pH regulator pond addition NaOH and regulates pH=9, and subsequently into flocculation sediment, bodied ferric sulfate addition is 100mg/L, and the flocculation sediment time is 2h.Cr ＜ 0.01mg/L, COD ＜ 50mg/L in flocculation sedimentation tank supernatant, qualified discharge, mud carries out subsequent treatment.
Applicant states, the present invention illustrates the method detailed of the present invention by above-described embodiment, but the invention is not limited in above-mentioned method detailed, does not i.e. mean that the present invention has to rely on above-mentioned method detailed and could implement.Person of ordinary skill in the field is it will be clearly understood that any improvement in the present invention, and the equivalence of raw material each to product of the present invention is replaced and the interpolation of auxiliary element, concrete way choice etc., within the scope of all falling within protection scope of the present invention and disclosure.
Claims (9)
1. the process technique of a chromium plating wastewater, it is characterised in that first described waste water is adjusted to acidity, enters Fe-C micro-electrolysis reactor by Cr after utilizing microsphere absorption removing oil6+It is reduced to Cr3+, then water outlet is carried out coagulating removal surfactant, water outlet pH is adjusted to alkalescence flocculation sediment, the supernatant qualified discharge finally given further by coagulation water outlet again after carrying out flocculation sediment.
Process technique the most as claimed in claim 1, it is characterised in that first described wastewater pH is adjusted to 3 ~ 5, then enters microballoon adsorbing column removing oil, oil content ＜ 3mg/L in absorption water outlet with the flow velocity of 2 ~ 5BV/h.
Process technique the most as claimed in claim 1 or 2, it is characterised in that described Fe-C micro-electrolysis reactor is by Cr6+It is reduced to Cr3+Gas-liquid volume ratio be 3:1, Inlet and outlet water flow velocity is 1-2BV/h.
Process technique the most as claimed in claim 1, it is characterised in that the Fe that described coagulating produces with Fe-C micro-electrolysis reaction3+Salt or Fe (OH)3For coagulant, the coagulating time is 1-3h.
Process technique the most as claimed in claim 4, it is characterised in that adding polymeric ferrous sulphate solution in coagulation water outlet and carry out flocculation sediment, the flocculation sediment time is 1-2 hour, obtains water outlet of flocculating.
Process technique the most as claimed in claim 5, it is characterized in that, in flocculation water outlet, add sodium hydroxide solution pH is adjusted to 8 ~ 9, flocculation sediment is carried out for flocculant with bodied ferric sulfate, the response time of flocculation sediment is 1 ~ 2h, Cr < 0.01mg/L, COD < 50mg/L, qualified discharge in supernatant water outlet.
7. the processing system realizing technique described in the claims, it is characterised in that include the first pH regulator groove, microballoon adsorbing column, Fe-C micro-electrolysis reactor and precipitation unit；The outlet of described first pH regulator groove is connected with the entrance of described microballoon adsorbing column, and the outlet of described microballoon adsorbing column is connected with the entrance of described Fe-C micro-electrolysis reactor, and the outlet of described Fe-C micro-electrolysis reactor is connected with described precipitation unit.
8. processing system as claimed in claim 7, it is characterized in that, described precipitation unit also includes coagulation tank, the first flocculation tank, the second pH regulator groove and the second flocculation tank, the outlet of described coagulation tank is connected with described first flocculation tank entrance, the outlet of described first flocculation tank is connected with described second pH regulator groove entrance, and described second pH regulator groove is connected with described second flocculation tank.
9. a purposes for Waste Water Treatment as claimed in claim 7 or 8, it is applied to chromium plating wastewater process field.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610441197.1A CN105923855A (en) | 2016-06-20 | 2016-06-20 | Treatment process and system of chromium plating wastewater and application of treatment process and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610441197.1A CN105923855A (en) | 2016-06-20 | 2016-06-20 | Treatment process and system of chromium plating wastewater and application of treatment process and system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105923855A true CN105923855A (en) | 2016-09-07 |
Family
ID=56831746
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610441197.1A Pending CN105923855A (en) | 2016-06-20 | 2016-06-20 | Treatment process and system of chromium plating wastewater and application of treatment process and system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105923855A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114804412A (en) * | 2022-04-15 | 2022-07-29 | 桂林电子科技大学 | Treatment process of mixed waste liquid of water quality online monitoring equipment |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104529017A (en) * | 2014-12-10 | 2015-04-22 | 北京市环境保护科学研究院 | Treatment method and treatment device of electroplating mixed water |
| CN104692560A (en) * | 2015-03-03 | 2015-06-10 | 石泰山 | Method for treating phosphorus/phosphine-containing electroplating wastewater |
| CN105601020A (en) * | 2016-03-30 | 2016-05-25 | 北京赛科康仑环保科技有限公司 | Treatment technology of raffinate wastewater of nickel, cobalt and manganese |
-
2016
- 2016-06-20 CN CN201610441197.1A patent/CN105923855A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104529017A (en) * | 2014-12-10 | 2015-04-22 | 北京市环境保护科学研究院 | Treatment method and treatment device of electroplating mixed water |
| CN104692560A (en) * | 2015-03-03 | 2015-06-10 | 石泰山 | Method for treating phosphorus/phosphine-containing electroplating wastewater |
| CN105601020A (en) * | 2016-03-30 | 2016-05-25 | 北京赛科康仑环保科技有限公司 | Treatment technology of raffinate wastewater of nickel, cobalt and manganese |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114804412A (en) * | 2022-04-15 | 2022-07-29 | 桂林电子科技大学 | Treatment process of mixed waste liquid of water quality online monitoring equipment |
| CN114804412B (en) * | 2022-04-15 | 2023-11-10 | 桂林电子科技大学 | Treatment process of mixed waste liquid of water quality on-line monitoring equipment |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102603097B (en) | Advanced treatment and recycling process for wastewater containing heavy metal ions | |
| CN104386874B (en) | A kind of wiring board industry high-concentration waste liquor treating process | |
| CN102765819B (en) | Self-draining water recycling process of water circulating system | |
| CN105502753A (en) | Processing technology for electroplating synthetic wastewater | |
| CN103011347B (en) | Method for carrying out electrolytic treatment on copper-containing electroplating wastewater and recycling copper | |
| CN103922521B (en) | Method used for chrome tanning waste water treatment and chrome recovery | |
| CN105254061A (en) | Treatment method of beneficiation wastewater | |
| CN109721187A (en) | A kind of chemical nickel plating waste solution processing method | |
| CN205740679U (en) | Alumilite process production wastewater treatment and reclaiming system | |
| Abdel Wahaab et al. | Wastewater treatment: a case study of electronics manufacturing industry | |
| WO2017080164A1 (en) | Electroplating waste water processing process | |
| CN106477766A (en) | A kind of waste electroplating liquor containing chromium processing method | |
| CN105800821A (en) | Up-to-standard treatment method and device for zinc-nickel alloy waste water | |
| CN105540958A (en) | Zero-discharge treatment process of power plant wastewater | |
| CN105417860A (en) | Method for processing high-concentration and high-phosphorus wastewater | |
| CN102795722A (en) | Method for treating waste water generated from surface treatment of aluminum products | |
| CN102101734A (en) | Method for pretreating acidic sapogenin wastewater through electrolysis and photoelectrocatalysis | |
| CN106186415A (en) | A kind of phosphorus removing method of the phosphorus-containing wastewater produced in anodic oxidation surface with chemical polishing technology | |
| CN103755089A (en) | Dithiophosphate wastewater pretreatment method | |
| CN103112970A (en) | Heavy metal recovery and zero emission system and process | |
| CN104163529A (en) | Treatment process of zinc-nickel alloy electroplating wastewater | |
| CN104211232A (en) | Method for coal ash and scrap iron combined treatment of dyeing and printing wastewater | |
| CN110818123B (en) | Treatment method of trivalent chromium plating waste water | |
| CN105923855A (en) | Treatment process and system of chromium plating wastewater and application of treatment process and system | |
| CN105923815A (en) | Wastewater purifying and treating method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160907 |
|
| RJ01 | Rejection of invention patent application after publication |