CN110759594A - Process method for efficiently treating coking wastewater by coupling A/O (anaerobic/oxic) with MBBR (moving bed biofilm reactor) - Google Patents
Process method for efficiently treating coking wastewater by coupling A/O (anaerobic/oxic) with MBBR (moving bed biofilm reactor) Download PDFInfo
- Publication number
- CN110759594A CN110759594A CN201911073895.0A CN201911073895A CN110759594A CN 110759594 A CN110759594 A CN 110759594A CN 201911073895 A CN201911073895 A CN 201911073895A CN 110759594 A CN110759594 A CN 110759594A
- Authority
- CN
- China
- Prior art keywords
- tank
- mbbr
- coking wastewater
- sedimentation tank
- sludge
- 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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
-
- 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
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
-
- 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
- C02F2001/007—Processes including a sedimentation step
Abstract
The invention relates to a process method for efficiently treating coking wastewater by coupling A/O (anaerobic/oxic) with MBBR (moving bed biofilm reactor), wherein the pretreated coking wastewater is sequentially treated by an A tank, an O tank, a primary sedimentation tank, an MBBR tank and a secondary sedimentation tank; a fixed filler is arranged in the tank A, a supernatant reflux system of the sedimentation tank is arranged between the tank A and the second-stage sedimentation tank, and a sludge reflux system is arranged between the tank O and the first-stage sedimentation tank; suspended fillers are added into the MBBR tank, and a sludge return system is arranged between the MBBR tank and the two-stage sedimentation tank. The invention has the characteristics of small occupied area, strong impact load resistance, stable operation and low operation cost.
Description
Technical Field
The invention relates to the technical field of coking wastewater treatment, in particular to a process method for efficiently treating coking wastewater by coupling A/O (anaerobic/oxic) with MBBR (moving bed biofilm reactor).
Background
The coking wastewater mainly comes from coking, coal gas purification processes and chemical product refining processes, wherein ammonia distillation wastewater generated in the ammonia distillation process is used as a main source. The pollutants contained in the coking wastewater comprise phenols, cyanides, sulfides, polycyclic aromatic hydrocarbons, nitrogen-containing heterocyclic compounds and the like, which belong to typical toxic pollutants and can generate inhibiting and even poisoning effects on the biological treatment of coking wastewater.
At present, typical coking wastewater treatment technologies of domestic and foreign coking plants mainly adopt biological methods, including A/0 (anoxic/aerobic) method, A2-The effluent indexes of the coking wastewater after biological treatment such as an O (anaerobic/anoxic/aerobic) method, an A/O/O (anoxic/aerobic) method, an A2/O2 ((anaerobic/anoxic/aerobic) method and the like can basically reach the COD (chemical oxygen demand) less than 300mg/L and NH (hydrogen peroxide) content3the-N is less than 25mg/L, and the effluent can reach the standard of discharge or reuse after further advanced treatment.
However, the existing biological treatment process of the coking wastewater generally has the problems of long retention time of an aerobic tank, large floor area and unstable effluent index. The main reason is that the coking wastewater contains a large amount of toxic and harmful pollutants for inhibiting the life activities of microorganisms, and the inhibition effect of the pollutants on autotrophic bacteria such as nitrifying bacteria and the like is far greater than that of heterotrophic bacteria mainly for degrading organic matters, so that the retention time of an aerobic tank needs to be prolonged for achieving the purpose of thorough nitration reaction, so as to ensure the reaction time required by a nitration stage, which can lead to larger tank capacity and long retention time (generally 80-100 h); meanwhile, nitrifying bacteria in the aerobic tank are often impacted due to fluctuation of water inflow indexes of the front-end ammonia evaporation wastewater, and the sludge needs to be recovered for a long time after being impacted, so that the fluctuation of water outflow indexes is large.
Disclosure of Invention
The invention provides a process method for efficiently treating coking wastewater by coupling A/O (anaerobic/oxic) with MBBR (moving bed biofilm reactor), which has the characteristics of small occupied area, strong impact load resistance, stable operation and low operation cost.
In order to achieve the purpose, the invention adopts the following technical scheme:
a process method for efficiently treating coking wastewater by coupling A/O with MBBR comprises the steps of sequentially treating the pretreated coking wastewater by an A tank, an O tank, a first-stage sedimentation tank, an MBBR tank and a second-stage sedimentation tank; a fixed filler is arranged in the tank A, a supernatant reflux system of the sedimentation tank is arranged between the tank A and the second-stage sedimentation tank, and a sludge reflux system is arranged between the tank O and the first-stage sedimentation tank; suspended fillers are added into the MBBR tank, and a sludge return system is arranged between the MBBR tank and the two-stage sedimentation tank.
A process method for efficiently treating coking wastewater by coupling A/O with MBBR specifically comprises the following steps:
(1) the pretreated coking wastewater firstly enters an A/O system, wherein a fixed filler is arranged in a pool A; adding phosphorus salt required by the growth of microorganisms into the pool A in the operation process of the system; the O tank adopts an activated sludge method, and dissolved oxygen in the O tank is maintained at 4-6 mg/L through a microporous aerator; the hydraulic retention time of the coking wastewater in the tank A is 25-30 h, and the hydraulic retention time in the tank O is 30-40 h;
(2) the effluent of the O tank enters a first-stage sedimentation tank for mud-water separation, and the surface load of the first-stage sedimentation tank is 1-1.5 m3/m2h, conveying the sludge precipitated to the bottom of the tank back to the O tank through a sludge reflux system, wherein the sludge reflux ratio is controlled to be 50-100%;
(3) the effluent of the first-stage sedimentation tank enters an MBBR tank, and PE tubular filler is added into the MBBR tank, wherein the filling ratio is 20-30%; maintaining the dissolved oxygen in the O tank at 2-4 mg/L by a microporous aerator; adding alkali into the MBBR tank in the system operation process; the coking wastewater stays for 15-20 h in the MBBR tank through water power;
(4) the effluent of the MBBR enters a second-stage sedimentation tank for mud-water separation, and the surface load of the second-stage sedimentation tank is 1-1.5 m3/m2And h, returning the sludge precipitated at the bottom of the pool to the MBBR pool, returning the supernatant to the pool A, controlling the sludge reflux ratio at 50-100% and controlling the supernatant reflux ratio at 200-300%.
The pretreatment of the coking wastewater is to remove heavy oil, emulsified oil and dissolved oil contained in the coking wastewater.
In the step (1), the amount of the phosphate salt added into the pool A is controlled according to the maintenance of the total phosphorus concentration of 0.3-0.5 mg/L in the water.
And (3) adding NaOH as the type of alkali into the MBBR tank, wherein the adding amount is controlled according to the maintenance of the pH value of the water to be 7.5-8.5.
Compared with the prior art, the invention has the beneficial effects that:
(1) the occupied area is reduced, and the construction cost is reduced; on the premise of ensuring the stable effluent index, the total biochemical reaction tank volume is about 1/2 of the tank volume of the prior art by shortening the hydraulic retention time of the aerobic tank, so that the occupied area of the reaction tank is greatly reduced, and the construction cost is reduced;
(2) the stable operation of the biochemical reaction system is facilitated; the coking wastewater inlet indexes are frequently fluctuated, so that nitrobacteria in the aerobic tank are frequently impacted, heterotrophic bacteria mainly used for degrading toxic and harmful substances such as thiocyanide, cyanide, volatile phenol and the like in the O tank at the front end of the split treatment are strong in impact resistance, and after the coking wastewater is degraded in the O tank, the toxic and harmful substances in the water are reduced to be below a threshold concentration, so that the stable operation of the nitrobacteria in the MBBR can be ensured;
(3) the operation cost is reduced; as the nitration reaction has higher requirement on the temperature, the temperature of the reaction tank needs to be maintained at about 20-30 ℃, and the heterotrophic bacteria have wider requirement on the temperature range and can be maintained at more than 10 ℃. In winter in northern cold areas, the waste water in the O tank needs to be heated by steam to ensure the temperature of the waste water in the tank; the invention adopts the A/0+ MBBR technology, the nitration reaction zone is in the MBBR tank, the nitration reaction temperature is maintained in advance, only the waste water is heated by steam in the MBBR tank, the steam usage is greatly reduced, and the operation cost is reduced.
Drawings
FIG. 1 is a flow chart of the process for efficiently treating coking wastewater by coupling A/O with MBBR of the invention.
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in figure 1, the coking wastewater after pretreatment sequentially passes through an A tank, an O tank, a primary sedimentation tank, an MBBR tank and a secondary sedimentation tank for treatment; a fixed filler is arranged in the tank A, a supernatant reflux system of the sedimentation tank is arranged between the tank A and the second-stage sedimentation tank, and a sludge reflux system is arranged between the tank O and the first-stage sedimentation tank; suspended fillers are added into the MBBR tank, and a sludge return system is arranged between the MBBR tank and the two-stage sedimentation tank.
A process method for efficiently treating coking wastewater by coupling A/O with MBBR specifically comprises the following steps:
(1) the pretreated coking wastewater firstly enters an A/O system, wherein a fixed filler is arranged in a pool A; adding phosphorus salt required by the growth of microorganisms into the pool A in the operation process of the system; the O tank adopts an activated sludge method, and dissolved oxygen in the O tank is maintained at 4-6 mg/L through a microporous aerator; the hydraulic retention time of the coking wastewater in the tank A is 25-30 h, and the hydraulic retention time in the tank O is 30-40 h;
(2) the effluent of the O tank enters a first-stage sedimentation tank for mud-water separation, and the surface load of the first-stage sedimentation tank is 1-1.5 m3/m2h, conveying the sludge precipitated to the bottom of the tank back to the O tank through a sludge reflux system, wherein the sludge reflux ratio is controlled to be 50-100%;
(3) the effluent of the first-stage sedimentation tank enters an MBBR tank, and PE tubular filler is added into the MBBR tank, wherein the filling ratio is 20-30%; maintaining the dissolved oxygen in the O tank at 2-4 mg/L by a microporous aerator; adding alkali into the MBBR tank in the system operation process; the coking wastewater stays for 15-20 h in the MBBR tank through water power;
(4) the effluent of the MBBR enters a second-stage sedimentation tank for mud-water separation, and the surface load of the second-stage sedimentation tank is 1-1.5 m3/m2And h, returning the sludge precipitated at the bottom of the pool to the MBBR pool, returning the supernatant to the pool A, controlling the sludge reflux ratio at 50-100% and controlling the supernatant reflux ratio at 200-300%.
The pretreatment of the coking wastewater is to remove heavy oil, emulsified oil and dissolved oil contained in the coking wastewater.
In the step (1), the amount of the phosphate salt added into the pool A is controlled according to the maintenance of the total phosphorus concentration of 0.3-0.5 mg/L in the water.
And (3) adding NaOH as the type of alkali into the MBBR tank, wherein the adding amount is controlled according to the maintenance of the pH value of the water to be 7.5-8.5.
The following examples are carried out on the premise of the technical scheme of the invention, and detailed embodiments and specific operation processes are given, but the scope of the invention is not limited to the following examples. The methods used in the following examples are conventional methods unless otherwise specified.
[ example 1 ]
The quality indexes of the pretreated coking wastewater of a coking wastewater treatment plant in a certain industrial park are as follows: 3500-4500 mg/L of COD, 20-30 mg/L of cyanide, 500-600 mg/L of volatile phenol, 20-30 mg/L of sulfide, 20-50 mg/L of petroleum, 100-150 mg/L of ammonia nitrogen and 7.5-8.5 of pH.
The pretreated coking wastewater firstly enters a first-stage A/O (anoxic/oxic) tank A, is mixed with supernatant liquid refluxed by a second-stage sedimentation tank to perform denitrification reaction, fixed fillers are installed in the tank A, the hydraulic retention time of the tank A is 25 hours, and the dissolved oxygen is controlled to be below 0.5 mg/L.
Next, the coking wastewater enters an O tank of a first-level A/O, a liftable microporous aerator is arranged in the O tank, an activated sludge method is adopted, microorganisms are utilized to carry out biodegradation on toxic and harmful substances such as phenol, cyanide, sulfide, polycyclic aromatic hydrocarbon and the like in the wastewater, the hydraulic retention time of the O tank is 32 hours, the dissolved oxygen is controlled to be 4-6 mg/L, the sludge concentration is 3-4 g/L, and the effluent indexes are as follows: volatile phenol is less than 0.5mg/L, sulfide is less than 0.3mg/L, cyanide is less than 0.3mg/L, and COD is 250-350 mg/L.
The effluent of the O tank enters a first-stage sedimentation tank for mud-water separation, and the surface load of the first-stage sedimentation tank is 1.35m3/m2And h, conveying the sludge precipitated to the bottom of the tank back to the O tank through a sludge reflux system, wherein the reflux ratio is controlled at 100%.
And (3) introducing the effluent of the first-stage sedimentation tank into an MBBR tank, adding PE tubular filler into the MBBR tank at a filling ratio of 20-30%, and installing a lifting microporous aerator in the tank. In the MBBR tank, the dominant flora is nitrobacteria, and because the growth period of the nitrobacteria is long, a large amount of nitrobacteria can be attached to the filler by adding the filler, so that a sufficient amount of nitrobacteria can be ensured in the tank. Nitrification reaction mainly occurs in the MBBR tank, ammonia nitrogen is finally degraded into nitrate nitrogen, alkali is added into the MBBR tank in the operation process, and the pH value is maintained to be 7.5-8.5; maintaining 2-4 mg/L of dissolved oxygen in the O tank, setting the hydraulic retention time of the MBBR tank to be 15h, and setting the effluent indexes to be 150-200 mg/L of COD and less than 3mg/L of ammonia nitrogen.
The effluent of the MBBR tank enters a second-stage sedimentation tank for sludge-water separation, and the surface load of the second-stage sedimentation tank is 1.33m3/m2And h, returning the sludge precipitated to the bottom of the pool to the MBBR pool, returning the supernatant to the pool A, and controlling the return ratio of the sludge to the supernatant to be 50% and 200% respectively.
[ example 2 ]
The water quality index of the pretreated coking wastewater of a certain coking plant is as follows: 6500-7500 mg/L of COD, 30-40 mg/L of cyanide, 700-800 mg/L of volatile phenol, 30-50 mg/L of sulfide, 40-50 mg/L of petroleum, 150-200 mg/L of ammonia nitrogen and 7.5-8.5 of pH.
The pretreated coking wastewater firstly enters a first-stage A/O (anoxic/oxic) tank A, is mixed with supernatant liquid refluxed by a second-stage sedimentation tank to perform denitrification reaction, fixed fillers are installed in the tank A, the hydraulic retention time of the tank A is 30 hours, and the dissolved oxygen is controlled to be below 0.5 mg/L.
Then, the coking wastewater enters a first-level A/O (anaerobic/oxic) tank, a liftable microporous aerator is arranged in the tank, an activated sludge method is adopted, microorganisms are utilized to carry out biodegradation on toxic and harmful substances such as phenol, cyanide, sulfide, polycyclic aromatic hydrocarbon and the like in the wastewater, the hydraulic retention time of the O tank is 40h, the dissolved oxygen is controlled to be 4-6 mg/L, the sludge concentration is 3-4 g/L, and the effluent indexes are as follows: volatile phenol is less than 0.5mg/L, sulfide is less than 0.3mg/L, cyanide is less than 0.3mg/L, and COD is 300-400 mg/L.
The effluent of the O tank enters a first-stage sedimentation tank for mud-water separation, and the surface load of the first-stage sedimentation tank is 1.3m3/m2h, conveying the sludge precipitated to the bottom of the tank back to the O tank through a sludge reflux system, wherein the reflux ratio is controlled at 90%;
the effluent of the first-stage sedimentation tank enters an MBBR tank, PE tubular filler is added into the tank, the filling ratio is 20% -30%, a lifting microporous aerator is installed in the tank, the dominant flora in the MBBR tank is nitrifying bacteria, a large amount of nitrifying bacteria are attached to the filler, the sufficient amount of nitrifying bacteria are ensured to exist in the tank, nitrification reaction mainly occurs in the MBBR tank, ammonia nitrogen is finally degraded into nitrate nitrogen, alkali is added into the MBBR tank in the operation process, and the pH value is maintained to be 7.5-8.5; maintaining 2-4 mg/L of dissolved oxygen in the O tank, wherein the hydraulic retention time of the MBBR tank is 20h, and the effluent indexes are that COD is 150-200 mg/L, and ammonia nitrogen is less than 3 mg/L;
the effluent of the MBBR enters a second-stage sedimentation tank for mud-water separation, and the surface load of the second-stage sedimentation tank is 1.3m3/m2And h, refluxing the sludge precipitated at the bottom of the pool to the MBBR pool, refluxing the overflow liquid to the pool A, and respectively controlling the reflux ratio at 100% and 300%.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (5)
1. A process method for efficiently treating coking wastewater by coupling A/O with MBBR is characterized in that the pretreated coking wastewater sequentially passes through an A tank, an O tank, a primary sedimentation tank, an MBBR tank and a secondary sedimentation tank for treatment; a fixed filler is arranged in the tank A, a supernatant reflux system of the sedimentation tank is arranged between the tank A and the second-stage sedimentation tank, and a sludge reflux system is arranged between the tank O and the first-stage sedimentation tank; suspended fillers are added into the MBBR tank, and a sludge return system is arranged between the MBBR tank and the two-stage sedimentation tank.
2. The process method for efficiently treating coking wastewater by A/O coupling MBBR according to claim 1, which is characterized by comprising the following steps:
(1) the pretreated coking wastewater firstly enters an A/O system, wherein a fixed filler is arranged in a pool A; adding phosphorus salt required by the growth of microorganisms into the pool A in the operation process of the system; the O tank adopts an activated sludge method, and dissolved oxygen in the O tank is maintained at 4-6 mg/L through a microporous aerator; the hydraulic retention time of the coking wastewater in the tank A is 25-30 h, and the hydraulic retention time in the tank O is 30-40 h;
(2) the effluent of the O tank enters a first-stage sedimentation tank for mud-water separation, and the surface load of the first-stage sedimentation tank is 1-1.5 m3/m2h, conveying the sludge precipitated to the bottom of the tank back to the O tank through a sludge reflux system, wherein the sludge reflux ratio is controlled to be 50-100%;
(3) the effluent of the first-stage sedimentation tank enters an MBBR tank, and PE tubular filler is added into the MBBR tank, wherein the filling ratio is 20-30%; maintaining the dissolved oxygen in the O tank at 2-4 mg/L by a microporous aerator; adding alkali into the MBBR tank in the system operation process; the coking wastewater stays for 15-20 h in the MBBR tank through water power;
(4) the MBBR effluent enters a second-stage precipitationCarrying out mud-water separation in the pool, wherein the surface load of the second-stage sedimentation tank is 1-1.5 m3/m2And h, returning the sludge precipitated at the bottom of the pool to the MBBR pool, returning the supernatant to the pool A, controlling the sludge reflux ratio at 50-100% and controlling the supernatant reflux ratio at 200-300%.
3. The process method for efficiently treating the coking wastewater by the A/O coupling MBBR according to claim 1 or 2, wherein the pretreatment of the coking wastewater is to remove heavy oil, emulsified oil and dissolved oil contained in the coking wastewater.
4. The process method for efficiently treating coking wastewater by using the A/O-coupled MBBR according to claim 2, wherein in the step (1), the amount of the added phosphorus salt to the A tank is controlled according to the maintenance of the total phosphorus concentration in the water to be 0.3-0.5 mg/L.
5. The process method for efficiently treating coking wastewater by using the A/O-coupled MBBR according to claim 2, wherein in the step (3), NaOH is added as the type of alkali to the MBBR tank, and the adding amount is controlled according to the maintenance of the pH value of water to be 7.5-8.5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911073895.0A CN110759594A (en) | 2019-11-06 | 2019-11-06 | Process method for efficiently treating coking wastewater by coupling A/O (anaerobic/oxic) with MBBR (moving bed biofilm reactor) |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911073895.0A CN110759594A (en) | 2019-11-06 | 2019-11-06 | Process method for efficiently treating coking wastewater by coupling A/O (anaerobic/oxic) with MBBR (moving bed biofilm reactor) |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110759594A true CN110759594A (en) | 2020-02-07 |
Family
ID=69336493
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911073895.0A Pending CN110759594A (en) | 2019-11-06 | 2019-11-06 | Process method for efficiently treating coking wastewater by coupling A/O (anaerobic/oxic) with MBBR (moving bed biofilm reactor) |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110759594A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111517561A (en) * | 2020-03-31 | 2020-08-11 | 临涣焦化股份有限公司 | Coking chemical product refining wastewater treatment method |
| CN113998848A (en) * | 2021-12-13 | 2022-02-01 | 大连重工环保工程有限公司 | Ammonia distillation, gas water seal, rainwater and sludge filtrate mixed wastewater treatment system and method |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030201225A1 (en) * | 2002-04-30 | 2003-10-30 | Josse Juan Carlos | Organic slurry treatment process |
| CN101514069A (en) * | 2009-04-03 | 2009-08-26 | 北京首钢国际工程技术有限公司 | Coking wastewater biological denitrificaion treatment process |
| CN101602564A (en) * | 2009-07-21 | 2009-12-16 | 南京大学 | A kind of treatment process of coking chemical waste water |
| ES2362298A1 (en) * | 2011-04-26 | 2011-07-01 | Universidade De Santiago De Compostela | Method for eliminating pharmaceutical products from waste water |
| CN103288300A (en) * | 2013-06-18 | 2013-09-11 | 哈尔滨工业大学 | Low-temperature treatment method of A/O/MBBR municipal sewage |
| CN108503141A (en) * | 2018-04-11 | 2018-09-07 | 宝钢工程技术集团有限公司 | A kind of processing method of coking wastewater removing total nitrogen |
-
2019
- 2019-11-06 CN CN201911073895.0A patent/CN110759594A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030201225A1 (en) * | 2002-04-30 | 2003-10-30 | Josse Juan Carlos | Organic slurry treatment process |
| CN101514069A (en) * | 2009-04-03 | 2009-08-26 | 北京首钢国际工程技术有限公司 | Coking wastewater biological denitrificaion treatment process |
| CN101602564A (en) * | 2009-07-21 | 2009-12-16 | 南京大学 | A kind of treatment process of coking chemical waste water |
| ES2362298A1 (en) * | 2011-04-26 | 2011-07-01 | Universidade De Santiago De Compostela | Method for eliminating pharmaceutical products from waste water |
| CN103288300A (en) * | 2013-06-18 | 2013-09-11 | 哈尔滨工业大学 | Low-temperature treatment method of A/O/MBBR municipal sewage |
| CN108503141A (en) * | 2018-04-11 | 2018-09-07 | 宝钢工程技术集团有限公司 | A kind of processing method of coking wastewater removing total nitrogen |
Non-Patent Citations (1)
| Title |
|---|
| 王建兵等编著: "《煤化工高浓度有机废水处理技术及工程实例》", 31 July 2015, 冶金工业出版社 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111517561A (en) * | 2020-03-31 | 2020-08-11 | 临涣焦化股份有限公司 | Coking chemical product refining wastewater treatment method |
| CN113998848A (en) * | 2021-12-13 | 2022-02-01 | 大连重工环保工程有限公司 | Ammonia distillation, gas water seal, rainwater and sludge filtrate mixed wastewater treatment system and method |
| CN113998848B (en) * | 2021-12-13 | 2023-07-14 | 大连重工环保工程有限公司 | Ammonia distillation, gas water seal, rainwater and sludge filtrate mixed wastewater treatment system and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106830324B (en) | Sectional water inlet A2Device and method for enhancing biological nitrogen and phosphorus removal by adopting/O (oxygen/phosphorus) process | |
| CN108946944B (en) | Method for promoting total nitrogen removal of wastewater by short-cut denitrification | |
| CN103508618B (en) | Method for treating high-concentration ammonia nitrogen wastewater | |
| CN110759593A (en) | Process for treating coking wastewater by multistage A/O (anoxic/oxic) through sectional water inflow | |
| CN101514069A (en) | Coking wastewater biological denitrificaion treatment process | |
| CN102874927B (en) | Biological treatment method, biological treatment system and bioreactor of coal chemical wastewater | |
| CN1887740A (en) | Short-path deep biological denitrogenation method for city garbage percolate | |
| CN1778725A (en) | Energy-saving coking waste-water denitrification | |
| CN101428940A (en) | Method for treating carbonized wastewater | |
| CN111072233A (en) | Ion type rare earth ore wastewater treatment device and process | |
| CN103553282A (en) | Deep treatment process of coking wastewater | |
| CN109626739A (en) | A kind of Denitrification of Coking Wastewater method | |
| CN110759594A (en) | Process method for efficiently treating coking wastewater by coupling A/O (anaerobic/oxic) with MBBR (moving bed biofilm reactor) | |
| CN102718370A (en) | Method for treating total nitrogen in coking wastewater by utilizing microorganisms | |
| CN105776749A (en) | Catalytic oxidation combination multi-element biochemical system for electroplating organic wastewater and deep treatment method thereof | |
| KR20020016674A (en) | Advanced Piggery Wastewater Treatment System | |
| CN111747601B (en) | Treatment method of PTA-containing wastewater RO concentrated water | |
| CN103373796A (en) | Method for treating oil refining wastewater | |
| CN111115802A (en) | Efficient culture and domestication method for treating coking wastewater activated sludge | |
| KR20010028550A (en) | Treatment method for livestock waste water including highly concentrated organic, nitrogen and phosphate | |
| KR100632487B1 (en) | Gradually operated sequencing batch reactor and method thereof | |
| CN113998848B (en) | Ammonia distillation, gas water seal, rainwater and sludge filtrate mixed wastewater treatment system and method | |
| CN112960773B (en) | Low C/N domestic sewage deep denitrification method based on normal state addition of oxidized nitrogen | |
| CN104609659A (en) | Method for enhancing denitrification efficiency of coal-chemical engineering wastewater treated with SBR technology | |
| CN113735386A (en) | Coking wastewater bioelectrochemical enhanced treatment system and method |
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 | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200207 |
|
| RJ01 | Rejection of invention patent application after publication |