CN112679049A - Method for treating coking wastewater by multistage anaerobic and multistage aerobic series coupling MBR - Google Patents
Method for treating coking wastewater by multistage anaerobic and multistage aerobic series coupling MBR Download PDFInfo
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- 238000004939 coking Methods 0.000 title claims abstract description 55
- 239000002351 wastewater Substances 0.000 title claims abstract description 52
- 238000000034 method Methods 0.000 title claims abstract description 26
- 230000008878 coupling Effects 0.000 title claims abstract description 10
- 238000010168 coupling process Methods 0.000 title claims abstract description 10
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 45
- 239000010865 sewage Substances 0.000 claims abstract description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 15
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 15
- 239000001301 oxygen Substances 0.000 claims abstract description 15
- 238000005273 aeration Methods 0.000 claims abstract description 11
- 229910019142 PO4 Inorganic materials 0.000 claims abstract description 9
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims abstract description 9
- 239000010452 phosphate Substances 0.000 claims abstract description 9
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000000945 filler Substances 0.000 claims abstract description 5
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 5
- 239000011574 phosphorus Substances 0.000 claims abstract description 5
- 239000012528 membrane Substances 0.000 claims description 33
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 14
- 239000007789 gas Substances 0.000 claims description 13
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 8
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- 239000012510 hollow fiber Substances 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 238000006396 nitration reaction Methods 0.000 claims description 5
- 239000002033 PVDF binder Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 238000000108 ultra-filtration Methods 0.000 claims description 4
- 239000011148 porous material Substances 0.000 claims 1
- 239000000126 substance Substances 0.000 abstract description 4
- 231100000331 toxic Toxicity 0.000 abstract description 3
- 230000002588 toxic effect Effects 0.000 abstract description 3
- 231100000419 toxicity Toxicity 0.000 abstract 1
- 230000001988 toxicity Effects 0.000 abstract 1
- 239000012065 filter cake Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- 230000005514 two-phase flow Effects 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 239000002574 poison Substances 0.000 description 2
- 231100000614 poison Toxicity 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 241000108664 Nitrobacteria Species 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 238000010170 biological method Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 150000002825 nitriles Chemical class 0.000 description 1
- -1 nitrogen-containing heterocyclic compounds Chemical class 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 230000010287 polarization Effects 0.000 description 1
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 231100001234 toxic pollutant Toxicity 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
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- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention discloses a method for treating coking wastewater by multistage anaerobic and multistage aerobic tandem coupling MBR, which comprises the steps of introducing pretreated coking wastewater into a water inlet tank, adding phosphate, and enabling the total phosphorus concentration to be 0.4-0.6 mg/L; then, multistage anaerobic equipment, multistage aerobic equipment and an MBR system which are connected in series are sequentially introduced, and can be discharged after being treated by the MBR system. The aerobic equipment and the anaerobic equipment are both of a closed structure, fixed fillers are arranged in the aerobic equipment and the anaerobic equipment, and the aerobic equipment at the head end is connected with an aeration system; a sewage backflow system is arranged between the water outlet end of the tail aerobic equipment and the water inlet end of the head anaerobic equipment, and a sewage backflow system is arranged between the concentrated water outlet end of the MBR system and the water inlet end of the head anaerobic equipment. The invention can solve the problem that the effluent index is unstable due to the toxicity of toxic and harmful substances in the coking wastewater to organisms in the biochemical treatment process; the utilization rate of the aerobic section oxygen is improved, the processing time is saved, and the occupied area is reduced.
Description
Technical Field
The invention relates to the technical field of coking wastewater treatment, in particular to a method for treating coking wastewater by coupling multistage anaerobic and multistage aerobic tandem MBR.
Background
The coking wastewater is mainly derived from high-concentration organic wastewater generated in the coking and coke oven gas purification processes. At present, typical treatment methods of coking wastewater of domestic and foreign coking plants mainly adopt biological methods, including an A/O method, an A2/O method, an A/O/O method, an A2/O2 method and the like, and the effluent index of the coking wastewater after biochemical treatment can reach COD<300mg/L，NH3-N<25mg/L, and can reach the standard of discharge or recycling through advanced treatment such as a membrane bioreactor, electrolysis and the like.
Pollutants in the coking wastewater comprise phenols, cyanides, sulfides, polycyclic aromatic hydrocarbons, nitrogen-containing heterocyclic compounds and the like, all belong to toxic pollutants, can inhibit or even poison biochemical treatment organisms, influence the biochemical reaction and cause unstable effluent indexes. In addition, the problems of long retention time of an aerobic section, large occupied area and the like generally exist in the conventional coking wastewater treatment process, and the main reason is that toxic and harmful pollutants in the coking wastewater have a strong inhibition effect on nitrobacteria and need to consume more oxygen to complete nitration reaction. The prior art mainly adopts an enlarged aerobic tank to prolong the retention time of the aerobic tank, if the oxygen utilization rate of an aerobic section can be effectively improved, the hydraulic retention time of the aerobic section can be saved, and the sewage treatment efficiency is improved.
Disclosure of Invention
The invention provides a method for treating coking wastewater by multistage anaerobic and multistage aerobic series coupling MBR, aiming at solving the problem that the effluent index is unstable due to the toxic and harmful substances in the coking wastewater poison the organisms in the biochemical treatment process; the utilization rate of the aerobic section oxygen is improved, the processing time is saved, and the occupied area is reduced.
In order to achieve the purpose, the invention is realized by adopting the following technical scheme.
A method for treating coking wastewater by multistage anaerobic and multistage aerobic series coupling MBR (membrane bioreactor) comprises the steps of introducing pretreated coking wastewater into a water inlet tank, and adding phosphate to ensure that the total phosphorus concentration is 0.4-0.6 mg/L; then sequentially introducing multistage anaerobic equipment, multistage aerobic equipment and an MBR system which are connected in series, and discharging after being treated by the MBR system; the number ratio of anaerobic equipment in the multi-stage anaerobic equipment to aerobic equipment in the multi-stage aerobic equipment is 3:2, the aerobic equipment and the anaerobic equipment are both in a closed structure, fixed fillers are arranged in the aerobic equipment and each aerobic equipment is connected with an aeration system; a sewage backflow system is arranged between the water outlet end of the tail aerobic equipment and the water inlet end of the head anaerobic equipment, and a sewage backflow system is arranged between the concentrated water outlet end of the MBR system and the water inlet end of the head anaerobic equipment.
The coking wastewater added with the phosphate enters a multi-stage anaerobic device to carry out denitrification reaction, the temperature of the multi-stage anaerobic device is controlled to be 32-35 ℃, the dissolved oxygen is less than or equal to 0.2mg/L, and the coking wastewater stays in the multi-stage anaerobic device for 30-45 hours.
The coking wastewater treated by the multistage anaerobic equipment enters the multistage aerobic equipment to carry out nitration reaction, and the temperature of the multistage aerobic equipment is controlled to be 25-28 ℃; continuously aerating the aerobic equipment by an aeration pump to keep dissolved oxygen at 6-8 mg/L; the coking wastewater stays in a multi-stage aerobic device for 20-30 hours; and part of the effluent of the multi-stage aerobic equipment flows back to the water inlet end of the first anaerobic equipment of the multi-stage anaerobic equipment through a backflow system, and the ratio of the backflow amount to the water inlet amount of the multi-stage aerobic or anaerobic equipment is 2-3: 1.
Mixing tail gas of the multistage aerobic equipment and effluent of the multistage aerobic equipment, allowing the mixture to enter an MBR system, controlling the pressure of the MBR system to be 0.1-0.2 Mpa, and staying for 1-2 h; clear water obtained by MBR treatment is discharged, the obtained sewage flows back to the water inlet end of the first anaerobic equipment of the multistage anaerobic equipment, and tail gas is discharged from the concentration end of the MBR system.
The ultrafiltration membrane component of the MBR system adopts a hollow fiber membrane made of PVDF (polyvinylidene fluoride), and the membrane aperture is 0.1 mm.
The pretreated coking wastewater has COD concentration of 3000-5500 mg/L, ammonia nitrogen concentration of 40-50 mg/L, total nitrogen concentration of 100-120 mg/L, volatile phenol concentration of 20-50 mg/L and pH of 8.5-9.5.
Clear water obtained by MBR treatment has COD concentration of less than 200mg/L, ammonia nitrogen concentration of less than 25mg/L, total nitrogen concentration of less than 50mg/L, volatile phenol concentration of less than 0.3mg/L and pH of 7.1-7.3.
The tail gas of the multistage aerobic equipment and the effluent of the multistage aerobic equipment are mixed and enter the MBR system, so that the membrane can be washed, and the membrane pollution is reduced. And when the transmembrane pressure is more than 30kPa, performing physical cleaning and chemical cleaning on the membrane.
Compared with the prior art, the invention has the beneficial effects that:
(1) by adopting the multi-stage anaerobic equipment and the sewage reflux system between the multi-stage anaerobic equipment and the multi-stage aerobic equipment, the coking wastewater can fully carry out denitrification reaction, and the removal of ammonia nitrogen in the coking wastewater is promoted; the carbon source in the coking wastewater is fully utilized, no additional carbon source is required to be provided, and the operation cost is reduced.
(2) The aerobic equipment and the anaerobic equipment are both closed containers, and certain pressure can be generated in the equipment in the operation process, so that the dissolved oxygen in water can be effectively increased, and the oxygen utilization rate is improved.
(3) By using the MBR system to carry out advanced treatment on the coking wastewater, the chemical oxygen demand of the effluent can be effectively reduced, microorganisms and particulate matters in the effluent are intercepted, the turbidity of the effluent is improved, meanwhile, the accumulation and growth of microorganisms with longer growth period are facilitated, and the impact load resistance of organisms is improved.
(4) The tail gas of the aerobic equipment enters the MBR system along with the effluent to form gas-liquid two-phase flow, different flow states of the gas-liquid two-phase flow can be changed by adjusting aeration quantity, the shearing force on the surface of the membrane is improved, the formation of a filter cake layer on the surface of the membrane and the phenomenon of concentration difference polarization are reduced, the membrane pollution is reduced, the operation period of the membrane is prolonged, and the service life of the membrane is prolonged.
(5) The hollow fiber membrane is beneficial to gas-liquid two-phase flow formed by sewage and tail gas, and the sewage and the tail gas scour the inner wall of the hollow fiber membrane in the operation process, so that turbulence is formed on the surface of the membrane, and the formation of a filter cake layer is inhibited. The existing membrane directly filters sewage, and the stable water flow can cause sludge in the sewage to be accumulated on the surface of the membrane to form a filter cake layer, so that the membrane pollution is accelerated, and the service cycle of the membrane component is shortened.
Drawings
FIG. 1 is a process flow diagram of a method for treating coking wastewater by multistage anaerobic and multistage aerobic series coupling MBR.
Detailed Description
The following describes embodiments of the present invention with reference to the drawings.
The coking wastewater in the embodiment of the invention is pretreated by a conventional method.
A method for treating coking wastewater by multistage anaerobic and multistage aerobic series coupling MBR (membrane bioreactor) comprises the steps of introducing pretreated coking wastewater into a water inlet tank, and adding phosphate to ensure that the total phosphorus concentration is 0.4-0.6 mg/L; then sequentially introducing multistage anaerobic equipment, multistage aerobic equipment and an MBR system which are connected in series, and discharging after being treated by the MBR system; the number ratio of anaerobic equipment in the multi-stage anaerobic equipment to aerobic equipment in the multi-stage aerobic equipment is 3:2, the aerobic equipment and the anaerobic equipment are both in a closed structure, fixed fillers are arranged in the aerobic equipment and each aerobic equipment is connected with an aeration system; a sewage backflow system is arranged between the water outlet end of the tail aerobic equipment and the water inlet end of the head anaerobic equipment, and a sewage backflow system is arranged between the concentrated water outlet end of the MBR system and the water inlet end of the head anaerobic equipment.
The coking wastewater added with the phosphate enters a multi-stage anaerobic device to carry out denitrification reaction, the temperature of the multi-stage anaerobic device is controlled to be 32-35 ℃, the dissolved oxygen is less than or equal to 0.2mg/L, and the coking wastewater stays in the multi-stage anaerobic device for 30-45 hours.
The coking wastewater treated by the multistage anaerobic equipment enters the multistage aerobic equipment to carry out nitration reaction, and the temperature of the multistage aerobic equipment is controlled to be 25-28 ℃; continuously aerating the aerobic equipment by an aeration pump to keep dissolved oxygen at 6-8 mg/L; the coking wastewater stays in a multi-stage aerobic device for 20-30 hours; and part of the effluent of the multi-stage aerobic equipment flows back to the water inlet end of the first anaerobic equipment of the multi-stage anaerobic equipment through a backflow system, and the ratio of the backflow amount to the water inlet amount of the multi-stage aerobic or anaerobic equipment is 2-3: 1.
Mixing tail gas of the multistage aerobic equipment and effluent of the multistage aerobic equipment, allowing the mixture to enter an MBR system, controlling the pressure of the MBR system to be 0.1-0.2 Mpa, and staying for 1-2 h; clear water obtained by MBR treatment is discharged, the obtained sewage flows back to the water inlet end of the first anaerobic equipment of the multistage anaerobic equipment, and tail gas is discharged from the concentration end of the MBR system.
The ultrafiltration membrane component of the MBR system adopts a hollow fiber membrane made of PVDF (polyvinylidene fluoride), and the membrane aperture is 0.1 mm.
The pretreated coking wastewater has COD concentration of 3000-5500 mg/L, ammonia nitrogen concentration of 40-50 mg/L, total nitrogen concentration of 100-120 mg/L, volatile phenol concentration of 20-50 mg/L and pH of 8.5-9.5.
Clear water obtained by MBR treatment has COD concentration of less than 200mg/L, ammonia nitrogen concentration of less than 25mg/L, total nitrogen concentration of less than 50mg/L, volatile phenol concentration of less than 0.3mg/L and pH of 7.1-7.3.
[ examples ] A method for producing a compound
The pretreated coking wastewater has a COD concentration of 4500-5500 mg/L, an ammonia nitrogen concentration of 40-50 mg/L, a total nitrogen concentration of 100-120 mg/L, a volatile phenol concentration of 20-50 mg/L and a pH of 8.5-9.5. It was processed according to the process flow of fig. 1.
Introducing the pretreated coking wastewater into a water inlet pool, and adding phosphate to ensure that the total phosphorus concentration is 0.4-0.6 mg/L; then sequentially introducing multistage anaerobic equipment, multistage aerobic equipment and an MBR system which are connected in series, and discharging after being treated by the MBR system; the number ratio of anaerobic equipment in the multi-stage anaerobic equipment to aerobic equipment in the multi-stage aerobic equipment is 3:2(6 anaerobic equipment with the volume of 36L and 4 aerobic equipment with the volume of 24L), the aerobic equipment and the anaerobic equipment are both of a closed structure, fixed fillers are arranged in the aerobic equipment and the anaerobic equipment, and each aerobic equipment is connected with an aeration system; a sewage backflow system is arranged between the water outlet end of the tail aerobic equipment and the water inlet end of the head anaerobic equipment, and a sewage backflow system is arranged between the concentrated water outlet end of the MBR system and the water inlet end of the head anaerobic equipment.
The coking wastewater added with the phosphate enters a multi-stage anaerobic device to carry out denitrification reaction, the temperature of the multi-stage anaerobic device is controlled to be 32-35 ℃, the dissolved oxygen is less than or equal to 0.2mg/L, and the coking wastewater stays in the multi-stage anaerobic device for 43 hours.
Coking wastewater treated by the multistage anaerobic equipment enters the multistage aerobic equipment to carry out nitration reaction, and the temperature of the multistage aerobic equipment is controlled to be 25 ℃; continuously aerating the aerobic equipment by an aeration pump (the aeration amount is 20L/h) to keep the dissolved oxygen at 6-8 mg/L; the coking wastewater stays in a multi-stage aerobic device for 29 hours; and part of the effluent of the multi-stage aerobic equipment flows back to the water inlet end of the first anaerobic equipment of the multi-stage anaerobic equipment through a backflow system, and the ratio of the backflow amount to the water inlet amount of the multi-stage aerobic or anaerobic equipment is 3: 1.
Mixing tail gas of the multistage aerobic equipment and effluent of the multistage aerobic equipment, allowing the mixture to enter an MBR system, controlling the pressure of the MBR system to be 0.1-0.2 Mpa, and staying for 1 h; clear water obtained by MBR treatment is discharged, the obtained sewage flows back to the head end of the multistage anaerobic equipment, and tail gas is discharged from the concentration end of the MBR system.
The ultrafiltration membrane component of the MBR system adopts a hollow fiber membrane made of PVDF (polyvinylidene fluoride), and the membrane aperture is 0.1 mm.
Clear water obtained by MBR treatment has COD concentration of less than 200mg/L, ammonia nitrogen concentration of less than 25mg/L, total nitrogen concentration of less than 50mg/L, volatile phenol concentration of less than 0.3mg/L and pH of 7.1-7.3.
The above description is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any idea or transformation proposed by those skilled in the art within the technical scope of the present invention is within the scope of the present invention.
Claims (6)
1. A method for treating coking wastewater by multistage anaerobic and multistage aerobic series coupling MBR is characterized in that pretreated coking wastewater is introduced into a water inlet tank and added with phosphate, so that the total phosphorus concentration is 0.4-0.6 mg/L; then sequentially introducing multistage anaerobic equipment, multistage aerobic equipment and an MBR system which are connected in series, and discharging after being treated by the MBR system; the number ratio of anaerobic equipment in the multistage anaerobic equipment to aerobic equipment in the multistage aerobic equipment is 3:2, the aerobic equipment and the anaerobic equipment are both in a closed structure, fixed fillers are arranged in the aerobic equipment and the aerobic equipment at the head end is connected with an aeration system; a sewage backflow system is arranged between the water outlet end of the tail aerobic equipment and the water inlet end of the head anaerobic equipment, and a sewage backflow system is arranged between the concentrated water outlet end of the MBR system and the water inlet end of the head anaerobic equipment.
2. The method for treating the coking wastewater by the multistage anaerobic and multistage aerobic series coupled MBR (membrane bioreactor) according to claim 1, wherein the coking wastewater after phosphate addition enters a multistage anaerobic device to perform denitrification reaction, the temperature of the multistage anaerobic device is controlled to be 32-35 ℃, the dissolved oxygen is less than or equal to 0.2mg/L, and the coking wastewater stays in the multistage anaerobic device for 30-45 hours.
3. The method for treating the coking wastewater by the multistage anaerobic and multistage aerobic series coupled MBR (membrane bioreactor) according to claim 1, wherein the coking wastewater treated by the multistage anaerobic equipment enters the multistage aerobic equipment for nitration reaction, and the temperature of the multistage aerobic equipment is controlled to be 25-28 ℃; continuously aerating the aerobic equipment by an aeration pump to keep dissolved oxygen at 6-8 mg/L; the coking wastewater stays in a multi-stage aerobic device for 20-30 hours; and part of the effluent of the multi-stage aerobic equipment flows back to the water inlet end of the first anaerobic equipment of the multi-stage anaerobic equipment through a backflow system, and the ratio of the backflow amount to the water inlet amount of the multi-stage aerobic or anaerobic equipment is 2-3: 1.
4. The method for treating the coking wastewater by the multistage anaerobic and multistage aerobic series coupled MBR (membrane bioreactor) according to claim 1, wherein tail gas of the multistage aerobic device and effluent of the multistage aerobic device are mixed and enter an MBR system, the pressure of the MBR system is controlled to be 0.1-0.2 Mpa, and the mixture stays for 1-2 hours; clear water obtained by MBR treatment is discharged, the obtained sewage flows back to the water inlet end of the first anaerobic equipment of the multistage anaerobic equipment, and tail gas is discharged from the concentration end of the MBR system.
5. The method for treating the coking wastewater by the multistage anaerobic and multistage aerobic tandem coupled MBR, according to claim 4, wherein an ultrafiltration membrane module of the MBR system adopts a hollow fiber membrane made of PVDF (polyvinylidene fluoride) and has a membrane pore size of 0.1 mm.
6. The method for treating the coking wastewater by the multistage anaerobic and multistage aerobic tandem coupling MBR, according to claim 1, wherein the pretreated coking wastewater has a COD concentration of 3000-5500 mg/L, an ammonia nitrogen concentration of 40-50 mg/L, a total nitrogen concentration of 100-120 mg/L, a volatile phenol concentration of 20-50 mg/L, and a pH of 8.5-9.5.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1289730A (en) * | 2000-10-25 | 2001-04-04 | 大连理工大学 | Anaerobic-aerobic process for treating sewage by biochemical reactor with vertical baffling |
| CN107344798A (en) * | 2016-05-06 | 2017-11-14 | 上海宝钢化工有限公司 | A kind of apparatus for treating carbonized waste water and its processing method |
| CN110759593A (en) * | 2019-11-06 | 2020-02-07 | 中冶焦耐(大连)工程技术有限公司 | Process for treating coking wastewater by multistage A/O (anoxic/oxic) through sectional water inflow |
| KR20200042273A (en) * | 2018-10-15 | 2020-04-23 | 주식회사 에코니티 | Membrane combined Advanced wastewater treatment system which applies Trisectional aeration and Changed inflow course and it's operation methods |
-
2020
- 2020-12-30 CN CN202011625448.4A patent/CN112679049A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1289730A (en) * | 2000-10-25 | 2001-04-04 | 大连理工大学 | Anaerobic-aerobic process for treating sewage by biochemical reactor with vertical baffling |
| CN107344798A (en) * | 2016-05-06 | 2017-11-14 | 上海宝钢化工有限公司 | A kind of apparatus for treating carbonized waste water and its processing method |
| KR20200042273A (en) * | 2018-10-15 | 2020-04-23 | 주식회사 에코니티 | Membrane combined Advanced wastewater treatment system which applies Trisectional aeration and Changed inflow course and it's operation methods |
| CN110759593A (en) * | 2019-11-06 | 2020-02-07 | 中冶焦耐(大连)工程技术有限公司 | Process for treating coking wastewater by multistage A/O (anoxic/oxic) through sectional water inflow |
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| Title |
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| 大连市史志办公室编: "《大连市志 环境保护志》", 31 May 2003, 大连理工大学出版社 * |
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Application publication date: 20210420 |