CN104773916A - Chemical engineering wastewater treatment method - Google Patents
Chemical engineering wastewater treatment method Download PDFInfo
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- CN104773916A CN104773916A CN201510150817.1A CN201510150817A CN104773916A CN 104773916 A CN104773916 A CN 104773916A CN 201510150817 A CN201510150817 A CN 201510150817A CN 104773916 A CN104773916 A CN 104773916A
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Abstract
The invention relates to a chemical engineering wastewater treatment method. Chemical engineering wastewater is sequentially processed through a regulation tank, a first-level coagulation reaction tank, a primary sedimentation tank, a sand filtering tank, a first-level ozone oxidation tank, an electro-catalysis reactor, a secondary sedimentation tank, a second-level coagulation reaction tank, a second-level ozone oxidation tank, a primary carbon bioreactor, a third-level ozone oxidation tank, and a secondary carbon bioreactor. Outlet water enters a water storage tank and is discharged, or is used for backwashing the sand filtering tank, the primary carbon bioreactor and the secondary carbon bioreactor. According to the chemical engineering wastewater treatment method provided by the invention, various advantages of coagulation, filtration, oxidation, electro-catalytic reduction, advanced oxidation, physical adsorption and biological treatment are combined. With the treatment, chromaticity and COD in wastewater can be effectively degraded, and chemical engineering wastewater B/C ratio can be improved. After the treatment, water quality related indicators can reach a first-grade B level discharge limitation specified in GB18919-2002. The method has the advantages of high treatment efficiency, low cost, simple operation, easy control, and the like.
Description
Technical field
The present invention relates to a kind for the treatment of process of waste water, be specifically related to a kind for the treatment of process of wastewater from chemical industry, belong to chemical wastewater treatment technical field.
Background technology
Chemicals production process needs to discharge a large amount of wastewater from chemical industry usually.And wastewater from chemical industry water-quality constituents is complicated, water yield change greatly, Pollutants in Wastewater content is high, hazardous and noxious substances is many, as halogen compounds, nitro-compound, the dispersion agent with germicidal action or tensio-active agent etc., chroma in waste water and specific conductivity high, bio-refractory material is many, B/C is low, and biodegradability is poor.Therefore, the difficulty of chemical wastewater treatment is larger.
Current large how many factory adopts materialization (pre-treatment)+biochemical method to process, because pollutent is deliquescent as organic sulfide, phosphide, nitride, and aromatic series, halogenated aromatic.Therefore materialization means clearance is low, and after needing a large amount of cleaning water to carry out being diluted to lower concentration, (10 ~ 50 times) carry out biochemistry again, and the biological non-degradable of some compounds, and biochemical is poor, and bio-chemical effluent is usually not up to standard; Meanwhile, such treatment process makes waste water disposal facility bulky, and cost increases, and working cost increases.At present, a kind of pre-processing device and technique of carrying out effectively process specially for wastewater from chemical industry is not yet had.
Therefore, for solving the problems of the technologies described above, the necessary treatment process providing a kind of wastewater from chemical industry of innovation, to overcome described defect of the prior art.
Summary of the invention
For solving the problems of the technologies described above, one is the object of the present invention is to provide can effectively to realize organism (COD
cr), the efficient removal of colourity, improve biochemical and the treatment process of the low wastewater from chemical industry of processing cost.
For achieving the above object, the technical scheme that the present invention takes is: a kind for the treatment of process of wastewater from chemical industry, and it comprises following processing step:
1), wastewater from chemical industry is disposed to equalizing tank, and in equalizing tank the residence time be 10 hours;
2), waste water is entered 1 grade of coagulation reaction tank afterwards, and in 1 grade of coagulation reaction tank, add ferrous sulfate and lime, reaction times 5min;
3), the water outlet of 1 grade of coagulation reaction tank enters preliminary sedimentation tank and carries out mud-water separation, and the residence time of preliminary sedimentation tank is 6 hours;
4), the water outlet of preliminary sedimentation tank being entered sand filter and removes suspended substance, is about 0.5 hour in the residence time of sand filter;
5), the water outlet of sand filter enters 1 grade of ozone oxidation pond, 0.2 hour reaction times;
6), the water outlet in 1 grade of ozone oxidation pond enters electric catalysis reactor, 0.5 hour reaction times;
7), the water outlet of electric catalysis reactor enters second pond, adopts activation process aeration 24 hours postprecipitations, and carries out mud-water separation;
8), afterwards the water outlet of second pond is entered 2 grades of coagulation reaction tank, and add PAC and PAM in 2 grades of coagulation reaction tank;
9), the water outlet of 2 grades of coagulation reaction tank enters 2 grades of ozone oxidation ponds;
10), 2 grades of ozone oxidation pond water outlets are entered in elementary carbon bio-reactor, 45 ~ 60 minutes residence time;
11), the water outlet of elementary carbon bio-reactor enters in 3 grades of ozone oxidation ponds and continues advanced oxidation advanced treatment;
12), the water outlet in 3 grades of level ozone oxidation ponds enters secondary carbon bio-reactor, and after treatment, water outlet enters retention reservoir discharge or carries out back flushing to sand filter, elementary carbon bio-reactor, secondary carbon bio-reactor.
The treatment process of wastewater from chemical industry of the present invention is set to further: the reaction pH in described step 3) is between 7-8, FeSO
4dosage be 800mg/L.
The treatment process of wastewater from chemical industry of the present invention is set to further: in described step 5), and ozone dosage is 30ppm.
The treatment process of wastewater from chemical industry of the present invention is set to further: the catalytic filler being provided with the many metal compositions in Cu/Fe and Pd/Fe highs and lows position in the electric catalysis reactor of described step 6), this filler diameter is 3-5mm.
The treatment process of wastewater from chemical industry of the present invention is set to further: the water outlet COD of described step 7)
crvalue is less than 180mg/L, and PH is between 7-9, and SS value is less than 50mg/L.
The treatment process of wastewater from chemical industry of the present invention is set to further: in described step 8), and the dosage of PAC is 20-60 mg/L, PAM dosage is 1-2 mg/L; The residence time of water outlet in 2 grades of coagulation reaction tank is about 3 hours.
The treatment process of wastewater from chemical industry of the present invention is set to further: in described step 9) and step 11), adding ozone amount is 20-30mg/L, and the residence time is 45 minutes.
The treatment process of wastewater from chemical industry of the present invention is set to further: in described elementary carbon bio-reactor and secondary carbon bio-reactor, gac loading height is 4.5 meters, early stage empty bed operating two weeks; The bottom of described elementary carbon bio-reactor and secondary carbon bio-reactor is respectively equipped with a backwash tube respectively, and described backwash tube is connected with water outlet water reservoir.
The treatment process of wastewater from chemical industry of the present invention is also set to: in described step 12), and the residence time of waste water in secondary carbon biological respinse tower is 1 hour.
Compared with prior art, the present invention has following beneficial effect:
1. the treatment process of wastewater from chemical industry of the present invention combines the advantage of advantage of multiple coagulation, filtration, oxidation, electrical catalyze reduction, advanced oxidation, physical adsorption and biological treatment, treated wastewater from chemical industry, effectively can be degraded colourity and COD, improve the B/C ratio of wastewater from chemical industry, after process, water quality index of correlation can reach the emission limit set that GB18919-2002 standard specifies one-level B, have processing efficiency high, cost is low, simple to operate is easy to the advantages such as control.
2. the treatment process of wastewater from chemical industry of the present invention is using the combination of sand filter and biological filter as advanced treatment, and compared with advanced oxidation and membrane processing method, processing cost is all relatively low.
3. the treatment process of wastewater from chemical industry of the present invention gives full play to the potential of traditional biological method, without the need to adding other structures again, and the sand filter of advanced treatment and biological filter are all the methods of taking up an area smaller process, be applicable to very much the Sewage Plant transformation of land used anxiety.
Accompanying drawing explanation
Fig. 1 is the schema of the treatment process of wastewater from chemical industry of the present invention.
Embodiment
Refer to shown in Figure of description 1, the present invention is a kind for the treatment of process of wastewater from chemical industry, and it comprises following processing step:
1), wastewater from chemical industry is disposed to equalizing tank 1, and in equalizing tank 1 residence time be 10 hours.
2), waste water is entered 1 grade of coagulation reaction tank 2 afterwards, and in 1 grade of coagulation reaction tank 2, add ferrous sulfate and lime, reaction times 5min; The reaction pH of this step is between 7-8, FeSO
4dosage be the Fe of 800mg/L, inflow
2+colloidalmaterial Fe (OH) is formed with milk of lime
3and Fe (OH)
2, have extremely strong throwing out, in absorption waste water, a large amount of insoluble substance, can fully precipitate.
3), the water outlet of 1 grade of coagulation reaction tank 2 enters preliminary sedimentation tank 3 and carries out mud-water separation, and the residence time of preliminary sedimentation tank 3 is 6 hours.
4), the water outlet of preliminary sedimentation tank 3 being entered sand filter 4 and removes suspended substance, is 0.5 hour in the residence time of sand filter 4.
5), the water outlet of sand filter 4 enters 1 grade of ozone oxidation pond 5,0.2 hour reaction times; Wherein, ozone dosage is 30ppm.
6), the water outlet in 1 grade of ozone oxidation pond 5 enters electric catalysis reactor 6,0.5 hour reaction times; Wherein, be provided with the catalytic filler of the many metal compositions in Cu/Fe and Pd/Fe highs and lows position in electric catalysis reactor 6, this filler diameter is 3-5mm; Be del bottom electric catalysis reactor 6, and with the downward intermission aeration of high-pressure air pipe, make catalytic filler and waste water fully contact formation galvanic interaction, be conducive to the generation of free radical and improve processing efficiency, can effectively avoid filler to harden inefficacy simultaneously.
7), the water outlet of electric catalysis reactor 6 enters second pond 7, adopts activation process aeration 24 hours postprecipitations, and carries out mud-water separation; Second pond 7 water outlet COD
crvalue is less than 180mg/L, and PH is between 7-9, and SS value is less than 50mg/L.
8), afterwards the water outlet of second pond 7 is entered 2 grades of coagulation reaction tank 8, and add PAC and PAM in 2 grades of coagulation reaction tank 8; Wherein, the dosage of PAC is 20-60 mg/L, PAM dosage is 1-2 mg/L; The residence time of water outlet in 2 grades of coagulation reaction tank 8 is 3 hours.
9), the water outlet of 2 grades of coagulation reaction tank 8 enters 2 grades of ozone oxidation ponds 9; Wherein, adding ozone amount is 20-30mg/L, and the residence time is 45 minutes.
10), 2 grades of ozone oxidation pond 9 water outlets are entered in elementary carbon bio-reactor 10,45 ~ 60 minutes residence time.
11), the water outlet of elementary carbon bio-reactor 10 enters in 3 grades of ozone oxidation ponds 11 and continues advanced oxidation advanced treatment; Wherein, adding ozone amount is 20-30mg/L, and the residence time is 45 minutes.
12), the water outlet in 3 grades of level ozone oxidation ponds 11 enters secondary carbon bio-reactor 12, and the residence time of waste water in secondary carbon biological respinse tower 12 is 1 hour; After treatment, water outlet enters water reservoir 13 and discharges or carry out back flushing to sand filter 4, elementary carbon bio-reactor 10, secondary carbon bio-reactor 12, guarantees that aforesaid device can normally work all the time.
Further, in described elementary carbon bio-reactor 10 and secondary carbon bio-reactor 12, gac loading height is 4.5 meters, early stage empty bed operating two weeks; The bottom of described sand filter 4, elementary carbon bio-reactor 10 and secondary carbon bio-reactor 12 is respectively equipped with a backwash tube 13, thus ensures the activity of sand filter 4, elementary carbon bio-reactor 10 and secondary carbon bio-reactor 12; Described backwash tube 13 is connected with water reservoir 13.
Before wastewater from chemical industry enters equalizing tank 1 process, its water-quality guideline is as follows: COD
cr: 9868mg/L, colourity 2500 times, B/C ratio is 0.14.
After 1 grade of coagulation reaction tank 2 and preliminary sedimentation tank 3 process, water-quality guideline is as follows: COD
cr: 7660mg/L, colourity 1800 times, B/C ratio is 0.19.
After sand filter 4 processes, water-quality guideline is as follows: COD
cr: 7520mg/L, colourity 1700 times, B/C ratio is 0.19.
After 1 grade of ozone oxidation pond 5 processes, water-quality guideline is as follows: COD
cr: 5420mg/L, colourity 1200 times, B/C ratio is 0.22.
Water outlet is after electric catalysis reactor 6 processes, and water-quality guideline is as follows: COD
cr: 3280mg/L; Colourity 800 times, B/C ratio is 0.26.
Water outlet is after second pond 7 and 2 grades of coagulation reaction tank 8 process, and water-quality guideline is as follows: COD
cr: 2920mg/L, colourity 500 times, B/C ratio is 0.26.
Water outlet is after 2 grades of ozone oxidation ponds 9 process, and water-quality guideline is as follows: COD
cr: 1320mg/L; Colourity 280 times, B/C ratio is 0.29.
Water outlet is after elementary carbon bio-reactor 10 processes, and water-quality guideline is as follows: COD
cr: 730mg/L; Colourity 130 times, B/C ratio is 0.29.
Water outlet is after 3 grades of ozone oxidation ponds 11 process, and water-quality guideline is as follows: COD
cr: 290mg/L; Colourity 60 times, B/C ratio is 0.33.
Water outlet is after the process of secondary carbon bio-reactor 12, and water-quality guideline is as follows: COD
cr: 59mg/L; Colourity 11 times, B/C ratio is 0.35.
Therefore, as can be seen from above-mentioned data: wastewater from chemical industry, through above-mentioned art breading, can draw to draw a conclusion: COD, the colourity of water outlet can be reduced by the method and improve B/C ratio, making discharge of wastewater meet relevant emission standards.
Above embodiment is only the preferred embodiment of this creation, and not in order to limit this creation, any amendment made within all spirit in this creation and principle, equivalent replacement, improvement etc., within the protection domain that all should be included in this creation.
Claims (9)
1. a treatment process for wastewater from chemical industry, is characterized in that: comprise following processing step:
1), wastewater from chemical industry is disposed to equalizing tank, and in equalizing tank the residence time be 10 hours;
2), waste water is entered 1 grade of coagulation reaction tank afterwards, and in 1 grade of coagulation reaction tank, add ferrous sulfate and lime, reaction times 5min;
3), the water outlet of 1 grade of coagulation reaction tank enters preliminary sedimentation tank and carries out mud-water separation, and the residence time of preliminary sedimentation tank is 6 hours;
4), the water outlet of preliminary sedimentation tank being entered sand filter and removes suspended substance, is 0.5 hour in the residence time of sand filter;
5), the sand filter water outlet of sand filter enters 1 grade of ozone oxidation pond, 0.2 hour reaction times;
6), the water outlet in 1 grade of ozone oxidation pond enters electric catalysis reactor, 0.5 hour reaction times;
7), the water outlet of electric catalysis reactor enters second pond, adopts activation process aeration 24 hours postprecipitations, and carries out mud-water separation;
8), afterwards the water outlet of second pond is entered 2 grades of coagulation reaction tank, and add PAC and PAM in 2 grades of coagulation reaction tank;
9), the water outlet of 2 grades of coagulation reaction tank enters 2 grades of ozone oxidation ponds;
10), 2 grades of ozone oxidation tower water outlets are entered in elementary carbon bio-reactor, 45 ~ 60 minutes residence time;
11), the water outlet of elementary carbon bio-reactor enters in 3 grades of ozone oxidation ponds and continues advanced oxidation advanced treatment;
12), the water outlet of 3 grades of level ozone oxidation tower enters secondary carbon bio-reactor, and after treatment, water outlet enters retention reservoir discharge or carries out back flushing to sand filter, elementary carbon bio-reactor, secondary carbon bio-reactor.
2. the treatment process of wastewater from chemical industry as claimed in claim 1, is characterized in that: the reaction pH in described step 3) is between 7-8, FeSO
4dosage be 800mg/L.
3. the treatment process of wastewater from chemical industry as claimed in claim 1, it is characterized in that: in described step 5), ozone dosage is 30ppm.
4. the treatment process of wastewater from chemical industry as claimed in claim 1, is characterized in that: the catalytic filler being provided with the many metal compositions in Cu/Fe and Pd/Fe highs and lows position in the electric catalysis reactor of described step 6), this filler diameter is 3-5mm.
5. the treatment process of wastewater from chemical industry as claimed in claim 1, is characterized in that: described step 7) water outlet COD
crvalue is less than 180mg/L, and PH is between 7-9, and SS value is less than 50mg/L.
6. the treatment process of wastewater from chemical industry as claimed in claim 1, it is characterized in that: in described step 8), the dosage of PAC is 20-60 mg/L, PAM dosage is 1-2 mg/L; The residence time of water outlet in 2 grades of coagulation reaction tank is about 3 hours.
7. the treatment process of wastewater from chemical industry as claimed in claim 1, is characterized in that: in described step 9) and step 11), adding ozone amount is 20-30mg/L, and the residence time is 45 minutes.
8. the treatment process of wastewater from chemical industry as claimed in claim 1, is characterized in that: in described elementary carbon bio-reactor and secondary carbon bio-reactor, gac loading height is 4.5 meters, early stage empty bed operating two weeks; The bottom of described elementary carbon bio-reactor and secondary carbon bio-reactor is respectively equipped with a backwash tube respectively, and described back flushing is connected with water outlet water reservoir.
9. the treatment process of wastewater from chemical industry as claimed in claim 1, it is characterized in that: in described step 12), the residence time of waste water in secondary carbon biological respinse tower is 1 hour.
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| CN201510150817.1A CN104773916A (en) | 2015-04-01 | 2015-04-01 | Chemical engineering wastewater treatment method |
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| CN201510150817.1A CN104773916A (en) | 2015-04-01 | 2015-04-01 | Chemical engineering wastewater treatment method |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101343131A (en) * | 2008-06-13 | 2009-01-14 | 嘉兴学院 | Multi-stage combined degradation and recycle method for printing and dyeing wastewater |
| CN102701495A (en) * | 2012-06-25 | 2012-10-03 | 杨德敏 | Treatment device and treatment method for organic wastewater difficult to degrade |
| CN102992535A (en) * | 2012-12-28 | 2013-03-27 | 徐乾均 | Treatment method enabling drilling wastewater of petroleum and natural gas to meet standard on scene |
| CN104326530A (en) * | 2014-11-06 | 2015-02-04 | 清华大学 | Device and method for performing oxidation treatment on sewage by cooperating pipeline type electric catalysis with ozone |
-
2015
- 2015-04-01 CN CN201510150817.1A patent/CN104773916A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101343131A (en) * | 2008-06-13 | 2009-01-14 | 嘉兴学院 | Multi-stage combined degradation and recycle method for printing and dyeing wastewater |
| CN102701495A (en) * | 2012-06-25 | 2012-10-03 | 杨德敏 | Treatment device and treatment method for organic wastewater difficult to degrade |
| CN102992535A (en) * | 2012-12-28 | 2013-03-27 | 徐乾均 | Treatment method enabling drilling wastewater of petroleum and natural gas to meet standard on scene |
| CN104326530A (en) * | 2014-11-06 | 2015-02-04 | 清华大学 | Device and method for performing oxidation treatment on sewage by cooperating pipeline type electric catalysis with ozone |
Non-Patent Citations (1)
| Title |
|---|
| 高宗峰等: "《给水排水工程》", 31 January 2014 * |
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Application publication date: 20150715 |