CN102206021A - Method for treating high-salinity inorganic ammonia nitrogen waste water - Google Patents
Method for treating high-salinity inorganic ammonia nitrogen waste water Download PDFInfo
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- CN102206021A CN102206021A CN 201110114835 CN201110114835A CN102206021A CN 102206021 A CN102206021 A CN 102206021A CN 201110114835 CN201110114835 CN 201110114835 CN 201110114835 A CN201110114835 A CN 201110114835A CN 102206021 A CN102206021 A CN 102206021A
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Abstract
The invention discloses a method for treating high-salinity inorganic ammonia nitrogen waste water, which comprises the following steps: (1) introducing waste water into a regulation tank to homogenize and regulate the pH value of the waste water; (2) pumping the homogenized waste water into a micro-electrolysis reaction tank for micro-electrolysis treatment; (3) introducing waste water subjected to micro-electrolysis treatment to a neutralizing precipitation pond, and regulating the pH value to complete neutralizing precipitation; (4) introducing the waste water in which precipitation is completed into a sequencing batch reactor (SBR) reaction pond to complete the sequencing batch reactor (SBR) activated sludge treatment; (5) introducing treated waste water discharged from the SBR reaction pond and performing contact oxidization; and (6) and completing the oxidized waste water. In the invention, a treatment scheme for high-salinity inorganic ammonia nitrogen waste water is provided, and the ammonia nitrogen content in the treated effluent reaches a national grade-I discharge standard.
Description
Technical field
The present invention relates to a kind of method of handling nitrogenous effluent, be meant the method that a kind of method of denitrogenation of waste water is applied to the inorganic ammonia nitrogen wastewater treatment of high salinity especially.
Background technology
Iron-carbon micro-electrolysis all has good treatment effect to all kinds of waste water, also is applied to ammonia nitrogen waste water.In " Chinese environmental protection industry " 2006 the 6th interim " high ammonia nitrogen high-enriched organics pharmacy sewage is handled pilot scale research " literary compositions of delivering, propose a kind of technology of handling high ammonia nitrogen, high-enriched organics pharmacy waste water, comprised acidication, micro cell, stripping pond, coagulating sedimentation, anaerobic baffle plate, BAF aeration tank, materialization settling tank, water outlet; 200610134616.3 of Chinese patent ZL put forward a kind of energy-saving ammonia nitrogen waste water treatment method, comprise pre-treatment, short distance nitration, little electrolysis, aftertreatment.And the high ammonia nitrogen of production petrochemical complex catalyst for cracking (200～500mg/l) inorganic ammonia nitrogen waste water, because of salinity height (Cl-3000～10000mg/l), existence has inhibiting toxicant to nitrifier and denitrifying bacteria in the existing biochemical processing, and the shortage carbon source does not see that at present effective treatment process can realize qualified discharge.
Summary of the invention
The purpose of this invention is to provide the inorganic method for treating ammonia-nitrogen wastewater of a kind of high salinity, this method makes full use of little electrolytic effect, effectively remove in this waste water nitrifier and denitrifying bacteria are had inhibiting toxicant, again in conjunction with intermittent activated sludge process SBR (Sequencing Batch Reactor) and catalytic oxidation, provide carbon source by adding starch, the nitrogen of waste water is deviate from the most at last, and the water outlet ammonia nitrogen can be less than 5mg/l.
Designed a kind of method of handling the inorganic ammonia nitrogen waste water of high salinity according to above-mentioned purpose, steps of the method are,
(1) described waste water is introduced the pH value that equalizing tank homogenizes and handles and adjust waste water;
(2) will homogenize waste water pump after handling is gone into the micro-electrolysis reaction pond and is carried out little electrolysis treatment;
(3) waste water after little electrolysis treatment is introduced the neutralization precipitation pond, finish neutralization precipitation through adjusting pH value;
(4) sequence intermittent activated sludge process SBR processing is carried out in the wastewater supernatant fluid introducing sbr reactor pond that will finish post precipitation;
(5) will carry out catalytic oxidation by waste water introducing oxidation pond that discharge, after treatment from the sbr reactor pond;
(6) waste water that will finish oxide treatment is discharged.
Wherein, the described processing that homogenizes of step (1) is with sulfuric acid or bodied ferric sulfate pH value to be adjusted to 2.5～3.5.The waste water that finishing homogenizes handles is pumped to the micro-electrolysis reaction pond, and waste water residence time in the micro-electrolysis reaction pond is to carry out little electrolysis treatment in 30～120 minutes.Waste water after little electrolysis is introduced into the neutralization precipitation pond, and described precipitation process is to drop into calcium oxide CaO, aluminium sesquioxide Al in settling tank
2O
3, a kind of or its mixture among the manganese oxide MgO, until pH value is adjusted to 7～9.Wastewater supernatant fluid behind neutralization precipitation is introduced into the sbr reactor pond and carries out the SBR processing, and stops in the pond 8～32 hours.Described waste water is during the SBR processing is carried out in the sbr reactor pond, need in the SBR pond, to add food starch, add-on is 0.3kg/m3, perhaps described waste water is introduced into oxidation pond and carries out the catalytic oxidation processing with further denitrification after SBR handles, need add food starch during this time, add-on is 0.3kg/m3, and the time of catalytic oxidation is 8～24 hours.
The present invention proposes a kind of processing scheme at the inorganic ammonia nitrogen waste water of high salinity, ammonia-nitrogen content not only reaches national grade one discharge standard in the discharge water according to the present invention after the processing, and, can reach about 5.0mg/l far below ammonia nitrogen national sewage comprehensive emission standard 15mg/l.
Description of drawings
Accompanying drawing 1 is a flow process simplified schematic diagram of the present invention.
Embodiment
Purport of the present invention provides a kind of processing scheme at the inorganic ammonia nitrogen waste water of high salinity, to solve the technical barrier that present this type of waste water can not be effectively addressed.So proposed following basic technical scheme and step:
(1) the inorganic ammonia nitrogen waste water of pending high salinity is introduced the pH value that equalizing tank homogenizes and handles and adjust waste water;
(2) will homogenize waste water pump after handling is gone into the micro-electrolysis reaction pond and is carried out little electrolysis treatment;
(3) waste water after little electrolysis treatment is introduced the neutralization precipitation pond, finish neutralization precipitation through adjusting pH value;
(4) sequence intermittent activated sludge process SBR processing is carried out in the wastewater supernatant fluid introducing sbr reactor pond that will finish post precipitation;
(5) will carry out catalytic oxidation by waste water introducing oxidation pond that discharge, after treatment from the sbr reactor pond;
(6) waste water that will finish oxide treatment is discharged.
Wherein, the described processing that homogenizes of step (1) is with sulfuric acid or bodied ferric sulfate pH value to be adjusted to 2.5～3.5.The waste water that finishing homogenizes handles is pumped to the micro-electrolysis reaction pond, and waste water residence time in the micro-electrolysis reaction pond is to carry out little electrolysis treatment in 30～120 minutes.Waste water after little electrolysis is introduced into the neutralization precipitation pond, and described precipitation process is to drop into calcium oxide CaO, aluminium sesquioxide Al in settling tank
2O
3, a kind of or its mixture among the manganese oxide MgO, until pH value is adjusted to 7～9.Wastewater supernatant fluid behind neutralization precipitation is introduced into the sbr reactor pond and carries out the SBR processing, and stops in the pond 8～32 hours.Described waste water is during the SBR processing is carried out in the sbr reactor pond, need in the SBR pond, to add food starch, add-on is 0.3kg/m3, perhaps described waste water is introduced into oxidation pond and carries out the catalytic oxidation processing with further denitrification after SBR handles, need add food starch during this time, add-on is 0.3kg/m3, and the time of catalytic oxidation is 8～24 hours.
The invention will be further described below in conjunction with specific embodiment.
Embodiment 1.Contain ammonia nitrogen 196mg/l, after the waste water of Cl-concentration 3600mg/l enters equalizing tank and homogenizes, add sulfuric acid and transfer PH=3.0, be promoted to the micro-electrolysis reaction pond with pump, micro-electrolysis reaction added lime and transfers the PH=8.5 neutralization precipitation after 45 minutes.The supernatant liquor of post precipitation enters the sbr reactor pond, and the temperature in sbr reactor pond is controlled at 18～35 ℃, adds starch to provide sbr reactor required carbon source, and the sbr reactor time is 16 hours.Water behind sbr reactor enters catalytic oxidation, and the residence time is 8 hours, and final outflow water contains ammonia nitrogen 10.8mg/l.
Embodiment 2.Contain ammonia nitrogen 215.7mg/l, Cl
-After the waste water of concentration 4100mg/l enters equalizing tank and homogenizes, add sulfuric acid and bodied ferric sulfate and transfer PH=3.0, be promoted to the micro-electrolysis reaction pond with pump, micro-electrolysis reaction added lime and MgO and transfers the PH=8.0 neutralization precipitation after 60 minutes.The supernatant liquor of post precipitation enters the sbr reactor pond, and the temperature in sbr reactor pond is controlled at 18～35 ℃, adds starch to provide sbr reactor required carbon source, and the sbr reactor time is 24 hours.Water behind sbr reactor enters catalytic oxidation, and the residence time is 12 hours, and final outflow water contains ammonia nitrogen 4.8mg/l.
Embodiment 3.Contain ammonia nitrogen 280.6mg/l, Cl
-After the waste water of concentration 5000mg/l enters equalizing tank and homogenizes, add H
2SO
4Transfer PH=3.0, be promoted to the micro-electrolysis reaction pond with pump, micro-electrolysis reaction added lime and Al after 90 minutes
2O
3Transfer the PH=8.0 neutralization precipitation.The supernatant liquor of post precipitation enters the sbr reactor pond, and the temperature in sbr reactor pond is controlled at 18～35 ℃, adds starch to provide sbr reactor required carbon source, and the sbr reactor time is 30 hours.Water behind sbr reactor enters catalytic oxidation, and the residence time is 16 hours, and final outflow water contains ammonia nitrogen 2.8mg/l.
Claims (7)
1. a method of handling the inorganic ammonia nitrogen waste water of high salinity steps of the method are,
(1) described waste water is introduced the pH value that equalizing tank homogenizes and handles and adjust waste water;
(2) will homogenize waste water pump after handling is gone into the micro-electrolysis reaction pond and is carried out little electrolysis treatment;
(3) waste water after little electrolysis treatment is introduced the neutralization precipitation pond, finish neutralization precipitation through adjusting pH value;
(4) sequence intermittent activated sludge process SBR processing is carried out in the wastewater supernatant fluid introducing sbr reactor pond that will finish post precipitation;
(5) will carry out catalytic oxidation by waste water introducing oxidation pond that discharge, after treatment from the sbr reactor pond;
(6) waste water that will finish oxide treatment is discharged.
2. the method for the inorganic ammonia nitrogen waste water of processing high salinity according to claim 1 is characterized in that: the described processing that homogenizes of step (1) is with sulfuric acid or bodied ferric sulfate pH value to be adjusted to 2.5～3.5.
3. the method for the inorganic ammonia nitrogen waste water of processing high salinity according to claim 2 is characterized in that: pump into waste water residence time in the micro-electrolysis reaction pond behind the micro-electrolysis reaction pond and be 30～120 minutes and carry out little electrolysis treatment.
4. the method for the inorganic ammonia nitrogen waste water of processing high salinity according to claim 3, it is characterized in that: the waste water after little electrolysis is introduced into the neutralization precipitation pond, and described precipitation process is to drop into calcium oxide CaO, aluminium sesquioxide Al in settling tank
2O
3, a kind of or its mixture among the manganese oxide MgO, until pH value is adjusted to 7～9.
5. the method for the inorganic ammonia nitrogen waste water of processing high salinity according to claim 4 is characterized in that: the wastewater supernatant fluid behind neutralization precipitation is introduced into the sbr reactor pond and carries out the SBR processing, and stops in the pond 8～32 hours.
6. the method for the inorganic ammonia nitrogen waste water of processing high salinity according to claim 5 is characterized in that: described waste water needs add food starch in the SBR pond during the SBR processing is carried out in the sbr reactor pond, and add-on is 0.3kg/m3.
7. the method for the inorganic ammonia nitrogen waste water of processing high salinity according to claim 5, it is characterized in that: described waste water is introduced into oxidation pond and carries out the catalytic oxidation processing with further denitrification after SBR handles, need add food starch during this time, add-on is 0.3kg/m3, and the time of catalytic oxidation is 8～24 hours.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102786182A (en) * | 2012-03-29 | 2012-11-21 | 波鹰(厦门)科技有限公司 | Device for processing landfill leachat |
| CN103102033A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Sulfur and ammonia-containing wastewater treatment method |
| CN106396242A (en) * | 2015-07-28 | 2017-02-15 | 江苏吉华化工有限公司 | Difficultly-degradable wastewater treatment method |
| CN107572720A (en) * | 2017-09-13 | 2018-01-12 | 中山中珠环保科技有限公司 | A kind of high-salinity wastewater zero-emission set treatment device |
| CN115571993A (en) * | 2021-07-01 | 2023-01-06 | 杭州国泰环保科技股份有限公司 | Ammonia nitrogen wastewater treatment device and treatment method |
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2011
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Non-Patent Citations (1)
| Title |
|---|
| 《环境科学与技术》 20071231 王妍等 微电解-吹脱-SBR法处理DSD酸生产废水 第80页左栏第1段，表1，图1，2.1.1-2.3节 1－7 第30卷, 第12期 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103102033A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Sulfur and ammonia-containing wastewater treatment method |
| CN103102033B (en) * | 2011-11-10 | 2014-08-20 | 中国石油化工股份有限公司 | Sulfur and ammonia-containing wastewater treatment method |
| CN102786182A (en) * | 2012-03-29 | 2012-11-21 | 波鹰(厦门)科技有限公司 | Device for processing landfill leachat |
| CN106396242A (en) * | 2015-07-28 | 2017-02-15 | 江苏吉华化工有限公司 | Difficultly-degradable wastewater treatment method |
| CN107572720A (en) * | 2017-09-13 | 2018-01-12 | 中山中珠环保科技有限公司 | A kind of high-salinity wastewater zero-emission set treatment device |
| CN115571993A (en) * | 2021-07-01 | 2023-01-06 | 杭州国泰环保科技股份有限公司 | Ammonia nitrogen wastewater treatment device and treatment method |
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