CN1448346A - Method for treatment of waste water containing ammonia using caustic soda as alkali source - Google Patents
Method for treatment of waste water containing ammonia using caustic soda as alkali source Download PDFInfo
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- CN1448346A CN1448346A CN02116394A CN02116394A CN1448346A CN 1448346 A CN1448346 A CN 1448346A CN 02116394 A CN02116394 A CN 02116394A CN 02116394 A CN02116394 A CN 02116394A CN 1448346 A CN1448346 A CN 1448346A
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- ammonia
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- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 title claims abstract description 118
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 62
- 239000002351 wastewater Substances 0.000 title claims abstract description 55
- 239000003513 alkali Substances 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims abstract description 33
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 32
- 235000011121 sodium hydroxide Nutrition 0.000 title description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 39
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 22
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 18
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 12
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims abstract description 9
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims abstract description 7
- 239000010802 sludge Substances 0.000 claims description 29
- 230000008569 process Effects 0.000 claims description 22
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 21
- 238000004062 sedimentation Methods 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 7
- 239000011734 sodium Substances 0.000 claims description 7
- 244000005700 microbiome Species 0.000 claims description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Substances [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 2
- 239000001569 carbon dioxide Substances 0.000 claims description 2
- 230000000717 retained effect Effects 0.000 claims description 2
- 238000001704 evaporation Methods 0.000 claims 1
- 230000008020 evaporation Effects 0.000 claims 1
- 239000000428 dust Substances 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 abstract description 2
- 235000017550 sodium carbonate Nutrition 0.000 abstract 2
- 230000007423 decrease Effects 0.000 abstract 1
- 229910052806 inorganic carbonate Inorganic materials 0.000 abstract 1
- 235000017557 sodium bicarbonate Nutrition 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 239000007788 liquid Substances 0.000 description 6
- 238000004065 wastewater treatment Methods 0.000 description 6
- 241000894006 Bacteria Species 0.000 description 5
- 238000004821 distillation Methods 0.000 description 5
- 230000002829 reductive effect Effects 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 238000005273 aeration Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000013019 agitation Methods 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000005188 flotation Methods 0.000 description 2
- 230000001546 nitrifying effect Effects 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- 241000108664 Nitrobacteria Species 0.000 description 1
- 241001148470 aerobic bacillus Species 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 150000001721 carbon Chemical class 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 231100000989 no adverse effect Toxicity 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 230000035764 nutrition Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The present invention relates to industry waste water treating technology, and is one improved ammonia containing waste water treating method. New carbon source and alkali source are provided, that is, relatively cheap NaOH is used to replace Na2CO3. In the case of constantly adding air, water solution of NaOH will react with CO2 in air to produce NaHCO3 and Na2CO3 as inorganic carbonate. The present invention reduces waste water treating cost, decreases dust pollution, saves investment and lowers power consumption.
Description
Technical Field
The invention relates to a wastewater treatment technology, in particular to the type and requirement of alkali added for treating ammonia nitrogen in wastewater, and belongs to an industrial wastewater treatment technology.
Background
At present, the more perfect and reasonable method for treating ammonia nitrogen in wastewater in China is an AO (anaerobic-anoxic/aerobic) process. The process is as follows: the method comprises the following steps of mixing ammonia nitrogen-containing wastewater with return water from a secondary sedimentation tank, then feeding the mixed wastewater into an anoxic tank, controlling the pH value to be 7-8, and converting nitrate nitrogen in the return water into nitrogen to escape. The effluent of the anoxic tank enters an aerobic tank and is fully mixed and contacted with activated sludge from the sedimentation tank through aeration, pollutants in the wastewater are adsorbed and degraded under the action of microorganisms and oxygen, and nitrosobacteria and nitrobacteria for decomposing ammonia nitrogen belong to the genus autonomyThe aerobic bacteria need inorganic nitrogen source as the nutrition for synthesizing living matters, and the total reaction equation of oxidation and self synthesis is as follows:
therefore, Na is respectively added at the water inlet of the aerobic tank, the return sludge inlet and the outlet 1/3 of the aerobic tank2CO3The solution meets the requirement, the effluent alkalinity is kept to be more than 150mg/L, the effluent of the aerobic tank is precipitated by a sedimentation tank, activated sludge flows back into the aerobic tank, most of the effluent enters the anoxic tank as the return water, and the rest of the effluent enters a post-treatment process and is discharged after being treated. As can be known from the oxidation of nitrifying bacteria and the self-synthesis total reaction equation, 1.7 g of inorganic carbon needs to be consumed for treating 1 g of ammonia nitrogen, namely 15 g of Na is consumed2CO3Therefore, the process has high treatment cost, and 3-4 kg of Na is consumed for treating 1 ton of wastewater containing ammonia nitrogen at about 200mg/L2CO3Due toeach ton of Na2CO3The market price of the process is 2000 yuan, which is equivalent to that the alkali adding cost for treating 1 ton of wastewater with the concentration is about 7 yuan, and the process is seriously high, so that the process restricts the popularization in China due to high treatment cost. In addition, adding the same Na2CO3Corresponding devices for dissolving, hoisting and the like are required to be added, and a specially-assigned person is equipped for operation, so that the labor cost is increased, and the dust pollution is increased in the process of pouring the solid alkali.
Disclosure of Invention
The invention aims to provide a method for treating ammonia-containing wastewater by using sodium hydroxide as an alkali source, which is an improvement of the conventional method for treating ammonia-containing wastewater by an AO (anaerobic-anoxic/aerobic) method, and provides a new carbon source and an alkali source for treating ammonia-containing wastewater, namely, a relatively cheap alkali source NaOH is used for replacing Na2CO3The NaOH aqueous solution is easy to react with CO in the air under the condition of continuous aeration2Reaction to produce Na2CO3Thereby achieving the purpose of obtaining the inorganic carbon salt. The reaction equation is as follows:
And simultaneously, the effluent alkalinity of the aerobic tank is further reduced, so that the alkali consumption is reduced, and the aim of further reducing the cost is fulfilled.
The purpose of the invention is realized as follows:
the ammonia-containing wastewater with the ammonia nitrogen concentration less than or equal to 300mg/l (or with the ammonia nitrogen concentration less than or equal to 300mg/l after dilution) is firstly mixed with the return water from the secondary sedimentation tank and then enters an anoxic tank, the PH value is controlled to be 7-8, and nitrate nitrogen in the return water is converted into nitrogen to escape. The effluent of the anoxic tank enters an aerobic tank. And respectively adding 3-5 wt% of NaOH dilute solution at a return sludge inlet and a wastewater inlet of the aerobic tank, wherein the total amount of the NaOH dilute solution is added by adding 5.5-6 g of 100% NaOH per gram of ammonia nitrogen in the ammonia-containing wastewater. The alkali adding amount of the two alkali adding points is distributed according to the ratio of 1: 1-3, namely the alkali adding amount at the sludge return inlet of the aerobic tank accounts for 25-50% of the total alkali adding amount of the aerobic tank, and the alkali adding amount at the wastewater inlet of the aerobic tank accounts for 50-75% of the total alkali adding amount of the aerobic tank. Under the condition that the aerobic pool is continuously aerated with air, the added sodium hydroxide reacts with carbon dioxide in the air to generate NaHCO3And a small amount of Na2CO3Activated sludge from the sedimentation tank is fully mixed and contacted with the wastewater through aeration, and microorganisms (mainly nitrite bacteria and nitrate bacteria) in the sludge adsorb ammonia nitrogen in the wastewater and convert the ammonia nitrogen into NO under the action of oxygen by utilizing a carbon source captured by NaOH3-. The effluent alkalinity of the aerobic tank is CaCO3Meter) is controlled to be 80-160 mg/l, and the pH value of the effluent of the aerobic tank is 6-7 at the moment. If the alkalinity of the effluent of the aerobic tank is too large (more than 160mg/l), although the conversion of ammonia nitrogen into nitrate and the conversion of NaOH into NaHCO are facilitated3、Na2CO3But can cause waste of alkali; the alkalinity of the effluent of the aerobic tank is too small (less than 80mg/l), which reduces the PH value in the aerobic tank, thereby inhibiting CO2Absorption and ammonia nitrogen conversion. In order to promote the absorption of CO by NaOH2Conversion to NaHCO3And Na2CO3The process is carried out to fully meet the requirement of microorganisms on inorganic carbon, and 30 to 50 percent of the total amount of NaOH required by the aerobic pool can be continuously added in any water storage pool in front of the anoxic pool in advance, and the water is continuously aerated with the CO-rich water2The pH value of the anoxic tank is less than 8.5, because the excessive pH value inhibits the denitrification process in the anoxic tank. Therefore, under the condition that the alkali added in the aerobic tank can meet the system requirement, the adding amount of the alkali before the anoxic tank is reduced as much as possible.
After the effluent of the aerobic tank is precipitated by the sedimentation tank, the activated sludge flows back into the aerobic tank, most of the effluent enters the anoxic tank as the backflow water, and the rest of the effluent enters the post-treatment process and is discharged after being treated.
For ammonia-containing wastewater with ammonia nitrogen concentration of more than 300mg/l (such as a coking plant), ammonia distillation treatment is carried out before biochemical treatment of the wastewater, and NaOH is added to decompose fixed ammonium salt in the wastewater, so that excessive NaOH can be added into an ammonia distillation tower, inorganic carbon in a large amount of carbonate contained in the wastewatercan be converted into Na by NaOH2CO3Is retained in the wastewater without being converted into CO2The ammonia is escaped and dissipated in the air, and the ammonia distillation efficiency of the ammonia distillation tower is improved, but the excessive degree of adding alkali into the ammonia distillation tower is preferably that the pH value in the anoxic pond is not more than 8.5. If the inorganic carbon fixed in the process can not meet the requirements of the microorganisms in the aerobic tank, namely the alkalinity of the effluent of the aerobic tank is lower than 80mg/l, and the pH value can not reach 6-7, NaOH is still added into the reflux sludge inlet and the wastewater inlet of the aerobic tank according to the proportion of 1: 1-3, and CO in the air is captured2To supplement the deficiency of inorganic carbon and meet the alkalinity of the effluent of the aerobic pond system (by CaCO)3In terms of) 80-160 mg/l, and the pH value is 6-7. The effluent of the aerobic tank meets the requirements.
It is to be noted that NaOH added in the aerobic tank is converted into NaHCO3And a small amount of Na2CO3A process is required whereby sufficient time is allowed for sufficient conversion of NaOH to NaHCO3(Na2CO3) Without running off with water, i.e. the location of adding alkali should be well awayEffluent of the oxygen poolAnd removing an alkali adding point closest to a water outlet of the aerobic tank, changing the original three-point alkali adding into two-point alkali adding, reserving two alkali adding points of a return sludge inlet of the aerobic tank and a waste water inlet of the aerobic tank, and adding the total amount according to the addition of 5.5-6 g of NaOH into ammonia nitrogen per gram of ammonia nitrogen entering the system. The alkali adding amount of the two alkali adding points is distributed according to the ratioof 1: 1-3.
In addition, the alkalinity of the effluent of the aerobic tank is too high, which easily causes alkali waste, and experiments prove that the alkalinity of the effluent of the aerobic tank (as CaCO)3Meter) is controlled to be slightly larger than 80mg/L to meet the requirement of microorganisms, and the pH value of effluent of the aerobic tank is 6-7 at the moment. Therefore, the alkali adding amount needs to be adjusted by taking the alkalinity of the effluent as a main index so as to further reduce the alkali consumption in the wastewater treatment process.
The invention uses cheap NaOH concentrated solution to replace expensive solid Na2CO3As an alkali source, solid Na is added into the continuously added alkali source2CO3The prepared dilute solution is changed into a dilute NaOH solution with the addition concentration (weight percentage) of 3-5%, and CO provided while continuously aerating air in an aerobic tank is utilized to provide oxygen2Reacting NaOH with CO2Chemical reaction occurs to produce NaHCO3And a small amount of Na2CO3Thereby obtaining the inorganic carbon necessary for the life activities of the nitrifying bacteria and reducing the treatment cost of the ammonia-containing wastewater. The invention also reduces the effluent alkalinity of the aerobic tank to reduce the waste of alkali and achieve the purpose of reducing the cost. Experiments prove that NaOH is used for replacing Na2CO3The alkaline source added into the aerobic tank has no adverse effect on the life activities of bacteria in the aerobic tank and the treatment effect of wastewater, and the excessive alkalinity of the effluent of the aerobic tank only causes the waste of alkali.
Compared with the alkali adding technology of the prior ammonia-containing wastewater treatment process AO method(namely anoxic/aerobic), the invention has the following advantages under the same treatment effect:
1. greatly reduces the treatment cost of the wastewater, and reduces the alkali addition cost of each ton of wastewater from about 7 yuan to about 2 yuan.
2. Saves investment and powerConsumption of solid Na is reduced2CO3The dissolving tank and the transportation and hoisting equipment.
3. The labor cost is saved, and the post does not need to be configured with a specially-assigned person for operation.
4. And dust pollution is reduced.
5. Avoid the solid Na2CO3Insoluble impurities contained in the waste water block an alkali pool and a pipeline, so that the pipeline replacement and the heavy pool cleaning work are reduced.
Drawings
FIG. 1 is a flow chart of the ammonia-containing wastewater treatment process of the invention. In the figure: 1-high tank, 2-pump, 3-ammonia still, 4-pump, 5-wastewater adjusting tank, 6-pump, 7-flotation oil removing tank, 8-water distribution well, 9-pump, 10-anoxic tank, 11-aerobic tank, 12-sedimentation tank, 13-water distribution well, 14-sludge well, 15-pump, 16-dilute alkali tank, 17-pump, 18-post treatment process.
Detailed Description
Example 1
The present invention will be further described with reference to FIG. 1 (excluding the portion indicated by the dashed line) and examples.
The flow rate is 36m3About one hour of ammonia-containing wastewater (containing 120mg/l of ammonia nitrogen, less than 2000mg/l ofCOD value and 7-8 of PH value) is distributed between the water distribution well 8 and 150m from the water distribution well 133About/h of reflux water mixtureThen, the mixed wastewater (H value of 7) is sent to an anoxic tank 10 by a pump 9. NO contained in the return water3Is converted here to N2Then the wastewater flows into the aerobic tank 11 automatically. Here, the wastewater is thoroughly mixed with the return sludge from the sedimentation tank 12 under vigorous agitation by continuously introduced compressed air. The concentrated NaOH solution with concentration (weight percentage) of about 40% enters a dilute alkali tank 16, is diluted into the dilute NaOH solution with concentration (weight percentage) of about 4% by 9 times of clean water under the stirring of compressed air, and is continuously pumped by a pump 17 at a speed of about 0.7m3Total flow/h, controlled by a valve in a ratio of 1: 2The aerobic tank 11 is respectively added at the sludge return inlet and the waste water inlet of the aerobic tank. Effluent of the aerobic tank (alkalinity is 80-160 mg/l, pH value is 6-7) automatically flows into a sedimentation tank 12, sludge is settled, sludge at the bottom automatically flows into a sludge well 14, then the sludge is sent back to the aerobic tank 11 by a pump 15 to be used as return sludge, clear liquid at the upper part automatically flows into a water distribution well 13, most of the clear liquid is used as return water to enter a water distribution well 8, and the rest of the clear liquid enters a post-treatment process 18 and is discharged as discharged water after treatment.
Example 2
The present invention is described in detail with reference to the accompanying FIG. 1 (the portion within the dotted line) and the following examples:
passing the concentrated NaOH solution with concentration (weight percentage) of about 40% through the high-position tank 1 at a speed of 0.45m3Flow rate/h and flow rate of 32m3The ammonia-containing wastewater (containing 3000-3300 mg/l ammonia nitrogen and having a pH value of 9) of the coking plant is sent into an ammonia still 3 by a pump 2. Introducing steam from the bottom of the tower to evaporate most of ammonia in the ammonia water from the top of the tower, and discharging water from the bottom of the tower (the flow rate is 36 m)3About 120mg/l of ammonia-containing nitrogen, about 4200mg/l of COD value and 10-11 of PH value) by a pump 4 to a wastewater adjusting tank 5 of a wastewater treatment device. The wastewater is sent to a flotation oil removal tank 7 by a pump 6 to remove light oil, and then automatically flows to a water distribution well 8 with the diameter of 40m3About/h of clean water and 150m from water distribution wells 133The reflux water is mixed for about/h, and then the mixed wastewater (the PH value is 7.5-8.5) is sent into an anoxic pond 10 by a pump 9. NO contained in the return water3Is converted here to N2Then the wastewater flows into the aerobic tank 11 automatically. Here, the wastewater is thoroughly mixed with the return sludge from the sedimentation tank 12 under vigorous agitation by continuously introduced compressed air. The concentrated NaOH solution with concentration (weight percentage) of about 40% enters a dilute alkali tank 16, is diluted into dilute NaOH solution with concentration (weight percentage) of about 4% by clean water under the stirring of compressed air, and is continuously pumped by a pump 17 at a speed of about 0.4m3The total flow of the flow/h is respectively added into the aerobic tank at the sludge return inlet and the waste water inlet of the aerobic tank according to the proportion of 1: 2. The effluent of the aerobic tank (alkalinity of 80-160 mg/l, pH value of 6-7) automatically flows into a sedimentation tank 12, the sludge is sedimentated, the sludge at the bottom automatically flows into a sludge well 14, and then a pump is used15 is sent back to the aerobic tank 11 to be used as return sludge, the upper clear liquid automatically flows into a water distribution well 13, most of the clear liquid is used as return water to enter a water distribution well 8, and the rest of the clear liquid enters a post-treatment process 18 to be treated and then discharged as discharged water.
Claims (3)
1. A method for treating ammonia-containing wastewater by taking sodium hydroxide as an alkali source is characterized by comprising the following steps:
(1) the ammonia-containing wastewater with the concentration less than or equal to 300mg/l is firstly mixed with return water from a secondary sedimentation tank and then enters an anoxic tank, the pH value is controlled to be 7-8, and effluent of the anoxic tank enters an aerobic tank. Respectively adding 3-5 wt% of NaOH dilute solution into a return sludge inlet and a wastewater inlet of an aerobic tank, wherein the total amount of the added NaOH dilute solution is that 100% NaOH with the amount of ammonia nitrogen contained in the ammonia-containing wastewater being 5.5-6 g/g of ammonia nitrogen is added into the ammonia nitrogen, and the alkali adding amount of the two alkali adding points is distributed according to the ratio of 1: 1-3, namely the alkali adding amount at the return sludge inlet of the aerobic tank accounts for 25-50% of the total alkali adding amount of the aerobic tank, and the alkali adding amount at the wastewater inlet of the aerobic tank accounts for 50-75% of the total alkali adding amount of the aerobic tank; the effluent alkalinity of the aerobic tank is CaCO3Metering) is controlled to be 80-160 mg/l, and the pH value of the effluent of the aerobic tank is 6-7 at the moment; after the effluent of the aerobic tank is precipitated by a sedimentation tank, the activated sludge flows back into the aerobic tank, most of the effluent enters an anoxic tank as reflux water, and the rest of the effluent enters a post-treatment process and is discharged after being treated;
(2) adding excessive NaOH into ammonia-containing wastewater with the concentration of more than 300mg/l in an ammonia still to ensure that inorganic carbon in a large amount of carbonate contained in the ammonia-containing wastewater can be changed into Na by NaOH2CO3Is retained in the wastewater without being converted into CO2The ammonia is escaped and lost in the air, but the excess degree of the ammonia evaporation and the alkali addition is to ensure that the pH value in the anoxic pond is not more than 8.5; if the inorganic carbon fixed in the above process can not meet the requirement of the microorganism in the aerobic tank, i.e. the alkalinity of the effluent of the aerobic tank (as CaCO)3Metering) can not be controlled to be 80-160 mg/l, and the pH value of the effluent of the aerobic tank is not 6-7; respectively adding 3-5 wt% of NaOH dilute solution into a return sludge inlet and a wastewater inlet of the aerobic tank, wherein the alkali adding amount of the two alkali adding points is 1: 1 ℃3, distribution, namely the alkali adding amount at the sludge return inlet of the aerobic tank accounts for 25-50% of the total alkali adding amount of the aerobic tank, and the alkali adding amount at the wastewater inlet of the aerobic tank accounts for 50-75% of the total alkali adding amount of the aerobic tank; the total addition amount of NaOH is based on the effluent alkalinity of the aerobic tank (based on CaCO)3Meter) is controlled to be 80-160 mg/l, and the pH value is controlled to be 6-7.
2. Method according to claim 1, characterized in that NaOH is added to react with CO2The reaction takes place to form NaHCO3And a small amount of Na2CO3Instead of directly adding Na2CO3。
3. The method of claim 1, wherein the added NaOH reacts with carbon dioxide in the air to form NaHCO under the condition that the aerobic pool is continuously aerated with the air3And a small amount of Na2CO3To obtain inorganic carbon; or continuously adding 30-50% of NaOH required by the aerobic pool in any water storage pool in front of the anoxic pool in advance, and continuously adding CO-rich water2The PH of the anoxic tank should be less than 8.5.
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|---|---|---|---|
| CNB021163944A CN1239413C (en) | 2002-04-01 | 2002-04-01 | Method for treatment of waste water containing ammonia using caustic soda as alkali source |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021163944A CN1239413C (en) | 2002-04-01 | 2002-04-01 | Method for treatment of waste water containing ammonia using caustic soda as alkali source |
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| CN1448346A true CN1448346A (en) | 2003-10-15 |
| CN1239413C CN1239413C (en) | 2006-02-01 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101402502B (en) * | 2008-07-21 | 2011-04-27 | 北京桑德环保集团有限公司 | Mifepristone wastewater treatment method and treatment equipment |
| CN105884115A (en) * | 2014-04-30 | 2016-08-24 | 滨州医学院 | Medical wastewater treatment system |
| CN106678479A (en) * | 2016-12-26 | 2017-05-17 | 中蓝连海设计研究院 | Method and device for realizing anti-freezing heat insulation for alkalifying pipeline of plateau wastewater treatment system |
| CN109264886A (en) * | 2018-09-17 | 2019-01-25 | 大丰跃龙化学有限公司 | A kind of wastewater treatment method in cyclopropylamine production process |
| CN119349771A (en) * | 2024-12-19 | 2025-01-24 | 河北协同水处理技术有限公司 | A system and method for comprehensive utilization of VOC waste gas from anoxic pool of coking wastewater |
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2002
- 2002-04-01 CN CNB021163944A patent/CN1239413C/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101402502B (en) * | 2008-07-21 | 2011-04-27 | 北京桑德环保集团有限公司 | Mifepristone wastewater treatment method and treatment equipment |
| CN105884115A (en) * | 2014-04-30 | 2016-08-24 | 滨州医学院 | Medical wastewater treatment system |
| CN105884115B (en) * | 2014-04-30 | 2018-11-20 | 滨州医学院 | A kind of medical waste water processing system |
| CN106678479A (en) * | 2016-12-26 | 2017-05-17 | 中蓝连海设计研究院 | Method and device for realizing anti-freezing heat insulation for alkalifying pipeline of plateau wastewater treatment system |
| CN109264886A (en) * | 2018-09-17 | 2019-01-25 | 大丰跃龙化学有限公司 | A kind of wastewater treatment method in cyclopropylamine production process |
| CN119349771A (en) * | 2024-12-19 | 2025-01-24 | 河北协同水处理技术有限公司 | A system and method for comprehensive utilization of VOC waste gas from anoxic pool of coking wastewater |
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