CN111018248A - Treatment method of high-ammonia-nitrogen high-phosphorus-salt wastewater - Google Patents
Treatment method of high-ammonia-nitrogen high-phosphorus-salt wastewater Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/288—Treatment of water, waste water, or sewage by sorption using composite sorbents, e.g. coated, impregnated, multi-layered
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
Abstract
The invention discloses a method for treating high-ammonia-nitrogen high-phosphorus-salt wastewater, belonging to the technical field of water treatment. The wastewater is directly subjected to distillation treatment without adjusting pH, byproduct salt is recovered, if COD (chemical oxygen demand) of the distilled water is more than or equal to 6000mg/L, the distilled water is subjected to resin adsorption treatment, then the distilled water enters a stripping tower to recover ammonia water, if the COD is less than 6000mg/L, the distilled water directly enters the stripping tower to recover the ammonia water, and the treated water enters a biochemical reaction tank to perform biological denitrification so as to meet the requirement of taking over in a park. The treatment method can effectively solve the problem of large solid waste generation amount caused by large addition amount of alkali or acid in the high-ammonia nitrogen and high-salinity wastewater treatment process, effectively reduces the wastewater treatment cost and the generation of secondary pollution, and simultaneously solves the problems of large fluctuation of effluent quality and unstable water quality.
Description
Technical Field
The invention belongs to the technical field of water treatment, and particularly relates to a method for treating high-ammonia-nitrogen high-phosphorus-salt wastewater.
Background
Chemical enterprises can produce a large amount of high-ammonia nitrogen high-salinity organic wastewater, and compared with other wastewater, the wastewater has the following characteristics: firstly, the ammonia nitrogen content in water is high, and high ammonia nitrogen wastewater is discharged into a water body, so that the water body generates eutrophication, seriously threatens the safety of water environment, and is easily oxidized into nitrite and nitrate, which becomes a factor threatening the health of human beings; secondly, the mineral water contains a large amount of inorganic salt, generally saturated salt water, which directly leads to the improvement of the mineralization degree of the water quality of rivers, brings more and more serious pollution to soil, surface water and underground water, endangers the ecological environment, and most of the salt substances contained are Cl-、SO4 2-、Na+、PO4 +Although these ions are all essential nutrients for the growth of microorganisms and play an important role in promoting enzyme reaction, maintaining membrane balance and regulating osmotic pressure during the growth process of microorganisms, if the concentration of these ions is too high, these ions will have inhibitory and toxic effects on microorganisms, and the main expression is: the salt concentration is high, the osmotic pressure is high, the microbial cell dehydration causes cell protoplasm separation, the salting-out action reduces the dehydrogenase activity, the chloride ion is high and has toxic action on bacteria, the salt concentration increases the density of the wastewater, and the activated sludge is easy to float upwards and run off, thereby seriously affecting the purification effect of a biological treatment system; and thirdly, the salt content is single, and if the inorganic salt is phosphate and the like with a buffering effect, a large amount of acid or alkali is added in the pH adjusting process, so that the treatment process is high in cost and generates a large amount of solid waste. The high ammonia nitrogen and high phosphorus salt chemical wastewater contains a large amount of ammonia nitrogen and inorganic salt, has the characteristics of high concentration, high salinity and difficult degradation, still lacks economic and effective treatment technology for the wastewater at the present stage,the traditional treatment process is that waste water is stripped to remove ammonia nitrogen in the waste water by adjusting pH to be strong alkalinity, then organic matters in the waste water are treated by a physical and chemical method or other low-concentration waste water is mixed for biochemical treatment, but high-concentration buffer inorganic salt enables the pH adjusting process to require a large amount of acid or alkali, so that the treatment process is high in cost and generates a large amount of solid waste, and high-concentration inorganic matters are not easy to decompose by a general physical and chemical method, so that the biochemical treatment cannot be carried out.
Through retrieval, Chinese invention patent application document, application number 201910061422.2, application date 2019.01.23 discloses a process for purifying high-salt high-ammonia nitrogen wastewater, the scheme adopts liquid caustic soda to adjust the pH of the wastewater to alkalinity and preheat, the principle that the boiling point of a liquid phase is greatly reduced under the action of a high-efficiency catalyst is utilized, the high-ammonia nitrogen wastewater and the catalyst are mixed in a separator, ammonia water is recovered at the low temperature of less than or equal to 75 ℃, the ammonia nitrogen content of the wastewater after the wastewater is treated is less than 5ppm, and the wastewater can directly reach the standard and be discharged. However, this technique has several problems: firstly, the catalyst is added into a 75 ℃ separating tower to reduce the boiling point of a liquid phase, meanwhile, the pressure of 0.25MPa is required, the water quality in the wastewater is generally complex, organic matters are easily activated under the conditions of high temperature and high pressure, the reaction is easy to occur, the catalyst is easily poisoned, the service life is reduced, meanwhile, the abrasion of the catalyst is increased under the high pressure, the catalyst after being used for many times is treated as solid waste, the operation cost is increased, and secondary pollution is caused; secondly, the raw water of the wastewater is directly adjusted to pH 11 by alkali liquor to recover ammonia water without generating solid waste, the treatment method cannot treat wastewater with high salt content and even wastewater close to saturation, otherwise, a large amount of waste salt is separated out due to excessive addition of alkali in the alkali adjusting process; and finally, the ammonia nitrogen content of the treated wastewater is lower than 5ppm, the wastewater can be directly discharged after reaching the standard, the lower the ammonia nitrogen content of the effluent is required to be after ammonia water is separated and blown off, the higher the treatment cost is, the wastewater after ammonia water recovery still contains a large amount of organic matters, the purity of the recovered ammonia water is not high due to the low-boiling-point organic matters, and the COD (chemical oxygen demand) and the total nitrogen of the treated effluent do not reach the standard due to the high-boiling-point organic matters.
In order to solve the problems that the COD content of the high-ammonia-nitrogen high-phosphorus-salt wastewater is higher after ammonia water is recovered by steam stripping, and finally the effluent cannot be discharged up to the standard, the ammonia water is recovered by steam stripping and mixed with other low-concentration wastewater for biochemical treatment, but the high-ammonia-nitrogen high-phosphorus-salt wastewater is not applicable to factories with low-concentration wastewater and high organic matter content; in order to reduce the treatment cost, the ammonia nitrogen concentration of the treated effluent of the high ammonia nitrogen wastewater is still high, the anaerobic and aerobic biochemical treatment can not meet the requirement of removing the ammonia nitrogen in the wastewater and can not reach the discharge standard of a park, namely the COD concentration is less than or equal to 500mg/L, the ammonia nitrogen concentration is less than or equal to 50mg/L and the total salt concentration is less than or equal to 3000 mg/L.
Disclosure of Invention
1. Problems to be solved
Aiming at the problems of low recovery purity of byproducts and large acid and alkali consumption in the existing treatment process of the high-ammonia-nitrogen high-phosphorus-salt wastewater, the invention provides the treatment method of the high-ammonia-nitrogen high-phosphorus-salt wastewater, the pH of the original wastewater is not required to be pretreated and adjusted by using a large amount of acid and alkali, the treated effluent can reach the discharge standard of a park, and high-purity ammonium phosphate and ammonia water can be recovered.
2. Technical scheme
In order to solve the problems, the technical scheme adopted by the invention is as follows:
a method for treating high-ammonia nitrogen high-phosphorus salt wastewater comprises the following steps:
1) distilling the wastewater, and recovering to obtain ammonium phosphate;
2) if the COD of the effluent after the distillation treatment is more than or equal to 6000mg/L, carrying out resin adsorption, and sending the effluent after the resin adsorption (namely the inlet water of the stripping tower) into the stripping tower for treatment after the pH value is adjusted to be alkaline, or
If the COD of the effluent after the distillation treatment is less than 6000mg/L, adjusting the pH of the effluent after the distillation treatment (namely the inlet water of the stripping tower) to be alkaline, and directly sending the effluent into the stripping tower for treatment;
3) and (4) performing biochemical treatment on the effluent treated by the stripping tower.
In the preferable scheme, the MVR four-effect evaporation is utilized to carry out distillation treatment on the wastewater in the step 1), and the temperature of the distillation treatment is 100-120 ℃.
Preferably, in the step 2), the pH value of inlet water of a stripping tower (outlet water after resin adsorption or outlet water after distillation treatment with COD (chemical oxygen demand) less than 6000 mg/L) is 10-13; .
Preferably, in 2), the resin is a super-crosslinked styrene resin (purchased from creative materials research center, ltd, of Jiangsu, under the model number GC-15).
Preferably, the stripping tower has the process parameters that the feeding temperature is 95-105 ℃, the working temperature at the top of the stripping tower is 115-127 ℃, and the temperature at the bottom of the stripping tower is 130-140 ℃.
Preferably, in the step 3), the effluent treated by the stripping tower is sequentially subjected to aerobic treatment, nitrification treatment and denitrification treatment.
Preferably, the COD of the effluent of the aerobic treatment is controlled to be less than or equal to 2000mg/L, and the ammonia nitrogen is controlled to be less than or equal to 200 mg/L; the ammonia nitrogen of the effluent of the nitration treatment is controlled to be less than or equal to 20 mg/L.
Preferably, the COD of the effluent of the aerobic treatment is controlled to be less than or equal to 2000mg/L, and the ammonia nitrogen is controlled to be less than or equal to 200 mg/L; the ammonia nitrogen of the effluent of the nitration treatment is controlled to be less than or equal to 20 mg/L.
Preferably, the resin adsorbed in 2) is subjected to desorption regeneration treatment by using a methanol solution, and a desorption solution is discharged after the treatment.
Preferably, the concentration of the methanol solution is more than 90%.
Preferably, the desorption liquid is mixed with effluent water after nitration and then subjected to denitrification treatment.
Preferably, the COD of the wastewater in the step 1) is 4000-60000 mg/L, the ammonia nitrogen concentration is 10000-100000 mg/L, the pH value is 5-9, and the total salt concentration is 5000-300000 mg/L.
3. Advantageous effects
Compared with the prior art, the invention has the beneficial effects that:
(1) according to the method for treating the high-ammonia-nitrogen high-phosphorus-salt wastewater, the phosphate is recovered from the production wastewater (which is phosphorus salt nearly saturated wastewater) by directly distilling raw water, so that the phosphate can be recovered in a byproduct salt form, meanwhile, the organic matter concentration of the wastewater can be obviously reduced, and the distilled water is subjected to stripping recovery treatment, so that the buffer effect caused by the high-concentration ammonia nitrogen and phosphorus salt in the production wastewater is effectively avoided; if a general treatment means is adopted, alkali is directly added into the production wastewater (which is phosphorus salt nearly saturated wastewater) to adjust the pH value for steam stripping treatment, a large amount of liquid alkali needs to be added, a large amount of solid waste can be separated out, and the subsequent treatment effect and the purity of the recovered product are influenced;
(2) the method for treating the high-ammonia-nitrogen high-phosphorus-salt wastewater provided by the invention has the advantages that the resin adsorption tower is arranged in front of the stripping tower for removing COD (chemical oxygen demand) in the wastewater, if the COD of the raw water distilled water is more than or equal to 6000mg/L, the raw water distilled water is sent into the acid-base regulation tank and then subjected to resin adsorption treatment, and the distilled water with the COD less than 6000mg/L does not need to enter the resin adsorption treatment, so that the treatment efficiency can be improved, the operation cost can be reduced, and most importantly, the high-purity ammonia water can be;
(3) the invention provides a method for treating high-ammonia nitrogen high-phosphorus salt wastewater, which comprises the steps of sending effluent of a stripping tower into an aerobic biochemical tank, carrying out aerobic treatment on microorganisms to reduce COD (chemical oxygen demand) and organic nitrogen of the wastewater, then sending the effluent into a nitrification reaction tank, carrying out nitrification treatment on the microorganisms to remove ammonia nitrogen in the wastewater, and finally sending the effluent into a denitrification reaction tank, and carrying out denitrification treatment on the microorganisms to remove nitrate nitrogen in the wastewater.
Drawings
FIG. 1 is a process flow diagram of wastewater treatment according to the present invention.
Detailed Description
The invention is further described with reference to specific examples.
Example 1
As shown in FIG. 1, the high ammonia nitrogen and high phosphorus salt wastewater is treated in the embodiment;
the steps for treating the wastewater in this example are as follows: 1) and (4) distilling the wastewater by utilizing MVR four-effect evaporation, wherein the temperature of the distillation treatment is 120 ℃, and recovering to obtain ammonium phosphate.
2) The COD of the effluent after distillation treatment is more than or equal to 6000mg/L, then resin adsorption is carried out by using the ultra-high cross-linked styrene resin, the pH of the effluent after resin adsorption is adjusted to 12 and then the effluent is sent into a stripping tower for treatment, or the COD of the effluent after distillation treatment is less than 6000mg/L, the pH of the effluent after distillation treatment is adjusted to 12 and then the effluent is directly sent into the stripping tower for treatment, and ammonia water is obtained through recovery;
the feed temperature of the stripping tower is 105 ℃, the working temperature of the top of the stripping tower is 127 ℃, and the temperature of the bottom of the stripping tower is 140 ℃.
3) Sequentially carrying out aerobic treatment on the effluent treated by the stripping tower, and controlling the pH of the inlet water to be 9 and the hydraulic retention time to be 4d by using lime milk;
then, carrying out nitration treatment on the effluent after the aerobic treatment, and controlling the pH of the influent water to be 9 by using sodium carbonate and the hydraulic retention time to be 5 d;
finally, performing denitrification treatment on the effluent after the nitrification treatment, and controlling the pH of the inlet water to be 8 by using lime milk and the hydraulic retention time to be 2 d; and the adsorbed resin realizes desorption and regeneration of the resin by using a methanol solution with the mass concentration of 99% as a regeneration liquid, the regeneration liquid firstly flows through the ultrahigh crosslinked styrene resin for elution to obtain a desorption liquid, the flow rate of the regeneration liquid flowing through the resin is controlled to be 20BV, the flow rate is 2BV/h, the washed desorption liquid is mixed with effluent water after nitrification treatment and then subjected to denitrification treatment, and a carbon source is supplemented for the denitrification treatment.
According to the method, COD, ammonia nitrogen and full salt are removed, the treated object is high ammonia nitrogen high phosphorus salt wastewater, the high ammonia nitrogen high phosphorus salt wastewater mainly contains organic pollutants of dimethylbenzene and pivalic acid, the purity of ammonium phosphate obtained by recovery is 93%, the purity of ammonia water obtained by recovery is 75%, and the content of each component in the wastewater sample before and after treatment is shown in table 1.
TABLE 1 wastewater treatment Water quality index
Example 2
As shown in FIG. 1, the high ammonia nitrogen and high phosphorus salt wastewater is treated in the embodiment;
the steps for treating the wastewater in this example are as follows:
1) and (4) distilling the wastewater by utilizing MVR four-effect evaporation, wherein the temperature of the distillation treatment is 110 ℃, and recovering to obtain ammonium phosphate.
2) The COD of the effluent after distillation treatment is more than or equal to 6000mg/L, then resin adsorption is carried out by using the ultrahigh cross-linked styrene resin, and the pH of the effluent after resin adsorption is adjusted to 11 and then the effluent is sent into a stripping tower for treatment; recovering to obtain ammonia water;
the parameters of the stripping tower treatment are that the feeding temperature is 100 ℃, the working temperature at the top of the tower is 121 ℃, and the temperature at the bottom of the tower is 135 ℃.
3) Sequentially carrying out aerobic treatment on the effluent after the treatment of the stripping tower, and controlling the pH of the inlet water to be 8 and the hydraulic retention time to be 3d by using lime milk;
then, carrying out nitration treatment on the effluent after the aerobic treatment, and controlling the pH of the influent water to be 8.5 by using sodium carbonate and the hydraulic retention time to be 4 d;
finally, performing denitrification treatment on the effluent after the nitrification treatment, and controlling the pH of the inlet water to be 7.5 by using lime milk and the hydraulic retention time to be 1.5 d; and the adsorbed resin realizes desorption and regeneration of the resin by using a methanol solution with the mass concentration of 95% as a regeneration liquid, the regeneration liquid firstly flows through the ultrahigh crosslinked styrene resin for elution to obtain a desorption liquid, the flow rate of the regeneration liquid flowing through the resin is controlled to be 15BV, the flow rate is 1.5BV/h, and the washed desorption liquid is mixed with effluent water after nitrification treatment and then subjected to denitrification treatment to supplement a carbon source for the denitrification treatment.
According to the method, COD, ammonia nitrogen and full salt are removed, the treated object is high ammonia nitrogen high phosphorus salt wastewater, the high ammonia nitrogen high phosphorus salt wastewater mainly contains organic pollutants of dimethylbenzene and pivalic acid, the purity of ammonium phosphate obtained by recovery is 91%, the purity of ammonia water obtained by recovery is 82%, and the content of each component in the wastewater sample before and after treatment is shown in Table 2.
TABLE 2 wastewater treatment Water quality index
Example 3
As shown in FIG. 1, the high ammonia nitrogen and high phosphorus salt wastewater is treated in the embodiment;
the steps for treating the wastewater in this example are as follows:
1) and (4) distilling the wastewater by utilizing MVR four-effect evaporation, wherein the temperature of the distillation treatment is 100 ℃, and recovering to obtain ammonium phosphate.
2) The COD of the effluent after the distillation treatment is less than 6000mg/L, the pH of the effluent after the distillation treatment is adjusted to 10 and then the effluent is directly sent into a stripping tower for treatment, and ammonia water is obtained through recovery;
the feeding temperature of ammonium phosphate is 95 ℃, the working temperature of the top of the tower is 115 ℃, and the temperature of the bottom of the tower is 130 DEG C
3) Sequentially carrying out aerobic treatment on the effluent treated by the stripping tower, and controlling the pH of the inlet water to be 7 and the hydraulic retention time to be 2d by using lime milk;
then, carrying out nitration treatment on the effluent after the aerobic treatment, and controlling the pH of the influent water to be 9 by using sodium carbonate and the hydraulic retention time to be 3 d;
finally, performing denitrification treatment on the effluent after the nitrification treatment, and controlling the pH of the inlet water to be 7 by using lime milk, wherein the hydraulic retention time is 1 d; and the adsorbed resin realizes desorption and regeneration of the resin by using a methanol solution with the mass concentration of 90% as a regeneration liquid, the regeneration liquid firstly flows through the ultrahigh crosslinked styrene resin for elution to obtain a desorption liquid, the flow rate of the regeneration liquid flowing through the resin is controlled to be 10BV, the flow rate is 2BV/h, the washed desorption liquid is mixed with effluent water after nitrification treatment and then subjected to denitrification treatment, and a carbon source is supplemented for the denitrification treatment.
According to the method, COD, ammonia nitrogen and full salt are removed, the treated object is high ammonia nitrogen high phosphorus salt wastewater, the high ammonia nitrogen high phosphorus salt wastewater mainly contains organic pollutants of dimethylbenzene and pivalic acid, the purity of the ammonium phosphate obtained by recovery is 90%, the purity of the ammonia water obtained by recovery is 88%, and the content of each component in the wastewater sample before and after treatment is shown in Table 3.
TABLE 3 wastewater treatment Water quality index
Comparative example 1
This comparative example is substantially the same as example 1 except that:
the steps of treating the wastewater in this comparative example were as follows:
step 1) same as example 1;
2) directly feeding the distilled effluent into a stripping tower for treatment without resin adsorption treatment;
step 3) the same as in example 1.
The COD, ammonia nitrogen and total salt are removed in the method, the purity of the recovered ammonium phosphate is 90 percent and the purity of the recovered ammonia water is 55 percent in the same manner as in example 1 for the wastewater treatment, and the content of each component in the wastewater sample before and after the wastewater treatment is shown in Table 4.
TABLE 4 wastewater treatment Water quality index
As can be seen from Table 4, the COD concentration of the wastewater is high, the COD of the wastewater cannot be effectively reduced by distillation and stripping treatment, the sludge loading is too high due to the too high organic matter concentration, the sludge adsorption performance is poor, the organic matter cannot be completely decomposed, the sludge structure is loose, the activity is poor, and the wastewater cannot be biochemically treated.
Comparative example 2
This comparative example is substantially the same as example 1 except that:
the steps of treating the wastewater in this comparative example were as follows:
1) adjusting the pH value of raw water to 12 instead, recovering to obtain ammonium phosphate, and not utilizing MVR (mechanical vapor recompression) four-effect evaporation to distill wastewater;
step 2), adjusting the COD of the effluent after pH adjustment to be more than or equal to 6000mg/L, then carrying out resin adsorption by using the ultrahigh cross-linked styrene resin, adjusting the pH of the effluent after resin adsorption to 12, and then sending the effluent into a stripping tower for treatment, or directly sending the effluent after pH adjustment to be more than or equal to 6000mg/L into the stripping tower for treatment; recovering to obtain ammonia water;
the feed temperature of the stripping tower is 105 ℃, the working temperature of the top of the stripping tower is 127 ℃, and the temperature of the bottom of the stripping tower is 140 ℃.
Step 3) the same as in example 1.
The COD, ammonia nitrogen and total salt are removed in the method, the purity of the recovered ammonium phosphate is 30 percent and the purity of the recovered ammonia water is 77 percent in the same manner as in example 1 for the wastewater treatment, and the content of each component in the wastewater sample before and after the treatment is shown in Table 5.
TABLE 5 wastewater treatment Water quality index
As can be seen from Table 5, the salinity of the wastewater is high, and the aerobic bacteria can lose activity due to the excessively high salinity under the condition of not performing distillation desalination, the existing halotolerant bacteria can bear the salinity of 25% at most, and the biochemical rate is reduced due to the excessively high salinity, so that the wastewater can not be biochemically treated under the condition of evaporation desalination.
Comparative example 3
This comparative example is substantially the same as example 1 except that:
the steps of treating the wastewater in this comparative example were as follows:
1) and (3) performing resin adsorption on the wastewater by using the ultra-high cross-linked styrene resin, adjusting the effluent after the resin adsorption directly, and then sending the effluent into MVR four-effect evaporation to perform distillation treatment on the wastewater, and recovering to obtain ammonium phosphate.
2) Directly feeding the distilled effluent into a stripping tower for treatment, and recovering to obtain ammonia water;
the feed temperature of the stripping tower is 105 ℃, the working temperature of the top of the stripping tower is 127 ℃, and the temperature of the bottom of the stripping tower is 140 ℃.
Step 3) the same as in example 1.
The COD, ammonia nitrogen and total salt are removed in the method, the purity of the recovered ammonium phosphate is 92 percent and the purity of the recovered ammonia water is 78 percent in the same manner as in example 1 for the wastewater treatment, and the content of each component in the wastewater sample before and after the wastewater treatment is shown in Table 6.
TABLE 6 wastewater treatment quality index
As can be seen from Table 6, the treatment method was comparable to that obtained in example 1 in treatment effect, because the effect of distillation on COD of wastewater was not so great, and the effect of adsorption of the resin before or after distillation on the overall treatment effect was not so great. However, an excessively high salt concentration has a certain influence on the life of the resin, and particularly, the salt in the wastewater close to saturation tends to block the resin pores, deteriorating the regeneration effect thereof, and thus is not suitable for industrial application.
Comparative example 4
This comparative example is substantially the same as example 1 except that:
the steps of treating the wastewater in this comparative example were as follows:
step 1) is the same as in example 1.
2) Directly feeding the distilled effluent into a stripping tower for treatment, and recovering to obtain ammonia water;
the feed temperature of the stripping tower is 105 ℃, the working temperature of the top of the stripping tower is 127 ℃, and the temperature of the bottom of the stripping tower is 140 ℃.
3) Adsorbing the effluent resin treated by the stripping tower by using the ultrahigh crosslinked styrene resin;
4) effluent after resin adsorption is subjected to biochemical treatment including aerobic treatment, nitrification treatment and denitrification treatment in sequence;
the aerobic treatment, nitrification treatment and denitrification treatment conditions were the same as in example 1.
The COD, ammonia nitrogen and total salt are removed in the method, the purity OR of the ammonium phosphate obtained by recycling the wastewater is 91 percent and the purity of the ammonia water obtained by recycling the wastewater is 50 percent in the same way as in example 1, and the contents of all components of the wastewater sample before and after the treatment are shown in Table 7.
TABLE 7 wastewater treatment quality index
As can be seen from Table 7, the treatment method is not much different from the treatment effect obtained in example 1, but the purity of the recovered ammonia water is obviously lowered because the concentration of organic matters in the wastewater is high and contains a large amount of low-boiling-point small molecules, and during the stripping process, some small-molecule organic matters enter the recovered ammonia water together with free ammonia to cause the purity of the ammonia water to be lowered, so that the resin adsorption is performed before the ammonia water is stripped and recovered.
Claims (10)
1. A method for treating high-ammonia nitrogen high-phosphorus salt wastewater is characterized by comprising the following steps: the method comprises the following steps:
1) carrying out distillation treatment on the wastewater;
2) if the COD of the effluent after the distillation treatment is more than or equal to 6000mg/L, carrying out resin adsorption, and sending the effluent after the resin adsorption into a stripping tower for treatment, or
If the COD of the effluent after the distillation treatment is less than 6000mg/L, directly feeding the effluent after the distillation treatment into a stripping tower for treatment;
the pH of inlet water of the stripping tower is adjusted to be alkaline during treatment;
3) and (4) performing biochemical treatment on the effluent treated by the stripping tower.
2. The method for treating high ammonia nitrogen and high phosphorus salt wastewater according to claim 1, which is characterized in that: and 1) carrying out distillation treatment on the wastewater by utilizing MVR four-effect evaporation, wherein the temperature of the distillation treatment is 100-130 ℃.
3. The method for treating high ammonia nitrogen and high phosphorus salt wastewater according to claim 1, which is characterized in that: the resin in the step 2) is a super-crosslinked styrene resin; and adjusting the pH of inlet water of the stripping tower to 10-13 during treatment.
4. The method for treating high ammonia nitrogen and high phosphorus salt wastewater according to claim 1, which is characterized in that: the feeding temperature of the stripping tower in the step 2) is 95-105 ℃, the working temperature of the top of the stripping tower is 115-127 ℃, and the temperature of the bottom of the stripping tower is 130-140 ℃.
5. The method for treating high ammonia nitrogen and high phosphorus salt wastewater according to claim 4, which is characterized in that: and in the step 3), the effluent treated by the stripping tower is sequentially subjected to aerobic treatment, nitrification treatment and denitrification treatment.
6. The method for treating high ammonia nitrogen and high phosphorus salt wastewater according to claim 5, which is characterized in that: the COD of the effluent of the aerobic treatment is controlled to be less than or equal to 2000mg/L, and the ammonia nitrogen is controlled to be less than or equal to 200 mg/L; the ammonia nitrogen of the effluent of the nitration treatment is controlled to be less than or equal to 20 mg/L.
7. The method for treating high ammonia nitrogen and high phosphorus salt wastewater according to claim 5, which is characterized in that: desorbing and regenerating the resin adsorbed in the step 2) by using a methanol solution, and discharging desorption liquid after treatment.
8. The method for treating high ammonia nitrogen and high phosphorus salt wastewater according to claim 5, which is characterized in that: the concentration of the methanol solution is more than 90%.
9. The method for treating high ammonia nitrogen and high phosphorus salt wastewater according to claim 6, which is characterized in that: mixing the desorption liquid with effluent after nitration treatment and then carrying out denitrification treatment.
10. The method for treating high-ammonia-nitrogen high-phosphorus-salt wastewater according to any one of claims 1 to 9, which is characterized by comprising the following steps: the COD of the wastewater in the step 1) is 4000-60000 mg/L, the ammonia nitrogen concentration is 10000-100000 mg/L, the pH value is 5-9, and the total salt concentration is 5000-300000 mg/L.
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| CN108002661A (en) * | 2017-12-29 | 2018-05-08 | 什邡市长丰化工有限公司 | A kind of nitrogenous, phosphorus waste water processing method |
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| US20080053909A1 (en) * | 2006-09-06 | 2008-03-06 | Fassbender Alexander G | Ammonia recovery process |
| CN105601020A (en) * | 2016-03-30 | 2016-05-25 | 北京赛科康仑环保科技有限公司 | Treatment technology of raffinate wastewater of nickel, cobalt and manganese |
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