CN111115934A - Desulfurization ammonia nitrogen wastewater treatment method - Google Patents
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Abstract
The utility model provides a desulfurization ammonia nitrogen waste water treatment method, desulfurization ammonia nitrogen waste water treatment system device that this method used includes the former water preliminary sedimentation pond that is used for waste water to deposit and retrieves heavy metal, the coagulation reaction sediment device that is used for deposiing to retrieve heavy metal, a calcium magnesium removal device that is used for getting rid of calcium magnesium ion, a negative pressure deamination system that is used for the deamination, an electric flocculation device that is used for flocculating to get rid of surplus heavy metal, and be used for exhaust gas treatment's ammonia cleaner, ammonia cleaner inside is provided with the water-locator, ammonia cleaner's water-locator below is provided with the water seal structure. According to the invention, by arranging the negative pressure deamination system, the deamination temperature in the whole deamination process is reduced by utilizing the principle that the liquid phase boiling point is greatly reduced under the negative pressure state, so that the whole system can perform high-efficiency deamination under the relatively low temperature state, the energy consumption can be greatly reduced, and the steam consumption is reduced; ammonia water and heavy metal can be recycled while ammonia nitrogen and heavy metal are removed, waste is turned into wealth, and secondary pollution is prevented.
Description
Technical Field
The invention belongs to the technical field of desulfurization wastewater treatment, and relates to a desulfurization ammonia nitrogen wastewater treatment method.
Background
Ammonia nitrogen sewage generated in the industrial production process can cause serious water pollution and affect the pollution of ground water, underground water, soil and crops. Therefore, ammonia nitrogen sewage needs to be treated and then discharged, and ammonia water is used as an energy source and can be recycled. In the prior art, the conventional scheme is an ammonia distillation process, ammonia-containing nitrogen water is boiled to be deaminated by utilizing high temperature in a tower, ammonia steam is condensed by a condenser, dilute ammonia water is recycled, and the reflux ratio is controlled to reach the required ammonia water concentration. However, the existing ammonia distillation process has large steam consumption (130-.
In addition, in actual use, the source of ammonia nitrogen sewage is often not only one, especially in the ammonia-acid method flue gas desulfurization treatment process, besides the sintering limestone-gypsum wet desulfurization waste water, acid making system waste water and ammonia station system waste water, if the waste water is treated respectively, a plurality of sets of waste water treatment systems are needed, the equipment cost is high, and the occupied area is large. And the wastewater has high water hardness and heavy metals, and has more suspended matters, if ammonia is directly stripped and evaporated, the deamination effect is poor, tower plates are easy to scale, and the heavy metals are also mixed with lime residues together, so that the subsequent treatment is difficult.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a method for treating desulfurization ammonia nitrogen wastewater.
In order to achieve the purpose, the invention adopts the following technical scheme:
the utility model provides a desulfurization ammonia nitrogen effluent disposal system device, is including the former water primary sedimentation pond that is used for waste water to deposit, the coagulation reaction who is used for deposiing retrieving heavy metal deposits the device, be used for getting rid of calcium magnesium ion remove calcium magnesium device, be used for deaminating negative pressure deamination system, be used for the electric flocculation device that the flocculation got rid of surplus heavy metal and be used for tail gas treatment wash ammonia purifier, wash the inside water-locator that is provided with of ammonia purifier, the water-locator below of washing ammonia purifier is provided with the water seal structure, the water seal structure includes will wash the ammonia purifier and separate into upper and lower two parts the baffle, run through to the intake pipe of baffle below, with the L type pipe of intake pipe top intercommunication, the horizontal segment of L type pipe is located keeps away from the water-locator and is close to baffle one end, the.
Further, the pond top closing cap in raw water primary sedimentation pond, the former water catch basin is passed through the pipe connection to the supernatant output in raw water primary sedimentation pond, the sediment output of raw water primary sedimentation pond bottom passes through the pipeline and the pump machine is connected one number of plate frame pressure filter, one number of plate frame pressure filter's filtrating output passes through the pipe connection raw water catch basin.
Further, the output of raw water catch basin passes through the pipeline and goes out the water pump and connects coagulation reaction sediment device, the supporting lift pump that thoughtlessly congeals, No. two plate frame pressure filters and charge device that is provided with of coagulation reaction sediment device, charge device is used for adding the heavy metal catching agent, No. two plate frame pressure filter's filtrating output passes through the pipe connection raw water catch basin.
Further, the waste water output end of coagulation reaction sedimentation device connects through a line mixer and removes the calcium magnesium device, a line mixer has the alkali lye storage tank through the pipe connection, it has analytic liquid storage tank through the pipe connection to remove the calcium magnesium device, the hydrous precipitate of removing the calcium magnesium device passes through pipe connection re-reaction unit, be the inside retort that is provided with the agitator at reaction unit, re-reaction unit passes through pipeline input acid raw water, No. three plate frame pressure filters of sludge transfer pump and pipe connection are passed through to re-reaction unit's output, No. three plate frame pressure filters's filtrating output passes through the raw water catch basin of pipe connection.
Further, the waste water output of calcium magnesium removal device passes through the pipe connection decalcification pond, the decalcification pond adopts vertical flow sedimentation tank, the inner wall of decalcification pond adopts the anticorrosive material preparation to form, the mud output of decalcification pond passes through mud delivery pump and pipe connection device of reacting again, the supernatant output of decalcification pond passes through the middle pond of pipe connection, the output in middle pond passes through No. two pipe-line mixer and connects the negative pressure deamination system, No. two pipe-line mixers are connected with the alkali supplementation system, the alkali supplementation system is including the alkali lye basin that is used for storing alkali lye, the PH appearance that is used for detecting PH, the alkali device that adds that is used for adding alkali lye.
Further, the negative pressure deamination system comprises a negative pressure deamination tower, a preheater and a condenser, wherein the heat source input end of the preheater is connected with the tower bottom of the negative pressure deamination tower, the input end of the preheater is connected with a second pipeline mixer through a pipeline, the output end of the preheater is connected with the input end of the negative pressure deamination tower through a lift pump, the negative pressure deamination tower is connected with a saturated steam storage tank through a pipeline, the ammonia steam output end at the top of the negative pressure deamination tower is connected with a condenser, the diluted ammonia water condensed by the condenser is connected with a gas-liquid separation tank through a pipeline, the gas-liquid separation tank reflows the diluted ammonia water to the negative pressure deamination tower through a pipeline, the ammonia gas output end of the condenser is connected with an ammonia recovery device through a pipeline, the ammonia recovery device is a rectifying tower, the packing inside the ammonia recovery device is replaced by a Z-shaped tower plate, and the non-condensable gas output end of the ammonia recovery device is connected with an ammonia washing purifier through a pipeline.
Further, the waste water at the bottom of the negative pressure deamination tower squeezes into the electric flocculation device after the pre-heater heat transfer, the electric flocculation device has the acid solution storage tank through the pipe connection, the mud output of electric flocculation device passes through the pipe connection heavy metal pressure filter, the play water outlet end of electric flocculation device passes through pipe connection PH back regulation pond, PH back regulation pond has the alkali lye storage tank through the pipe connection, the play water outlet end in PH back regulation pond passes through the pipe connection play water pond.
A method for treating desulfurization ammonia nitrogen wastewater uses any one of the desulfurization ammonia nitrogen wastewater treatment system devices.
Further, the method comprises the following steps:
s1, intensively discharging the raw wastewater into a raw water primary sedimentation tank through a pipeline, precipitating, pumping the precipitate into a first plate-frame filter press by a pump to remove impurity slag in the raw water, and roasting the impurity slag;
s2, enabling supernatant subjected to precipitation treatment to flow into a raw water collecting tank, pumping the supernatant into a coagulation reaction precipitation device by a pump, adding a heavy metal capture agent, precipitating and recovering heavy metals, and conveying sludge containing the heavy metals to a second plate-frame filter press for filtering and then sintering;
s3, adding alkali into the wastewater with heavy metal recovered by a pump through a pipeline mixer to adjust the pH value to be more than 12, pumping the wastewater into a calcium and magnesium removing device, adding an analytic solution to remove calcium and magnesium ions, pumping the water-containing precipitate into a re-reaction device by the pump, adjusting the pH value to be neutral with acidic raw water, sending the water-containing precipitate to a third plate-and-frame filter press to perform slag-water separation treatment, and recovering calcium salt;
s4, after calcium is resolved and removed, the wastewater enters a decalcification sedimentation tank for clarification, clear liquid flows into an intermediate water tank, alkali is supplemented to pH 11 through a pipeline mixer, effluent is preheated by a preheater and then enters a negative pressure deamination tower, free ammonia is continuously separated by a tower plate and concentrated towards the tower top under the action of a V-shaped tower plate and steam, ammonia gas at the tower top enters a condenser, condensate liquid flows back to the negative pressure deamination tower, the ammonia gas enters an ammonia recovery device through an ammonia extraction mixer for recovering ammonia water, and tail gas is purified and discharged by an ammonia washing purifier;
and (3) adding acid into the tower bottom wastewater subjected to the deamination treatment of S5 to adjust the pH value to 3-4, then removing residual heavy metals by using an electric flocculation device, adjusting the pH value of effluent to 6-9, and then discharging.
Further, in the step S4, ammonia station wastewater is also pumped into the intermediate water tank, and the ammonia distillation temperature in the negative pressure deamination tower is 55-65 ℃.
According to the method for treating the desulfurization ammonia nitrogen wastewater, the deamination temperature in the whole deamination process is reduced by setting the negative pressure deamination system and utilizing the principle that the liquid-phase boiling point is greatly reduced in a negative pressure state, so that the whole system can perform high-efficiency deamination in a relatively low-temperature state, the energy consumption can be greatly reduced, and the steam consumption is reduced;
according to the invention, the ammonia recovery device is used for rectifying, and the ammonia water concentration is completed in a manner of absorbing by the ammonia washing purifier, so that the problem of ammonia nitrogen content change of wastewater in a reflux regulation method can be dynamically solved, the flow rate of an absorption process of the ammonia washing recovery tower is controlled, the required ammonia water concentration is obtained, and the operation is stable;
according to the invention, through the arrangement of the calcium and magnesium removing device, in the wastewater treatment process, the hardness of water quality can be reduced by adding the analytic liquid, so that the problem of scaling of a system device is avoided, the repeated pickling of the equipment is frequent, the operation is difficult, the analytic liquid converts calcium ions into calcium salt precipitate, and the calcium salt is favorably recycled;
according to the invention, the water seal structure is arranged in the ammonia washing purifier, so that the non-condensable gas is prevented from being directly discharged from the top of the ammonia washing purifier, and the discharged tail gas can be discharged up to the standard;
in conclusion, the invention can recover ammonia water and heavy metal while ensuring the removal of ammonia nitrogen and heavy metal, changes waste into valuable and prevents secondary pollution.
Drawings
FIG. 1 is a schematic diagram of a system for treating desulfurized ammonia nitrogen wastewater according to the invention;
FIG. 2 is a schematic view of a process for treating desulfurized ammonia nitrogen wastewater according to the invention;
fig. 3 is an enlarged schematic view at a of fig. 1.
In the figure: 1. a raw water primary sedimentation tank; 2. a raw water collecting tank; 3. a coagulation reaction precipitation device; 4. a calcium and magnesium removal device; 5. a decalcification sedimentation tank; 6. a middle water tank; 7. a preheater; 8. a negative pressure deamination tower; 9. an electrocoagulation device; 10. the PH value is adjusted back to the pool; 11. a water outlet pool; 12. a first plate-frame filter press; 13. a second plate-frame filter press; 14. a re-reaction device; 15. a third plate-frame filter press; 16. heavy metal filter press; 17. a condenser; 18. a gas-liquid separation tank; 19. an ammonia extraction mixer; 20. an ammonia recovery unit; 21. washing ammonia purifier; 22. a water distributor; 23. a partition plate; 24. an air inlet pipe; 25. an L-shaped pipe; 26. a water seal structure.
Detailed Description
In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the invention easy to understand, the invention is further described with the specific embodiments. The method for treating the desulfurized ammonia nitrogen wastewater is not limited to the description of the following examples.
Example 1
Referring to fig. 1 and 3, a desulfurization ammonia nitrogen wastewater treatment system device comprises a raw water primary sedimentation tank 1 for wastewater sedimentation, a coagulation reaction sedimentation device 3 for precipitating and recovering heavy metals, a calcium and magnesium removal device 4 for removing calcium and magnesium ions, a negative pressure deamination system for deamination, an electric flocculation device 9 for flocculating and removing residual heavy metals, and an ammonia washing purifier 21 for tail gas treatment, wherein the ammonia washing purifier 21 is selected from, but not limited to, WDJHT-2000 type, a water distributor 22 is arranged inside the ammonia washing purifier 21, a water sealing structure 26 is arranged below the water distributor 22 of the ammonia washing purifier 21, the water sealing structure 26 comprises a partition plate 23 for dividing the ammonia washing purifier 21 into an upper part and a lower part, an air inlet pipe 24 penetrating below the partition plate 23, and an L-shaped pipe 25 communicated with the top of the air inlet pipe 24, the horizontal part of the L-shaped pipe 25 is positioned at one end far away from the water distributor 22 and close to the, a plurality of air nozzles are distributed on the horizontal part of the L-shaped pipe 25.
Through adopting above-mentioned technical scheme, through setting up water seal structure 26 in washing ammonia clarifier 21, avoid noncondensable gas directly to discharge from washing ammonia clarifier 21's top, guarantee that the tail gas of emission can discharge to reach standard.
Referring to fig. 1, the pool top closing cap of raw water primary sedimentation tank 1, raw water primary sedimentation tank 1 bury the steel concrete structure for ground, and the inner wall adopts anticorrosive material to make, the supernatant output of raw water primary sedimentation tank 1 passes through pipe connection raw water catch basin 2, the precipitate output of raw water primary sedimentation tank 1 bottom passes through the pipeline and pump machine connects a board frame pressure filter 12, and the model of a board frame pressure filter 12 adopts but not limited to XAJ80/800 type, the filtrating output of a board frame pressure filter 12 passes through pipe connection raw water catch basin 2, and raw water catch basin 2 buries the steel concrete structure for ground, pool top closing cap.
Referring to fig. 1, the output of raw water catch basin 2 passes through the pipeline and goes out the water pump and connects coagulation reaction sediment device 3, and coagulation reaction sediment device 3 adopts but not limited to HNFYQ-2000 type, the supporting coagulation elevator pump that is provided with of coagulation reaction sediment device 3, No. two plate frame pressure filter 13 and charge device, charge device is used for adding the heavy metal trapping agent, and sodium sulfide is chooseed for use to the heavy metal trapping agent, No. two plate frame pressure filter 13's filtrating output passes through pipe connection raw water catch basin 2, No. two plate frame pressure filter 13 chooses for use but not limited to XAJ20/630 type.
Referring to fig. 1, the waste water output end of the coagulation reaction sedimentation device 3 is connected with a calcium and magnesium removing device 4 through a first pipeline mixer, the first pipeline mixer is connected with an alkali liquor storage tank through a pipeline, the calcium and magnesium removing device 4 adopts a JXFYT-500 type analysis reaction device and a JXFLT-1400 type analysis separation device, the calcium and magnesium removing device 4 is connected with a analytic solution storage tank through a pipeline, the hydrous sediment of the calcium and magnesium removing device 4 is connected with a re-reaction device 14 through a pipeline, the reaction device is a reaction tank with a stirrer arranged inside, the re-reaction device 14 inputs acid raw water through a pipeline, the output end of the re-reaction device 14 is connected with a third plate-and-frame filter press 15 through a sludge delivery pump and a pipeline, the third plate-and-frame filter press 15 is selected from but not limited to XAJ80/800 type, and the filtrate output end of the third plate-frame filter press 15 is connected with the raw water collecting tank 2 through a pipeline.
Through adopting above-mentioned technical scheme, through the setting that removes calcium magnesium device 4, in waste water treatment process, can reduce the hardness of quality of water earlier through adding analytic liquid, avoid the problem that system's device appears the scale deposit, cause equipment to carry out the pickling repeatedly frequently, the operation difficulty, analytic liquid converts calcium ion into calcium salt sediment, is favorable to recycling calcium salt, and the calcium salt principal ingredients is CaCO3It can be used as sintering flux.
Referring to fig. 1, the waste water output end of the calcium and magnesium removing device 4 is connected with a decalcification sedimentation tank 5 through a pipeline, the decalcification sedimentation tank 5 adopts a vertical flow sedimentation tank, the decalcification sedimentation tank 5 is of a steel concrete structure, the inner wall of the decalcification sedimentation tank 5 is made of an anticorrosive material, the sludge output end of the decalcification sedimentation tank 5 is connected with a re-reaction device 14 through a sludge delivery pump and a pipeline, the supernatant output end of the decalcification sedimentation tank 5 is connected with an intermediate water tank 6 through a pipeline, the intermediate water tank 6 is of a steel concrete structure, the inner wall of the intermediate water tank is made of an anticorrosive material, a tank top sealing cover is arranged, the output end of the intermediate water tank 6 is connected with a negative pressure deamination system through a second pipeline mixer, the second pipeline mixer is connected with an alkali supplementing system, the alkali supplementing system comprises an, An alkali adding device for adding alkali liquor.
Referring to fig. 1, the negative pressure deamination system comprises a negative pressure deamination tower 8, a preheater 7 and a condenser 17, wherein the heat source input end of the preheater 7 is connected with the tower bottom of the negative pressure deamination tower 8, the water temperature at the tower bottom is 60-65 ℃, the negative pressure deamination tower 8 is selected from but not limited to FYTAT-800-II type, the input end of the preheater 7 is connected with a second pipeline mixer through a pipeline, the preheater 7 is selected from but not limited to WDYR-10 type, the output end of the preheater 7 is connected with the input end of the negative pressure deamination tower 8 through a lift pump, the negative pressure deamination tower 8 is connected with a saturated steam storage tank through a pipeline, the ammonia steam output end at the top of the negative pressure deamination tower 8 is connected with the condenser 17, the condenser 17 is selected from but not limited to LN-40 type, the dilute ammonia water condensed by, the ammonia-liquid separation tank 18 is used for refluxing dilute ammonia water to the negative-pressure deamination tower 8 through a pipeline, the ammonia output end of the condenser 17 is connected with the ammonia recovery device 20 through a pipeline, the ammonia recovery device 20 is a rectifying tower, a filler in the ammonia recovery device 20 is replaced by a Z-shaped tower plate, the Z-shaped tower plate has the advantages of low resistance drop, high separation efficiency and particle resistance, the non-condensable gas output end of the ammonia recovery device 20 is connected with the ammonia washing purifier 21 through a pipeline, the ammonia recovery device 20 is selected from and limited to XAHST-800-II, dilute ammonia water is generated after condensation is converted into liquid for refluxing, non-condensed ammonia gas enters the ammonia recovery device 20, 15-18% of concentrated ammonia water is recycled through cyclic absorption, and the non-condensable gas is discharged after being purified by the ammonia washing purification tower.
Through adopting above-mentioned technical scheme, through the setting of negative pressure deamination system, utilized liquid phase boiling point greatly reduced's under the negative pressure state principle for whole deamination in-process deamination temperature obtains reducing, thereby makes entire system can carry out high-efficient deamination under relative low temperature state, can greatly reduced energy consumption, the reduction steam consumption.
According to the traditional ammonia water recovering process by deamination, in order to ensure the concentration of product ammonia water, the temperature of the tower top needs to be adjusted by backflow, so that the concentration of the ammonia water is changed, when the ammonia content in wastewater is low, a large backflow amount is needed, a system is not in an optimal operation state, the energy consumption is increased, the ammonia content in steam is controlled by backflow, and the control mode is unstable. The ammonia concentration device is used for rectifying by the ammonia recovery device 20, and the ammonia water concentration is completed by the absorption mode of the ammonia washing purifier 21, so that the problem of ammonia nitrogen content change of the wastewater in the reflux regulation method can be dynamically solved, the flow rate of the absorption process of the ammonia washing recovery tower is controlled, the required ammonia water concentration is obtained, and the operation is stable.
Referring to fig. 1, the waste water at the bottom of negative pressure deamination tower 8 is thrown into electrocoagulation device 9 after preheater 7 heat transfer, and electrocoagulation device 9 chooses for use but not limited to WDXN-5 type, electrocoagulation device 9 has the acid solution storage tank through the pipe connection, the mud output of electrocoagulation device 9 passes through pipe connection heavy metal filter press 16, the play water end of electrocoagulation device 9 passes through pipe connection PH back regulation pond 10, PH back regulation pond 10 has the alkali lye storage tank through pipe connection, the play water end of PH back regulation pond 10 passes through pipe connection play water pool 11.
The desulfurization ammonia nitrogen wastewater treatment system device adopts an automatic system of SIEMENS to control the production and operation process of a sewage treatment system. The real-time parameters of the process are monitored, managed and operated in a central control room through an engineer station and an operator station, equipment control is controlled by a lower PLC cabinet, and the PLC is selected from Siemens company S7-200 series products, so that the purposes of stable and reliable operation of control equipment and convenience in management and maintenance are achieved. The GCS power cabinet of the control room supplies power to field power equipment, wherein the GCS power cabinet comprises a water pump, a metering pump, a field box and the like.
In the whole process, an operator station is independently arranged in a control room, and 1 industrial personal computer is adopted to monitor and operate all equipment in a boundary area. Each operator station is matched with a corresponding automatic control system, the automatic control system adopts a German Siemens S7-200 system, and the running state, fault alarm, parameter setting, operation instructions and the like of all electric control equipment in a boundary area are brought into the system, so that the working intensity of operators is reduced.
Example 2
In the embodiment, ammonia nitrogen in 125t/d total wastewater of a certain company is treated and ammonia water is recycled, wherein the total amount of the wastewater is three, one is sintered limestone-gypsum wet desulphurization wastewater, the water amount is 5t/h, and the wastewater contains a large amount of calcium ions and suspended matters; the other strand is dry desulfurization wastewater, namely acidic raw water with the water amount of 1.5t/h and containing a large amount of sulfuric acid and suspended matters; the third waste water is the waste water of an ammonia station system, the water amount is 5t/d, and the ammonia content is about 5 percent; the relevant parameters of the wastewater are shown in table 1.
Table 1 ammonia nitrogen wastewater relevant parameters, treated water amount: 125t/d, calculated as 5.5t/h
| Project (mg/L) | Waste water of wet desulfurization | Dry desulfurization of waste water | Ammonia plant system wastewater |
| Amount of water (t/h) | 5 | 1.5 | 0.5 |
| pH | 4-6 | / | / |
| SS | 70000 | 6000 | / |
| Ammonia nitrogen | 2000 | 8000 | 50000 |
| Ca2+ | 100000 | / | / |
| Lead (II) | <120 | <0.8 | / |
| Copper (Cu) | <5 | <0.6 | / |
| Iron | <200 | <35 | / |
| Zinc | <25 | <2.5 | / |
| Chromium (III) | <0.2 | <0.24 | / |
| Cadmium (Cd) | <1.5 | <0.05 | / |
| Nickel (II) | <0.2 | / | / |
| Mercury | <150 | - |
A method for treating desulfurization ammonia nitrogen wastewater, which uses the system device for treating desulfurization ammonia nitrogen wastewater in the embodiment.
The method comprises the following steps:
s1, intensively discharging the raw wastewater into a raw water primary sedimentation tank 1 through a pipeline, precipitating, pumping the precipitate into a first plate-frame filter press 12 by a pump to remove impurity slag in the raw water, and roasting the impurity slag;
s2, enabling supernatant subjected to precipitation treatment to flow into a raw water collecting tank 2, pumping the supernatant into a coagulation reaction precipitation device 3 by a pump, adding a heavy metal capture agent, precipitating and recovering heavy metals, and conveying sludge containing the heavy metals to a second plate-and-frame filter press 13 for filtering and then sintering;
s3, adding alkali into the wastewater with heavy metal recovered by a pump through a pipeline mixer to adjust the pH value to be more than 12, pumping the wastewater into a calcium and magnesium removing device 4, adding an analytic solution to remove calcium and magnesium ions, pumping the water-containing precipitate into a re-reaction device 14 by the pump, adjusting the pH value to be neutral by acidic raw water, sending the water-containing precipitate to a third plate-and-frame filter press 15 to perform slag-water separation treatment, and recovering calcium salt;
s4, after calcium is resolved and removed, the wastewater enters a decalcification sedimentation tank 5 to be clarified, clear liquid flows into an intermediate water tank 6, the wastewater of an ammonia station is pumped into the intermediate water tank 6, alkali is supplemented to PH 11 through a pipeline mixer, effluent is preheated by a preheater 7 and then enters a negative pressure deamination tower 8, the requirement of the negative pressure deamination on steam pressure is low, the steam pressure is less than or equal to 0.25MPa, ammonia nitrogen is more likely to volatilize under the negative pressure, the ammonia nitrogen removal rate can be more than or equal to 99.9% at the highest, and the ammonia nitrogen at the bottom of the tower can be less; the recovery rate of ammonia nitrogen can reach 99 percent; under the action of a V-shaped tower plate and steam, the temperature of ammonia distillation in the negative pressure deamination tower 8 is 60 ℃, free ammonia is continuously separated by the tower plate and concentrated to the tower top, ammonia gas at the tower top enters a condenser 17, condensate liquid flows back to the negative pressure deamination tower 8, the ammonia gas enters an ammonia recovery device 20 through an ammonia extraction mixer 19 to recover ammonia water, and tail gas is purified by an ammonia washing purifier 21 and then is discharged;
and (3) adding acid into the tower bottom wastewater subjected to the deamination treatment of S5 to adjust the pH value to 4, then removing residual heavy metals by using an electric flocculation device 9, adjusting the pH value of effluent to 7, and then discharging.
In the treatment process of this example, the ammonia nitrogen concentration, the calcium ion concentration, the heavy metal concentration, and the PH value of the wastewater after each step of treatment were measured, and the measurement results are shown in table 2.
TABLE 2 effects of wastewater treatment
| Item | Water inlet and outlet conditions | Ammonia nitrogen (mg/L) | Ca2+(mg/L) | Total weight metal (mg/L) | pH |
| Primary sedimentation tank for raw water | Discharging water | 2000 | ＜100000 | 490 | 4 |
| First plate frame filter press | Discharging water | 1890 | ＜9900 | 480 | 4 |
| Coagulation reaction device | Discharging water | 1882 | ＜9000 | 47 | 4 |
| Calcium and magnesium removing device | Discharging water | 1880 | 18 | 40 | 10 |
| Middle water pool | Discharging water | 6880 | 18 | 40 | 11 |
| Negative pressure deamination system | Discharging water | 42 | 17 | 40 | 10 |
| PH (potential of hydrogen) callback pool | Discharging water | 42 | 17 | 40 | 4 |
| Electric flocculation device | Discharging water | 38 | 15 | 27 | 4 |
| Water outlet pool | Discharging water | 35 | 15 | 27 | 7 |
| Water outlet requirement | ≤50 | ＜20 | ≤35 | 7 |
As can be seen from Table 2, when the method provided by the invention is used for treating the desulfurization ammonia nitrogen wastewater, the ammonia nitrogen concentration is reduced from 6880mg/L after the wastewater is added into an ammonia station to 35mg/L of discharged water, the concentration is greatly reduced, the discharge requirement of the discharged water is met, heavy metal ions in the wastewater can be effectively removed, the total weight metal ion concentration is reduced from 490mg/L to 27mg/L, the heavy metal ion concentration requirement of the discharged water is met, the calcium ion concentration is reduced from 100000mg/L to 15mg/L, and the discharged water requirement is met, so that the method provided by the invention has a good treatment effect on the desulfurization ammonia nitrogen wastewater.
The foregoing is a more detailed description of the invention in connection with specific preferred embodiments and it is not intended that the invention be limited to these specific details. For those skilled in the art to which the invention pertains, several simple deductions or substitutions can be made without departing from the spirit of the invention, and all shall be considered as belonging to the protection scope of the invention.
Claims (10)
1. The utility model provides a desulfurization ammonia nitrogen effluent disposal system device which characterized in that: comprises a raw water primary sedimentation tank (1) for precipitating waste water, a coagulation reaction sedimentation device (3) for precipitating and recovering heavy metals, a calcium and magnesium removal device (4) for removing calcium and magnesium ions, a negative pressure deamination system for deamination, an electric flocculation device (9) for flocculating and removing residual heavy metals, and an ammonia washing purifier (21) for treating tail gas, wherein a water distributor (22) is arranged inside the ammonia washing purifier (21), a water sealing structure (26) is arranged below the water distributor (22) of the ammonia washing purifier (21), the water sealing structure (26) comprises a partition plate (23) for separating the ammonia washing purifier (21) into an upper part and a lower part, an air inlet pipe (24) penetrating below the partition plate (23) and an L-shaped pipe (25) communicated with the top of the air inlet pipe (24), the horizontal part of the L-shaped pipe (25) is positioned far away from the water distributor (22) and close to one end of the partition plate (, and a plurality of air nozzles are distributed on the horizontal part of the L-shaped pipe (25).
2. The desulfurization ammonia nitrogen wastewater treatment system device of claim 1, which is characterized in that: the pool top closing cap of raw water primary sedimentation pond (1), the supernatant output of raw water primary sedimentation pond (1) passes through pipe connection raw water catch basin (2), the precipitate output of raw water primary sedimentation pond (1) bottom passes through the pipeline and the pump machine is connected one number of plate frame pressure filter (12), the filtrating output of one number of plate frame pressure filter (12) passes through pipe connection raw water catch basin (2).
3. The desulfurization ammonia nitrogen wastewater treatment system device of claim 2, characterized in that: the output of former water catch basin (2) passes through the pipeline and goes out the water pump and connects coagulation reaction sediment device (3), coagulation reaction sediment device (3) are supporting to be provided with and coagulate elevator pump, No. two board frame pressure filter (13) and charge device, charge device is used for adding the heavy metal trapping agent, No. two board frame pressure filter's (13) filtrating output passes through pipe connection former water catch basin (2).
4. The desulfurization ammonia nitrogen wastewater treatment system device of claim 3, characterized in that: the waste water output of coagulation reaction precipitation device (3) connects through a line mixer and removes calcium magnesium device (4), a line mixer has the alkali lye storage tank through the pipe connection, it has analytic liquid storage tank to remove calcium magnesium device (4) through the pipe connection, the hydrous precipitate of removing calcium magnesium device (4) passes through pipe connection re-reaction unit (14), be the inside retort that is provided with the agitator at reaction unit, reaction unit (14) are through the acidic raw water of pipeline input again, the output of re-reaction unit (14) passes through mud delivery pump and pipe connection No. three plate frame pressure filters (15), the former water catch basin of pipe connection (2) is passed through to the filtrating output of No. three plate frame pressure filters (15).
5. The desulfurization ammonia nitrogen wastewater treatment system device of claim 4, characterized in that: remove the waste water output of calcium magnesium device (4) and pass through pipe connection decalcification sedimentation tank (5), decalcification sedimentation tank (5) adopt vertical flow sedimentation tank, the inner wall of decalcification sedimentation tank (5) adopts the anticorrosive material preparation to form, the mud output of decalcification sedimentation tank (5) passes through mud delivery pump and pipe connection device (14) of reacting again, pond (6) in the middle of the supernatant output of decalcification sedimentation tank (5) passes through pipe connection, the output in middle pond (6) passes through No. two pipeline mixers and connects negative pressure deamination system, No. two pipeline mixers are connected with the alkali supplementation system, the alkali supplementation system is including the alkali lye basin that is used for storing alkali lye, the PH appearance that is used for detecting PH, the alkali-adding device that is used for adding alkali lye.
6. The desulfurization ammonia nitrogen wastewater treatment system device of claim 5, characterized in that: the negative pressure deamination system comprises a negative pressure deamination tower (8), a preheater (7) and a condenser (17), wherein the bottom of the negative pressure deamination tower (8) is connected with the heat source input end of the preheater (7), the input end of the preheater (7) is connected with a pipeline mixer II through a pipeline, the output end of the preheater (7) is connected with the input end of the negative pressure deamination tower (8) through a lift pump, the negative pressure deamination tower (8) is connected with a saturated steam storage tank through a pipeline, the ammonia steam output end at the top of the negative pressure deamination tower (8) is connected with the condenser (17), dilute ammonia water condensed by the condenser (17) is connected with a gas-liquid separation tank (18) through a pipeline, the gas-liquid separation tank (18) reflows the dilute ammonia water to the negative pressure deamination tower (8) through a pipeline, the ammonia output end of the condenser, the ammonia recovery device (20) is a rectifying tower, the packing inside the ammonia recovery device (20) is replaced by a Z-shaped tower plate, and the non-condensable gas output end of the ammonia recovery device (20) is connected with an ammonia washing purifier (21) through a pipeline.
7. The desulfurization ammonia nitrogen wastewater treatment system device of claim 6, characterized in that: waste water at the bottom of negative pressure deamination tower (8) squeezes into electric flocculation device (9) after preheater (7) heat transfer, there is the acid solution storage tank electric flocculation device (9) through the pipe connection, the mud output of electric flocculation device (9) passes through pipe connection heavy metal filter press (16), the water outlet end of electric flocculation device (9) passes through pipe connection PH back regulation pond (10), PH back regulation pond (10) have the alkali lye storage tank through the pipe connection, the water outlet end of PH back regulation pond (10) passes through pipe connection water outlet pond (11).
8. A method for treating desulfurization ammonia nitrogen wastewater, which is characterized by using the desulfurization ammonia nitrogen wastewater treatment system device of any one of claims 1 to 7.
9. The method for treating desulfurization ammonia nitrogen wastewater according to claim 8, characterized in that: the method comprises the following steps:
s1, intensively discharging the raw water of the wastewater into a raw water primary sedimentation tank (1) through a pipeline, precipitating, pumping the precipitate into a first plate-frame filter press (12) by a pump to remove impurity slag in the raw water, and roasting the impurity slag;
s2, enabling supernatant subjected to precipitation treatment to flow into a raw water collecting tank (2), pumping the supernatant into a coagulation reaction precipitation device (3) by a pump, adding a heavy metal capture agent, precipitating and recovering heavy metals, and conveying sludge containing the heavy metals to a second plate-and-frame filter press (13) for filtering and then sintering;
s3, adding alkali into the wastewater with heavy metal recovered by a pump through a pipeline mixer to adjust the pH value to be more than 12, pumping the wastewater into a calcium and magnesium removing device (4), adding an analytic solution to remove calcium and magnesium ions, pumping the water-containing precipitate into a re-reaction device (14) by the pump, adjusting the pH value to be neutral with acidic raw water, and then sending the water-containing precipitate to a third plate-and-frame filter press (15) for slag-water separation treatment to recover calcium salt;
s4 the waste water after calcium removal by resolving enters a decalcification sedimentation tank (5) for clarification, the clear liquid flows into an intermediate water tank (6), alkali PH is supplemented to 11 through a pipeline mixer, the effluent water enters a negative pressure deamination tower (8) after being preheated by a preheater (7), free ammonia is continuously separated by a tower plate and concentrated to the tower top under the action of a V-shaped tower plate and steam, the ammonia gas at the tower top enters a condenser (17), condensate liquid flows back to the negative pressure deamination tower (8), the ammonia gas enters an ammonia recovery device (20) through an ammonia extraction mixer (19) for recovering ammonia water, and the tail gas is discharged after being purified by an ammonia washing purifier (21);
and (3) adding acid into the tower bottom wastewater subjected to the deamination treatment of S5 to adjust the pH value to 3-4, then removing residual heavy metals by an electric flocculation device (9), adjusting the pH value of effluent to 6-9, and discharging.
10. The method for treating desulfurization ammonia nitrogen wastewater according to claim 8, characterized in that: in the step S4, ammonia station wastewater is also pumped into the intermediate water tank (6), and the ammonia distillation temperature in the negative pressure deamination tower (8) is 55-65 ℃.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102503015A (en) * | 2011-11-25 | 2012-06-20 | 武汉兴能环保技术有限公司 | Method for treating wastewater generated by ammonia process desulfurization |
| CN102765842A (en) * | 2012-08-03 | 2012-11-07 | 济钢集团有限公司 | Pressure-reduction, alkali-addition and ammonia-distillation system |
| CN204395712U (en) * | 2015-01-14 | 2015-06-17 | 王磊 | A kind of industrial waste-gas purifier |
| CN104743728A (en) * | 2015-03-27 | 2015-07-01 | 王文领 | Energy-saving type deaminizing method for realizing negative pressure deamination by coking surplus ammonia water |
| CN206325367U (en) * | 2016-11-17 | 2017-07-14 | 天津市天佑环保设备有限公司 | A kind of VOC tail gas absorptions purifier |
| CN109607909A (en) * | 2018-11-27 | 2019-04-12 | 核工业北京化工冶金研究院 | A kind of high ammonia nitrogen uranium containing manganese wastewater treatment method |
-
2019
- 2019-12-20 CN CN201911323863.1A patent/CN111115934A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102503015A (en) * | 2011-11-25 | 2012-06-20 | 武汉兴能环保技术有限公司 | Method for treating wastewater generated by ammonia process desulfurization |
| CN102765842A (en) * | 2012-08-03 | 2012-11-07 | 济钢集团有限公司 | Pressure-reduction, alkali-addition and ammonia-distillation system |
| CN204395712U (en) * | 2015-01-14 | 2015-06-17 | 王磊 | A kind of industrial waste-gas purifier |
| CN104743728A (en) * | 2015-03-27 | 2015-07-01 | 王文领 | Energy-saving type deaminizing method for realizing negative pressure deamination by coking surplus ammonia water |
| CN206325367U (en) * | 2016-11-17 | 2017-07-14 | 天津市天佑环保设备有限公司 | A kind of VOC tail gas absorptions purifier |
| CN109607909A (en) * | 2018-11-27 | 2019-04-12 | 核工业北京化工冶金研究院 | A kind of high ammonia nitrogen uranium containing manganese wastewater treatment method |
Non-Patent Citations (2)
| Title |
|---|
| 刘军 等主编: "《汽车电控发动机技术 下》", 31 December 2012 * |
| 张奇 等: "活性焦烟气净化系统制酸废水处理工艺研究", 《矿业工程》 * |
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