CN103130361A - Ammonia-removing method and device for high-concentration ammonia-containing wastewater - Google Patents
Ammonia-removing method and device for high-concentration ammonia-containing wastewater Download PDFInfo
- Publication number
- CN103130361A CN103130361A CN2013100948368A CN201310094836A CN103130361A CN 103130361 A CN103130361 A CN 103130361A CN 2013100948368 A CN2013100948368 A CN 2013100948368A CN 201310094836 A CN201310094836 A CN 201310094836A CN 103130361 A CN103130361 A CN 103130361A
- Authority
- CN
- China
- Prior art keywords
- ammonia
- containing water
- stripping
- wastewater
- alkali
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Landscapes
- Physical Water Treatments (AREA)
Abstract
The invention relates to an ammonia-removing method and an ammonia-removing device for high-concentration ammonia-containing wastewater. The ammonia-removing method comprises the following steps: an alkali adding process of adding alkali liquor to the ammonia-containing raw material to improve the pH value of the ammonia-containing raw water; a temperature raising process of heating the high-concentration ammonia-containing wastewater with the alkali added therein to raise the temperature of the high-concentration ammonia-containing wastewater; a blowing process of dissolving the high-concentration ammonia-containing wastewater in the ammonia in the wastewater by an air blowing method; and an acid absorbing process of absorbing the ammonia-containing waste gas by acid to purify the waste gas. The ammonia-removing device for high-concentration ammonia-containing wastewater comprises an alkali adding mixer (2), a heater (5a), a blowing tower (9), an acid absorbing tower (12) and a connecting pipeline among the components. According to the ammonia-removing method and the ammonia-removing device for high-concentration ammonia-containing wastewater disclosed by the invention, the ultrasonic treatment technology and flash evaporation technology are combined, and air blowing is then carried out, so that the blowing efficiency is improved, the used amount of air is reduced and the power consumption is reduced. The waste gas is purified and the nitrogen is recycled by the acid absorbing method, so that the secondary pollution possibly caused to the atmosphere is avoided and the resource utilization of the nitrogen is realized. Compared with other ammonia-removing methods, the ammonia-removing method disclosed by the invention realizes the purposes of high efficiency and low cost.
Description
Technical field
The present invention relates to a kind of method and apparatus that adopts the air stripping method to remove contained ammonia nitrogen in strong ammonia wastewater, belong to energy-conservation and field of Environment Protection, particularly the deamination method of the strong ammonia wastewater of coking industry remained ammonia and device.
Background technology
Ammonia-containing water extensively is present in daily life and industry-by-industry, and particularly coking industry approximately gives off the ammonia-containing water of tens million of cubic metres every year, and its complicated component is more difficult.Efflux or reuse after common this ammonia-containing water is up to standard through biological treatment.If but these strong ammonia wastewaters directly adopt biological method to process, because ammonia nitrogen concentration content is high, can produce serious impact to biological treatment, affect treatment effect.Therefore, at first tackle strong ammonia wastewater and take suitable preconditioning technique, removal of ammonia and nitrogen.The ammonia still process method because technical maturity, deamination efficient are relatively high, is the most frequently used method of coking industry Ammonia-Containing Wastewater Treatment.But ammonia still process process steam consumption is large, causes processing cost higher.Air stripping method is because technique simply also often is used.The process of traditional stripping technology deamination is to improve the pH value of waste water, under alkaline condition, and the NH in waste water
3-N mainly is free NH
3Form, enter atmosphere by stripping.But this air stripping method only is used for processing the lower waste water of ammonia nitrogen concentration usually.For the higher waste water of ammonia nitrogen concentration, such as the ammonia-containing water of ammonia nitrogen concentration up to 4000mg/L, often realize because of very large being difficult to of stripping tower tower height of needs, and need a large amount of air, power consumption is large, and running cost is high, also can cause stripping tower to eject mouth large-minded, contain ammonia concentration low, be unfavorable for the ammonia nitrogen recycling.Therefore, research and develop a kind of high-level efficiency, deamination method and the device of less energy-consumption have great importance.
Summary of the invention
The object of the invention is to the conventional air blow-off method is improved, propose a kind of high ammonia-containing water stripping method that processing power is high, power consumption is little, and utilize the method that acid absorbs to purify the ammonia-contaminated gas that stripping tower is discharged.Compare with the ammonia still process method with traditional blow-off method, have energy-conservation, efficient, resource utilization, do not produce the characteristics such as secondary pollution.
Concrete technical scheme of the present invention is as follows:
A kind of ammonia-removal method of strong ammonia wastewater is characterized in that being comprised of following process at least;
(1) add alkali lye to containing in the former water of ammonia, that improves the pH value adds the alkali process;
(2) to through the described temperature-rise period that the heating of alkali strong ammonia wastewater improves temperature that adds that adds after alkali process (1);
(3) to removing through the strong ammonia wastewater after described temperature-rise period (2) raising temperature the stripping process that is dissolved in ammonia in described waste water by air stripping;
(4) the sour absorption process that the ammonia-contaminated gas that described stripping process (3) is produced absorbs to purify by acid.
The pH value scope that it is suitable that described process (1) adds the alkali process is 10-11.5; The suitable temperature range of process (2) temperature-rise period is 45-75 ℃.
Before or after process (2) temperature-rise period, ammonia-containing water is carried out ultrasonication.
Cross the Cheng Qian at process (3) stripping strong ammonia wastewater is carried out the flash distillation processing.
The deamination waste water that process (3) stripping process is discharged and high density contain the former water heat exchange of ammonia and heat containing the former water of ammonia.
The off-air that purifies through the sour absorption process of process (4) or turn back to again described stripping process circulation blow-removing, or directly diffuse in atmosphere.
Device of the present invention is comprised of the connecting pipeline that adds alkali mixing tank 2, well heater 5a, stripping tower 9, acid absorption column 12, add between ammonia-containing water connecting pipeline, stripping tower 9 and the acid absorption column 12 between ammonia-containing water connecting pipeline, well heater 5a and the stripping tower 9 between alkali mixing tank 2 and well heater 5a at least; The ammonia-containing water outlet side that adds alkali mixing tank 2 is connected with the ammonia-containing water inlet side of well heater 5a; The ammonia-containing water outlet side of well heater 5a is connected with stripping tower 9 ammonia-containing water inlet sides; Stripping tower 9 gas discharge outlets are connected with the ammonia off-air entrance that contains of acid absorption column 12, the clean air outlet of acid absorption column 12 or be connected with the gas inlet of stripping tower, or directly communicate with atmosphere.
Be provided with processor for ultrasonic wave 6 on the ammonia-containing water pipeline before or after ammonia-containing water well heater 5a; If double-bank heater 5a connects with 5b and heats that processor for ultrasonic wave 6 is arranged on the pipeline of the ammonia-containing water between one-level well heater 5a and secondary well heater 5b; The acoustic density of ul-trasonic irradiation face is 0.5-3W/cm
2, be 0.1-2 minute action time.
On the front ammonia-containing water pipeline of stripping tower 9, flasher 8 is set, the ammonia-containing water outlet side of flasher 8 is connected with the ammonia-containing water inlet side of stripping tower 9.
Interchanger 4 is set adding on the rear ammonia-containing water pipeline of alkali mixing tank 2, the low-temperature receiver inlet side of interchanger 4 with add alkali mixing tank ammonia-containing water outlet side and be connected, the thermal source inlet side is connected with the deamination wastewater outlet side of stripping tower bottom.
Be described as follows:
The present inventor carries out to the residual coking ammonia water that high density contains the former water of ammonia such as 3500mg/L the result confirmation that stripping is tested, and pH value and temperature are very large to the stripping effectiveness affects, and the pH value and the temperature that improve waste water can improve stripping efficient greatly, and can reduce the air consumption.So at first the present invention adds alkali lye in strong ammonia wastewater, improve the pH value of waste water; Then by heating, improve the temperature of waste water; Adopt again the air stripping method to remove the ammonia that is dissolved in strong ammonia wastewater.Owing to surpassing after 12 when the pH of strong ammonia wastewater value, the variation of stripping efficient tends towards stability, without obviously raising; After temperature reaches 75 ℃, along with rising, the rising stripping efficient of temperature also becomes slow; So, considering stripping efficient, reagent cost and energy consumption, the pH value scope of suitable selection is 10-11.5, temperature range is 45-75 ℃.What produce in the stripping process contains the higher waste gas of ammonia concentration ratio, can cause secondary pollution if directly enter atmosphere, and can cause the waste of nitrogen resource.Utilize sour absorption cleaning ammonia-contaminated gas, can obtain liquid at the bottom of the tower of ammonium salt-containing in absorption tower bottom, at the bottom of these towers, liquid can be recycled, and realizes resource utilization, can obtain ammonium sulfate as make absorption agent with sulfuric acid, can be used as the raw material of nitrogenous fertilizer.As the acid of absorption agent, can use sulfuric acid, nitric acid, hydrochloric acid or organic acid, also can use these sour mixtures, can consider its price, assimilation effect and product recovery value and decide according to particular case.
High density in strong ammonia wastewater of the present invention is for the ammonia nitrogen concentration of the deamination waste water after stripping.
Before or after described process (2) heat-processed, strong ammonia wastewater is carried out ultrasonication.Not only can promote to contain the degraded of some hardly degraded organic substances of the former water of ammonia through ultrasonication, improve the effect of subsequent biological treatment, can also strengthen NH in waste water
3The volatilization of-N and mass transfer make it easier from liquid phase to the gas phase transmission.
Cross the Cheng Qian at described process (3) stripping strong ammonia wastewater is carried out the flash distillation processing.Be elevated to 100-110 ℃ after strong ammonia wastewater is boosted, in the process that reduces pressure, the ammonia nitrogen generation flash distillation in waste water makes interior a large amount of reduction of ammonia nitrogen concentration short period of time of ammonia-containing water, thereby reduces the stripping load, is conducive to improve ammonia nitrogen removal efficient.
The deamination waste water that described process (3) stripping process is discharged and high density contain the former water heat exchange of ammonia and heat containing the former water of ammonia.Adopt after heating the method for stripping again, usually the deamination wastewater temperature of stripping tower bottom discharge is still higher, can at first itself and high density be contained the former water heat exchange of ammonia before heating, take full advantage of its waste heat and improve the temperature that contains the former water of ammonia, enter again well heater, namely the energy consumption of heating can be reduced, the subsequent biological treatment operation can be avoided again affecting because the deamination wastewater temperature is higher.The device of heat exchange adopts existing heat exchanger to get final product.
The off-air that purifies through the sour absorption process of process (4) or turn back to again described stripping process circulation blow-removing, or directly diffuse in atmosphere.Gas after sour absorption cleaning is in the water saturation state, and temperature is also higher, uses if return to the stripping tower circulation blow-removing, the descend decline of the stripping effect that causes of the temperature that can reduce the waste water that in the stripping process, the moisture evaporation brings.Certainly, recycle and can make operating system become complicated, therefore, also can select ammonia-contaminated gas by directly entering the method for atmosphere after purifying, this respect can be selected as the case may be.
Realize the device of described strong ammonia wastewater deamination method, as shown in Figure 1, formed by the connecting pipeline that adds alkali mixing tank 2, well heater 5a, stripping tower 9, acid absorption column 12, add between ammonia-containing water connecting pipeline, stripping tower 9 and the acid absorption column 12 between ammonia-containing water connecting pipeline, well heater 5a and the stripping tower 9 between alkali mixing tank 2 and well heater 5a at least; The ammonia-containing water outlet side that adds alkali mixing tank 2 is connected with the ammonia-containing water inlet side of well heater 5a; The ammonia-containing water outlet side of well heater 5a is connected with stripping tower 9 ammonia-containing water inlet sides; Stripping tower 9 gas discharge outlets are connected with the ammonia off-air entrance that contains of acid absorption column 12, the clean air outlet of acid absorption column 12 or be connected with the gas inlet of stripping tower, or directly communicate with atmosphere.
Realizing the device of described ultrasonication, is on the ammonia-containing water pipeline, processor for ultrasonic wave 6 to be set before or after ammonia-containing water well heater 5a; If double-bank heater 5a connects with 5b and heats that processor for ultrasonic wave 6 is arranged on the pipeline of the ammonia-containing water between one-level well heater 5a and secondary well heater 5b; The acoustic density of ul-trasonic irradiation face is 0.5-3W/cm
2, be 0.1-2 minute action time.By the effect of hyperacoustic short period of time of such low energy densities, can realize promoting the purpose of degraded and the ammonia volatilization of difficult degradation thing with very little ultrasonic equipment.And it is little to bear the required material stress of the hyperacoustic oscillating action of low energy densities, and the life-span is long, not only can reduce the cost of equipment, can also reduce the equipment replacement frequency of maintenance.
Realizing the device that described flash distillation is processed, is on the front ammonia-containing water pipeline of stripping tower 9, flasher 8 to be set, and the ammonia-containing water outlet side of flasher 8 is connected with the ammonia-containing water inlet side of stripping tower 9.By set up flasher before stripping tower, can reduce the stripping load, further improve the processing power to the higher ammonia-containing water of ammonia nitrogen concentration.The ammonia nitrogen concentration that can contain according to pending high density the former water of ammonia whether set up by flasher and the ammonia nitrogen removal effect that expectation reaches decided.
Realize that described deamination waste water and high density contain the device of the former water heat exchange of ammonia, it is characterized in that interchanger 4 being set adding on the rear ammonia-containing water pipeline of alkali mixing tank 2, the low-temperature receiver inlet side of interchanger 4 with add alkali mixing tank ammonia-containing water outlet side and be connected, the thermal source inlet side is connected with the deamination wastewater outlet side of stripping tower bottom.Can realize like this heat of deamination waste water is passed to strong ammonia wastewater, can reduce the energy consumption of follow-up heat-processed, also can avoid the too high subsequent biological treatment that affects of deamination wastewater temperature.
In Practical Project, regulate the alkali lye of former water pH value, generally adopt 30%NaOH solution, but also can select alkali concn and medicament according to practical situation.The ammonia of discharging in the ammonia that volatilizes due to ultrasonic wave and flasher is large-minded, concentration is high, it can be sent in the coal gas treatment system, enters coal gas deamination operation; The acid that also can send into the stripping tower ammonia-contaminated gas absorbs operation and reclaims ammonia.The ammonia of discharging from the air stripping tower also can water absorbs waste gas and removes wherein ammonia, but the gained ammonia concn low being difficult to utilized, and assimilated efficiency is lower, so high with the acid solution assimilated efficiency, and recyclable product, avoid the utilization of ammoniacal liquor or the difficulty of processing aspect.
The treatment process of strong ammonia wastewater of the present invention is applicable to equally also that other industry produces, and to contain in ammonia liquid ammonia volatile, the main body of liquid composition is the deamination of volatile ammonia-containing water not, also is applicable to substitute other and removes existing traditional stripping method of volatile components from liquid.
The removal method and apparatus of strong ammonia wastewater of the present invention, added alkali and intensification to containing the former water of ammonia before stripping, and in conjunction with ultrasonication technology, flash evaporation technology, carry out again air stripping, greatly improved the efficient of stripping, and can reduce the air consumption, and reduce power consumption, save running cost; The method that absorbs by acid purifies stripping waste gas and reclaims nitrogen, has not only avoided the secondary pollution that may cause atmosphere but also has realized the recycling of nitrogen.Compare with other deamination method, present method has realized cost-effective purpose.
Description of drawings
Fig. 1 is the process flow diagram of example 1 of the present invention;
Fig. 2 is the process flow diagram of example 2 of the present invention;
Fig. 3 is the process flow diagram of example 3 of the present invention;
Fig. 4 is the process flow diagram of example 4 of the present invention;
Fig. 5 is the process flow diagram of example 5 of the present invention;
Fig. 6 is the process flow diagram of example 6 of the present invention;
Shown in figure: 1-high density contains the former water of ammonia, 2-add alkali mixing tank, 3-NaOH alkaline solution, 4-interchanger, 5a-one-level well heater, 5b-secondary well heater, 6-processor for ultrasonic wave, 7a-ultrasonic wave desorb ammonia, 7b-flasher steams ammonia, 7c-stripping tower top ammonia-contaminated gas, 8-flasher, 9-stripping tower, 10-air, deamination waste water at the bottom of 11-stripping tower, 12-acid absorption column, 13-dilute sulphuric acid, 14-except ammonia Purge gas, 15-ammoniumsulphate soln, deamination waste water after 16-heat exchange.
Embodiment
The invention will be further described below in conjunction with embodiment:
Fig. 1 has represented the described treating processes of the embodiment of the present invention 1.Treating processes mainly forms by adding alkali, heating, air stripping and acid absorption operation.Add alkali mixing tank 2, one-level well heater 5a, stripping tower 9, acid absorption column 12 and be connected successively, air stripping tower top waste gas outlet is connected with the gas inlet of acid absorption column bottom, and the wastewater outlet of stripping tower 9 bottoms is towards the subsequent biological treatment operation.
Coke-oven plant's remained ammonia contains the former water 1 of ammonia as high density, mixes with certain proportion adding alkali mixing tank 2 with 38% NaOH alkaline solution 3, after pH reaches 11.2, sends in one-level well heater 5a, is heated to 72 ℃.Ammonia-containing water after heating is sent to the top of stripping tower 9, contacts with the air 10 that enters from the bottom in stripping tower, and the ammonia in liquid is transferred to gas phase.The deamination waste water 11 of discharging at the bottom of stripping tower enters the subsequent biological treatment link and further processes.Stripping tower top ammonia-contaminated gas 7c is sent to the bottom of acid absorption column 12, carries out counter current contact with the dilute sulphuric acid 13 that enters from top, and the ammonia in ammonia-contaminated gas is become ammonium sulfate by the absorption of sulfuric acid liquid and transfers to liquid phase.Ammoniumsulphate soln 15 is discharged from acid absorption column 12 bottoms, and sends into the chemical fertilizers production operation, discharges and turn back to stripping tower 9 from the tower top of acid absorption column 12 except ammonia Purge gas 14 to recycle.
The ammonia concentration that contains that high density contains the former water 1 of ammonia is 3000mg/L, and the ammonia concentration that contains of the deamination waste water 11 of stripping tower 9 bottoms discharges is 220mg/L.Adopt air stripping deamination method of the present invention, under reasonably stripping tower height and less air capacity condition, can realize the efficient denitrification for this dense ammonia-containing water of remained ammonia.This shows, strong ammonia wastewater deamination method processing power of the present invention is large, and efficient is high, and power consumption is few.
Fig. 2 has represented the described treating processes of the embodiment of the present invention 2.Treating processes mainly forms by adding alkali, heat exchange, heating, ultrasonication, flash distillation processing, air stripping and acid absorption operation.Adding alkali mixing tank 2, interchanger 4, one-level well heater 5a, processor for ultrasonic wave 6, flasher 8, stripping tower 9, acid absorption column 12 is connected successively, air stripping tower top waste gas outlet is connected with the gas inlet of acid absorption column bottom, and the wastewater outlet of stripping tower 9 bottoms is connected with the thermal source entrance of interchanger 4.
Coke-oven plant's remained ammonia contains the former water 1 of ammonia as high density, mix with certain proportion adding alkali mixing tank 2 with 30% NaOH alkaline solution 3, after pH reaches 10.5, after being sent to deamination waste water 11 heat exchange of interchanger 4 and stripping tower 9 bottoms discharging, send in one-level well heater 5a, be heated to 65 ℃.Ammonia-containing water after heating enters processor for ultrasonic wave 6 after ultrasonication, enters flasher 8, and ultrasonic wave desorb ammonia 7a and flasher steam and be sent to coal gas treatment system deamination operation after ammonia 7b mixes.The ammonia-containing water that flasher is discharged is sent to the top of stripping tower 9, contacts with the air 10 that enters from the bottom in stripping tower, and the ammonia in liquid is transferred to gas phase.The deamination waste water 11 of discharging at the bottom of stripping tower by interchanger with contain the former water heat exchange of ammonia, after heat exchange, deamination waste water 16 enters the subsequent biological treatment link and further processes.Stripping tower top ammonia-contaminated gas 7c is sent to the bottom of acid absorption column 12, carries out counter current contact with the dilute sulphuric acid 13 that enters from top, and the ammonia in ammonia-contaminated gas is become ammonium sulfate by the absorption of sulfuric acid liquid and transfers to liquid phase.Ammoniumsulphate soln 15 is discharged from acid absorption column 12 bottoms, and sends into the chemical fertilizers production operation, discharges and turn back to stripping tower 9 from the tower top of acid absorption column 12 except ammonia Purge gas 14 to recycle.
The acoustic density of the acoustic wave action face of processor for ultrasonic wave 6 is 1.0W/cm
2, be 1 minute action time.The ammonia concentration that contains that high density contains the former water 1 of ammonia is 4000mg/L, and the ammonia concentration that contains of the deamination waste water 11 of stripping tower 9 bottoms discharges is 185mg/L.The present embodiment high density contains the former water ammonia nitrogen concentration of ammonia and wants high by 33% than embodiment 1, has therefore set up processor for ultrasonic wave and flasher on the basis of embodiment 1.Can be found out by its treatment effect, set up the processing power that processor for ultrasonic wave and flasher have further improved whole technique, be suitable for the more processing of the ammonia-containing water of high-concentration ammonia-nitrogen.
Strong ammonia wastewater deamination apparatus and flow process are substantially the same manner as Example 2, as shown in Figure 3, and before difference is that the position of processor for ultrasonic wave is positioned at the one-level well heater.Be ammonia-containing water through add alkali regulate pH value and with deamination waste water 11 heat exchange of stripping tower discharge after, enter processor for ultrasonic wave 6, the ammonia-containing water after ultrasonication is again through one-level well heater 5a heat temperature raising.In addition, after high density contained the former water of ammonia and 35%NaOH alkaline solution 3 mixes, the pH value reached 11.0, and heater via 5a is heated to 55 ℃.
The acoustic density of the acoustic wave action face of processor for ultrasonic wave 6 is 1.5W/cm
2, be 0.5 minute action time.The ammonia concentration that contains that high density contains the former water 1 of ammonia is 3600mg/L, and the ammonia concentration that contains of the deamination waste water 11 of stripping tower 9 bottoms discharges is 190mg/L.
Strong ammonia wastewater deamination apparatus and flow process are substantially the same manner as Example 2, and as shown in Figure 4, difference has been to reduce the flash distillation treatment process between ultrasonication and stripping operation.Be that ammonia-containing water is directly sent into stripping tower 9 after ultrasonication top is carried out stripping and processed.In addition, ultrasonic wave desorb ammonia 7a communicates with stripping tower top ammonia-contaminated gas 7c, sends into together acid absorption column 12 through sour absorption cleaning.After high density contained the former water of ammonia and 40%NaOH alkaline solution 3 mixes, the pH value reached 11.5, and heater via 5a is heated to 70 ℃.
The acoustic density of the acoustic wave action face of processor for ultrasonic wave 6 is 3.0W/cm
2, be 1.5 minutes action time.The ammonia concentration that contains that high density contains the former water 1 of ammonia is 3200mg/L, and the ammonia concentration that contains of the deamination waste water 11 of stripping tower 9 bottoms discharges is 210mg/L.
Embodiment 5
Strong ammonia wastewater deamination apparatus and flow process are substantially the same manner as Example 4, as shown in Figure 5, difference is to adopt the double-bank heater series connection that ammonia-containing water is heated, and the position of processor for ultrasonic wave 6 is between one-level well heater 5a and secondary well heater 5b.That discharges from acid absorption column 12 tops in addition, 14 directly diffuses in atmosphere except ammonia purifies air.After high density contained the former water of ammonia and 25%NaOH alkaline solution 3 mixes, the pH value reached 10.3, and after one-level well heater 5a and secondary well heater 5b heating, temperature reaches 75 ℃.
The acoustic density of the acoustic wave action face of processor for ultrasonic wave 6 is 2.8W/cm
2, be 2 minutes action time.The ammonia concentration that contains that high density contains the former water 1 of ammonia is 3300mg/L, and the ammonia concentration that contains of the deamination waste water 11 of stripping tower 9 bottoms discharges is 195mg/L.
Strong ammonia wastewater deamination apparatus and flow process are substantially the same manner as Example 2, and as shown in Figure 6, difference has been to reduce the ultrasonication operation after well heater, and the ammonia-containing water after namely heating directly enters flasher 8 and carries out the flash distillation processing.In addition, after high density contained the former water of ammonia and 28%NaOH alkaline solution 3 mixes, the pH value reached 10.8, and heater via 5a is heated to 50 ℃.
The ammonia concentration that contains that high density contains the former water 1 of ammonia is 3500mg/L, and the ammonia concentration that contains of the deamination waste water 11 of stripping tower 9 bottoms discharges is 175mg/L.
Claims (10)
1. the ammonia-removal method of a strong ammonia wastewater, is characterized in that being comprised of following process at least;
1) add alkali lye to containing in the former water of ammonia, that improves the pH value adds the alkali process;
2) to through the described alkali process 1 that adds) after add the temperature-rise period that the heating of alkali strong ammonia wastewater improves temperature;
3) to through described temperature-rise period 2) strong ammonia wastewater that improves after temperature removes the stripping process that is dissolved in ammonia in described waste water by air stripping;
4) to described stripping process 3) ammonia-contaminated gas that the produces sour absorption process that absorbs to purify by acid.
2. the ammonia-removal method of strong ammonia wastewater as claimed in claim 1, is characterized in that process 1) suitable pH value scope is 10-11.5 to add the alkali process; Process 2) the suitable temperature range of temperature-rise period is 45-75 ℃.
3. the ammonia-removal method of strong ammonia wastewater as claimed in claim 1, is characterized in that in process 2) ammonia-containing water is carried out ultrasonication before or after temperature-rise period.
4. the ammonia-removal method of strong ammonia wastewater as claimed in claim 1, is characterized in that in process 3) stripping crosses the Cheng Qian and strong ammonia wastewater is carried out flash distillation processes.
5. the ammonia-removal method of strong ammonia wastewater as claimed in claim 1, is characterized in that process 3) the stripping process deamination waste water of discharging and high density contain the former water heat exchange of ammonia and heat containing the former water of ammonia.
6. the ammonia-removal method of strong ammonia wastewater as claimed in claim 1, is characterized in that through process 4) off-air that purifies of sour absorption process or turn back to again described stripping process circulation blow-removing, or directly diffuse in atmosphere.
7. realize the device of the described method of claim 1, it is characterized in that at least being formed by the connecting pipeline that adds alkali mixing tank (2), well heater (5a), stripping tower (9), acid absorption column (12), add between ammonia-containing water connecting pipeline, stripping tower (9) and the acid absorption column (12) between ammonia-containing water connecting pipeline, well heater (5a) and the stripping tower (9) between alkali mixing tank (2) and well heater (5a); The ammonia-containing water outlet side that adds alkali mixing tank (2) is connected with the ammonia-containing water inlet side of well heater (5a); The ammonia-containing water outlet side of well heater (5a) is connected with stripping tower (9) ammonia-containing water inlet side; Stripping tower (9) gas discharge outlet is connected with the ammonia off-air entrance that contains of acid absorption column (12), the clean air outlet of acid absorption column (12) or be connected with the gas inlet of stripping tower, or directly communicate with atmosphere.
8. device as claimed in claim 6, is characterized in that being provided with processor for ultrasonic wave (6) on the ammonia-containing water pipeline before or after ammonia-containing water well heater (5a); If double-bank heater (5a) is connected with (5b) and is heated that processor for ultrasonic wave (6) is arranged on the pipeline of the ammonia-containing water between one-level well heater (5a) and secondary well heater (5b); The acoustic density of ul-trasonic irradiation face is 0.5-3W/cm
2, be 0.1-2 minute action time.
9. device as claimed in claim 6, is characterized in that on the front ammonia-containing water pipeline of stripping tower (9), flasher (8) being set, and the ammonia-containing water outlet side of flasher (8) is connected with the ammonia-containing water inlet side of stripping tower (9).
10. device as claimed in claim 6, it is characterized in that on the ammonia-containing water pipeline, interchanger (4) being set adding after alkali mixing tank (2), the low-temperature receiver inlet side of interchanger (4) with add alkali mixing tank ammonia-containing water outlet side and be connected, the thermal source inlet side is connected with the deamination wastewater outlet side of stripping tower bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013100948368A CN103130361A (en) | 2013-03-22 | 2013-03-22 | Ammonia-removing method and device for high-concentration ammonia-containing wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013100948368A CN103130361A (en) | 2013-03-22 | 2013-03-22 | Ammonia-removing method and device for high-concentration ammonia-containing wastewater |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103130361A true CN103130361A (en) | 2013-06-05 |
Family
ID=48490879
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013100948368A Pending CN103130361A (en) | 2013-03-22 | 2013-03-22 | Ammonia-removing method and device for high-concentration ammonia-containing wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103130361A (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103449591A (en) * | 2013-08-19 | 2013-12-18 | 中山大学 | High-concentration ammonia nitrogen wastewater treatment device |
| CN106587272A (en) * | 2016-12-22 | 2017-04-26 | 高频美特利环境科技（北京）有限公司 | Ammonia-containing wastewater treatment method |
| CN106630265A (en) * | 2016-11-30 | 2017-05-10 | 江西蓝星星火有机硅有限公司 | Processing method for recycling ammonia from ammonia-containing wastewater |
| CN107585961A (en) * | 2017-10-17 | 2018-01-16 | 南京圆点环境清洁技术有限公司 | One kind is used for coal chemical industry enterprises high-concentration ammonia nitrogenous wastewater recycling treatment system |
| CN107697969A (en) * | 2017-05-09 | 2018-02-16 | 北京合力清源科技有限公司 | A kind of system and method for reducing biogas slurry ammonia nitrogen concentration |
| CN110550799A (en) * | 2019-08-21 | 2019-12-10 | 天津大学 | method and device for treating ammonia-containing wastewater |
| CN111748012A (en) * | 2020-06-22 | 2020-10-09 | 广东闻扬环境科技有限公司 | Device and method for recovering ammonium from ammonian-containing stock solution and concentrating protein stock solution |
| CN111924998A (en) * | 2019-05-13 | 2020-11-13 | 自然资源部天津海水淡化与综合利用研究所 | Closed-cycle efficient recycling ammonia nitrogen removal equipment and method |
| CN112047522A (en) * | 2020-08-22 | 2020-12-08 | 深圳中科环保产业发展有限公司 | Treatment process and treatment system for comprehensive wastewater |
| CN113698017A (en) * | 2021-07-16 | 2021-11-26 | 南京工业大学 | Resource utilization and treatment method of alkynol wastewater |
| CN114751534A (en) * | 2022-06-15 | 2022-07-15 | 江苏新聚环保科技有限公司 | Ammonia gas treatment method by aeration stripping and catalytic combustion |
| CN116462342A (en) * | 2023-03-17 | 2023-07-21 | 武平飞天电子科技有限公司 | High-concentration ammonia nitrogen-containing wastewater separation tower and treatment method |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102923896A (en) * | 2012-11-07 | 2013-02-13 | 天津大学 | Deaminizing method and device for high-concentration ammonia-containing waste water |
-
2013
- 2013-03-22 CN CN2013100948368A patent/CN103130361A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102923896A (en) * | 2012-11-07 | 2013-02-13 | 天津大学 | Deaminizing method and device for high-concentration ammonia-containing waste water |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103449591B (en) * | 2013-08-19 | 2015-06-10 | 中山大学 | High-concentration ammonia nitrogen wastewater treatment device |
| CN103449591A (en) * | 2013-08-19 | 2013-12-18 | 中山大学 | High-concentration ammonia nitrogen wastewater treatment device |
| CN106630265A (en) * | 2016-11-30 | 2017-05-10 | 江西蓝星星火有机硅有限公司 | Processing method for recycling ammonia from ammonia-containing wastewater |
| CN106587272A (en) * | 2016-12-22 | 2017-04-26 | 高频美特利环境科技（北京）有限公司 | Ammonia-containing wastewater treatment method |
| CN107697969A (en) * | 2017-05-09 | 2018-02-16 | 北京合力清源科技有限公司 | A kind of system and method for reducing biogas slurry ammonia nitrogen concentration |
| CN107585961A (en) * | 2017-10-17 | 2018-01-16 | 南京圆点环境清洁技术有限公司 | One kind is used for coal chemical industry enterprises high-concentration ammonia nitrogenous wastewater recycling treatment system |
| CN111924998A (en) * | 2019-05-13 | 2020-11-13 | 自然资源部天津海水淡化与综合利用研究所 | Closed-cycle efficient recycling ammonia nitrogen removal equipment and method |
| CN110550799A (en) * | 2019-08-21 | 2019-12-10 | 天津大学 | method and device for treating ammonia-containing wastewater |
| CN111748012A (en) * | 2020-06-22 | 2020-10-09 | 广东闻扬环境科技有限公司 | Device and method for recovering ammonium from ammonian-containing stock solution and concentrating protein stock solution |
| CN112047522A (en) * | 2020-08-22 | 2020-12-08 | 深圳中科环保产业发展有限公司 | Treatment process and treatment system for comprehensive wastewater |
| CN113698017A (en) * | 2021-07-16 | 2021-11-26 | 南京工业大学 | Resource utilization and treatment method of alkynol wastewater |
| CN113698017B (en) * | 2021-07-16 | 2022-07-29 | 南京工业大学 | Resource utilization and treatment method of alkynol wastewater |
| CN114751534A (en) * | 2022-06-15 | 2022-07-15 | 江苏新聚环保科技有限公司 | Ammonia gas treatment method by aeration stripping and catalytic combustion |
| CN116462342A (en) * | 2023-03-17 | 2023-07-21 | 武平飞天电子科技有限公司 | High-concentration ammonia nitrogen-containing wastewater separation tower and treatment method |
| CN116462342B (en) * | 2023-03-17 | 2023-12-29 | 武平飞天电子科技有限公司 | High-concentration ammonia nitrogen-containing wastewater separation tower and treatment method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103130361A (en) | Ammonia-removing method and device for high-concentration ammonia-containing wastewater | |
| CN102190341B (en) | Stripping ammonia-removing method based on flash evaporation and heat pump technologies | |
| CN102061197B (en) | Coke oven gas desulfuration and deamination combined purifying method and special device thereof | |
| CN108821308B (en) | Method and device for preparing high-concentration ammonia water by using coking residual ammonia water | |
| WO2004016717A1 (en) | Wet gas purification method and system for practicing the same | |
| CN201658945U (en) | Sintering smoke purifying system based on heat pipe afterheat recovery technology | |
| CN103408467B (en) | Low-energy-consumption urea production technology and system adopting CO2 stripping method | |
| CN103102033A (en) | Sulfur and ammonia-containing wastewater treatment method | |
| CN102030431A (en) | Process method for recovering nitrogen and phosphorus composite nutrients from biogas slurry and purifying primary methane | |
| CN104860465B (en) | Double-tower catalysis thermal-coupling reflux deamination method and deamination device thereof | |
| CN102923896A (en) | Deaminizing method and device for high-concentration ammonia-containing waste water | |
| CN101993173A (en) | Improved alkaline process flow with coking sewage treatment (A/O) method | |
| CN102583866A (en) | Comprehensive treatment method for ammonia nitrogen wastewater generated in production of thioxophosphamide | |
| CN111747382B (en) | Method and system for concentrating and recycling dilute acid by using alkylation waste acid recycling device | |
| CN101734813B (en) | Technology for recovering ammonium sulfate by waste acid pickle generated in process of producing cyanuric acid and equipment therefor | |
| CN204384885U (en) | Waste Sulfuric Acid waste water produces the treatment system of ammonium sulfate | |
| CN217526958U (en) | Ammonia tail gas absorption device | |
| CN103435214B (en) | Comprehensive treatment method for formaldehyde-containing acid wastewater | |
| CN102530868B (en) | Ammonia oxidation synthetic gas is except the environment-protective process method of ammonia | |
| CN104276685A (en) | Process for recovering ammonia from wastewater containing ammonia nitrogen | |
| KR102221791B1 (en) | Energy-saving recycling system and recycling method for by-products produced during sewage treatment | |
| CN113087267A (en) | High ammonia nitrogen waste liquid purification process | |
| CN103183430A (en) | Device for treating ammonia nitrogen wastewater by utilizing direct contact type degassing membrane technology | |
| CN113213433A (en) | Method for directly preparing sulfuric acid for storage battery by using secondary lead smelting flue gas | |
| CN203437120U (en) | Deamination and dehydration device for sodium persulfate (persulfate) synthetic fluid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20130605 |