CN104117280A - Ammonia stripping tail gas treatment method, ammonia-nitrogen wastewater treatment method and equipment - Google Patents
Ammonia stripping tail gas treatment method, ammonia-nitrogen wastewater treatment method and equipment Download PDFInfo
- Publication number
- CN104117280A CN104117280A CN201410355370.7A CN201410355370A CN104117280A CN 104117280 A CN104117280 A CN 104117280A CN 201410355370 A CN201410355370 A CN 201410355370A CN 104117280 A CN104117280 A CN 104117280A
- Authority
- CN
- China
- Prior art keywords
- stripping
- ammonia
- absorption
- tower
- tail gas
- 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
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
The invention provides an ammonia stripping tail gas treatment method, an ammonia-nitrogen wastewater treatment method and equipment. The ammonia stripping tail gas treatment method comprises the following steps: (1) absorption: introducing stripping tail gas into an absorption liquid so as to obtain absorption tail gas and an ammonia-containing liquid; and (2) crystallization: guiding the ammonia-containing liquid into a crystallization mother liquor to be crystallized so as to obtain ammonium sulfate crystal, wherein the absorption liquid is a mixed liquid formed by mixing concentrated sulfuric acid and a crystallization mother liquid according to the mass volume ratio of (8-20)kg to 1 m<3>, and the seed crystal solid content in the crystallization mother liquid is 20-60%. The method can be used for preventing the problem that ammonium sulfate solution is directly crystallized in an absorption tower without additionally added seed crystals, so that the bottom of a crystallization tower and an outlet pipeline at the bottom of the crystallization tower are blocked by crystallized products.
Description
Technical field
The present invention relates to ammonia nitrogen waste water process field, especially, relate to a kind of ammonia stripping exhaust gas treating method and nitrogen-containing wastewater processing method and equipment.
Background technology
The industries such as smelting, chemical industry, plating, cultivation all can produce ammonia nitrogen waste water, ammonia nitrogen waste water wide material sources, and discharge capacity is large.In this waste water, ammonia nitrogen thing exceeds standard and can cause algae and other microorganism amount reproduction, causes body eutrophication, accelerates the consumption of Dissolved Oxygen in Water, causes the death of different kind organism in water body.Harm is serious.In waste water, ammonia-nitrogen content has been classified as " 12 " and has been reduced discharging one of the binding indicator by China.How efficient, economic processing high-concentration ammonia nitrogenous wastewater, has become current environment worker's research emphasis.
At present, the processing method of ammonia nitrogen waste water mainly comprises bioanalysis, absorption method, magnesium ammonium phosphate sediment method etc.Blow-off method have ammonia nitrogen removal frank high, operation control simple advantage, in the waste gas producing in stripping process, ammonia content is higher, easily to environment produce secondary pollution, the scope of application of blow-off method is restricted.It is harmless nitrogen that bioanalysis mainly utilizes the nitrification and denitrification effect of microorganism to make mineralized nitrogen, and owing to being subject to the restriction of C/N ratio and microorganism living environment, bioanalysis is unsuitable for processing the waste water that ammonia nitrogen concentration is high and biodegradability is poor.The advantages such as that absorption method has is simple to operate, adsorbent can recycle, but because the adsorption capacity of adsorbent is less and be subject in waste water the impact of competing ions larger, therefore absorption method is only suitable for processing the ammonia nitrogen waste water of low concentration.Magnesium ammonium phosphate sediment method is in waste water, to add precipitating reagent (as MgCl
2with Na
2hPO
4), with NH
4 +reaction generates MgNH
4pO
46H
2o precipitation, realizes separating of ammonia nitrogen and water.Because medicament expense is higher, the research that ammonium sulfate magnesium precipitate method is processed ammonia nitrogen waste water mainly rests on laboratory stage.
Although the treatment technology of ammonia nitrogen waste water, in constantly progressive and development, still lacks a kind of efficient, economic high-concentration ammonia nitrogenous wastewater at present and processes the technique reclaiming with ammonia resource.Although traditional stripping process can be for the pretreatment of high-concentration ammonia nitrogenous wastewater, the ammonia in stripping tail gas can not reclaim, and causes secondary pollution and the wasting of resources.Patent (102060406B, 102030386A) utilizes stripping or stripping process to process high-concentration ammonia nitrogenous wastewater, and from ammonium sulfate, reclaims and obtained ammonia sulfate crystal or concentrated ammonia liquor by the mode of high temperature or heating evaporation.Although these techniques have realized the resource of ammonia and have reclaimed, but still have the problem that evaporative crystallization energy consumption is high, ammonium sulfate cost recovery is high.
Summary of the invention
The object of the invention is to provide a kind of ammonia stripping exhaust gas treating method and nitrogen-containing wastewater processing method and equipment, processes the technical problem of the recovery of ammonia in the waste gas producing after nitrogen-containing wastewater to solve available technology adopting blow-off method.
For achieving the above object, according to an aspect of the present invention, provide a kind of ammonia stripping exhaust gas treating method, comprised the following steps: 1) absorbed: stripping tail gas is passed in absorption liquid, and tail gas and containing ammonium liquid has been absorbed; 2) crystallization: will pass in crystalline mother solution and carry out crystallization containing ammonium liquid, and obtain ammonia sulfate crystal; Absorption liquid is that the concentrated sulfuric acid and crystalline mother solution are 8～20kg: 1m by mass volume ratio
3the mixed liquor being mixed to form; In crystalline mother solution, crystal seed solid content is 20～60%.
Further, in crystalline mother solution, the solid content of crystal seed is 20～40%.
Further, the acidity of crystalline mother solution is 2～10mmol/L.
Further, the concentration > 80% of the concentrated sulfuric acid.
Further, crystallisation step carries out under the condition stirring, and mixing speed is 30～60rpm.
Further, ammonia sulfate crystal obtains ammonium sulfate product after dehydrating.
Further, comprise the following steps: 1) stripping: regulate after the pH value of ammonia nitrogen waste water, after stripping air-blowing is de-, produce ammonia stripping tail gas and deamination waste water; 2) ammonia stripping tail gas is processed by above-mentioned method, produced and absorb tail gas; Absorbing tail gas enters in stripping step as stripping gas.
Further, the pH value of ammonia nitrogen waste water is adjusted to 10.0～13.0.
Also provide according to a further aspect in the invention a kind of for as the ammonia nitrogen sewage treatment equipment of the method for claim 8 or 9, ammonia nitrogen sewage treatment equipment comprises: waste water regulating tank, stripping tower, absorption tower, induced crystallization groove; The liquid outlet of waste water regulating tank is connected with the inlet of stripping tower, and the liquid outlet of stripping tower is connected with the inlet of waste water regulating tank; The gas outlet of stripping tower is connected with the air inlet on absorption tower, and the liquid outlet on absorption tower is connected with induced crystallization groove, and the gas outlet on absorption tower is connected with the air inlet of stripping tower; The mother liquor outlet of induced crystallization groove is connected with the absorption liquid import on absorption tower.
The present invention has following beneficial effect:
Method provided by the invention is taking more than 80% concentrated sulfuric acid and induced crystallization groove mother liquor as ammonia absorption liquid, and controlling ammonia absorption liquid is that the concentrated sulfuric acid and crystalline mother solution are 8～20kg: 1m by mass volume ratio
3the mixed liquor being mixed to form, increases the degree of supersaturation of the ammonium sulfate after absorbing, and controls ammonium sulfate degree of supersaturation in critical crystallization Jie Wen district.Improve the absorptivity of the waste gas that blow-off method is produced.Avoid ammonium sulfate direct crystallization in the absorption tower without plus seed, at the bottom of causing crystallizing tower and the problem stopped up by crystallized product of crystallizing tower bottom outlet pipeline simultaneously.
Except object described above, feature and advantage, the present invention also has other object, feature and advantage.Below with reference to figure, the present invention is further detailed explanation.
Brief description of the drawings
The accompanying drawing that forms the application's a part is used to provide a further understanding of the present invention, and schematic description and description of the present invention is used for explaining the present invention, does not form inappropriate limitation of the present invention.In the accompanying drawings:
Fig. 1 is the schematic flow sheet of the preferred embodiment of the present invention;
Fig. 2 is the material flow schematic diagram of the preferred embodiment of the present invention;
Fig. 3 is the equipment flowsheet schematic diagram of the preferred embodiment of the present invention;
Fig. 4 is the absorption tower internal structure schematic diagram of the preferred embodiment of the present invention.
Marginal data:
1, waste water regulating tank; 2, spray pump; 3, air blast; 4, stripping tower; 5, absorption tower; 6, induced crystallization groove; 7, centrifuge; 8, ammonium sulfate liquor groove; 9, absorption pump; 10, vibrated fluidized bed; 510, air inlet; 520, overflow pipe; 530, riser; 540, tower base plate; 550, the first packing layer; 560, spraying layer; 570, the second packing layer; 580, gas outlet.
Detailed description of the invention
Below in conjunction with accompanying drawing, embodiments of the invention are elaborated, but the multitude of different ways that the present invention can be defined by the claims and cover is implemented.
Referring to Fig. 1, an aspect of of the present present invention provides a kind of stripping exhaust gas treating method, comprises the following steps:
1) absorb: stripping tail gas is passed in absorption liquid, and tail gas and containing ammonium liquid is absorbed;
2) crystallization: will pass in crystalline mother solution and carry out crystallization containing ammonium liquid, and obtain ammonia sulfate crystal;
Stripping tail gas is by gained waste gas after conventional stripping processing ammonia nitrogen waste water.Ammonia nitrogen waste water is conventional pending ammonia nitrogen waste water.Absorption liquid is that the concentrated sulfuric acid and crystalline mother solution are 8～20kg: 1m by mass volume ratio
3.
Absorption step completes in absorption tower, and absorption tower structure is referring to Fig. 2.Bottom, absorption tower sidewall is provided with air inlet 510.Stripping tail gas enters in absorption tower 5 from air inlet 510.The top of air inlet 510, offers overflow pipe 520 on 5 sidewalls of absorption tower.Liquid after absorption flows out from overflow pipe 520.The lower inner wall on absorption tower 5 is provided with tower base plate 540.Tower base plate 540 aligns with the lower limb of overflow pipe 520.The middle part of tower base plate 540 offers riser 530.Enter stripping tail gas in absorption tower 5 rises up into absorption tower 5 top by riser 530.The stage casing, inside on absorption tower 5 is provided with the first packing layer 550.The top of the first packing layer 550 is provided with spraying layer 560.Spraying layer 560 is made up of multiple spray heads.Absorption liquid sprays from spraying layer 560.The top of spraying layer 560 is provided with the second packing layer 570.The first packing layer 550, the second packing layer 570, spraying layer 560 are all arranged in absorption tower 5.On the end face on absorption tower 5, set out gas port 580.Absorbing tail gas discharges from gas outlet 580.Can increase the contact area of stripping tail gas and absorption liquid by the first packing layer 560 and the second packing layer 570 are set, improve absorption efficiency.Adopt the absorption tower 5 of this structure can promote separating out of ammonia in stripping tail gas, there is not crystallization in the ammonium sulfate containing in ammonium liquid forming simultaneously.
Stripping tail gas enters bottom, absorption tower, is absorbed the ammonia absorbent solution absorption that tower top sprays, and generates saturated ammonium sulfate solution.
The ammonia that the method can effectively be processed blow-off method in the waste gas producing after ammonia nitrogen waste water reclaims, and makes stripping waste gas can reach discharge standard.If adopt the concentrated sulfuric acid directly to absorb stripping tail gas, because concentrated sulfuric acid concentration is higher, will produce the ammonium sulfate that concentration is higher in absorption tower.Because ammonium sulfate concentration in this solution often can reach crystallization concentration, thereby ammonium sulfate can be separated out at absorption tower intercrystalline.The ammonia sulfate crystal of separating out can stop up absorption tower, causes absorption technique to continue, and impact is produced.And adopt absorption liquid provided by the invention.This absorption liquid is by adjusting the addition of the concentrated sulfuric acid and the addition of crystalline mother solution, increase the degree of supersaturation of the ammonium sulfate forming after absorbing in absorption tower, make ammonium sulfate degree of supersaturation in whole absorption process in critical crystallization Jie Wen district, avoid ammonium sulfate in absorption tower due to supersaturation direct crystallization separate out.And then while having avoided the employing concentrated sulfuric acid directly to absorb stripping tail gas, the normal ammonium sulfate occurring is separated out the problem of blocking absorption tower at absorption tower intercrystalline.
Adopt this absorption liquid can also make the ammonia in stripping tail gas in absorption tower, absorb completely.Reduce the ammonia content being discharged in atmosphere, play the effect of protection of the environment.Preferably adopt the concentrated sulfuric acid of concentration > 80% to absorb, the sulfuric acid water content of this concentration is low, and absorbing ammonia gained without heating evaporation, can obtain ammonium sulfate by direct crystallization containing ammonium liquid, thereby plays the effect that reduces energy consumption.If the ammonium sulfate degree of supersaturation producing after concentrated sulfuric acid concentration lower than 80% time, absorbs is not high, be unfavorable for ammonium sulfate direct crystallization.Simultaneously in absorption and crystallization process, the heat that the sulfuric acid self that concentration is lower discharges cannot make contained humidity in sulfuric acid volatilize completely, and therefore moisture constantly accumulation in crystal solution, cannot keep water balance, need to reduce wherein moisture by follow-up heating, thereby increase energy resource consumption.
After absorbing, gained can directly pass into and in induced crystallization groove, carry out crystallization containing ammonium liquid.In induced crystallization groove, place in advance crystalline mother solution.Crystalline mother solution is the solution of liquid containing ammonium sulfate crystal seed.In crystalline mother solution, the solid content of crystal seed is 20～60%.Adopt this crystalline mother solution can make all to separate out containing the ammonium sulfate overwhelming majority in ammonium liquid.Ensure simultaneously crystalline mother solution after using mix with the concentrated sulfuric acid after during as absorption liquid, can make ammonium sulfate in absorption tower in hypersaturated state, prevent that ammonium sulfate from separating out in absorption tower.Crystal seed solid content lower than 20% time, induced crystallization poor effect.Crystal seed solid content higher than 60% time, stirs resistance and increases in groove, energy consumption is too high.Crystal seed solid content in preferred crystalline mother solution is 20～40%.Now absorption liquid is more thorough to the absorption of ammonia, and ammonium sulfate can be in hypersaturated state in whole absorption process.Avoid ammonium sulfate to separate out in absorption tower completely.
Preferably the acidity of crystalline mother solution is 2～10mmol/L.Adopt the crystalline mother solution of this acidity can make sulfate ion in ammonium sulfate and ammonium radical ion in free state.Avoid because crystalline mother solution acidity is too high, cause sulfate ion and ammonium radical ion to be easy in conjunction with separating out, and produce crystal in absorption tower.Can promote the combination of the two that it is separated out by the follow-up mode stirring in induced crystallization groove.Preferably in crystallisation step, mixing speed is 30～60rpm.Under this speed, stir, can make fully to contact with the crystal seed in crystalline mother solution with ammonium radical ion containing the free sulfuric acid radical ion in ammonium liquid.Under this speed, stir, the ammonia sulfate crystal in groove and solution can be realized AUTOMATIC ZONING.Mixing speed is during lower than 30rpm, and ammonium sulfate crystal seed mainly concentrates on crystallization tank bottom, dispersed poor, induced crystallization poor effect.Mixing speed during higher than 60rpm, stirs turbulence intensity larger, and crystal is difficult to realize AUTOMATIC ZONING and Separation of Solid and Liquid.Crystallization is preferably carried out in induced crystallization groove.
For gained ammonia sulfate crystal, after preferably it being dehydrated, obtain ammonium sulfate product.Ammonium sulfate product output reaches 192.5kg/ hour.Output is higher.In ammonium sulfate product, moisture is 0.8%, and nitrogen content is 20.84%, and free acid concentration is 0.15%, and product quality reaches the quality requirement of certified products in " ammonium sulfate national standard (GBT535-1995) ".
Referring to Fig. 3, another aspect of the present invention also provides a kind of nitrogen-containing wastewater processing method, comprises the following steps:
1) stripping: regulate after the pH value of ammonia nitrogen waste water, after stripping air-blowing is de-, produce stripping tail gas and deamination waste water;
2) stripping tail gas is processed by aforesaid method, produced and absorb tail gas;
Absorbing tail gas enters in stripping step as stripping gas.
The equipment method of wastewater treatment provided by the invention that the present invention also provides a kind of above-mentioned nitrogen-containing wastewater processing method to use on the other hand can use in sewage treatment equipment as shown in Figure 4.This equipment comprises waste water regulating tank 1, spray pump 2, air blast 3, stripping tower 4, absorption tower 5, induced crystallization groove 6, centrifuge 7, ammonium sulfate liquor groove 8, absorption pump 9, vibrated fluidized bed 10.The liquid outlet of waste water regulating tank 1 is connected with spray pump 2.Spray pump 2 is connected with the spray thrower inlet in stripping tower 4.The delivery port of stripping tower 4 bottoms is connected with waste water regulating tank 1.The deamination waste water producing enters in waste water regulating tank 1, carries out circular treatment, processes to reduce stripping the ammonia content in waste liquid that produced.Avoid the too high problem of waste liquid ammonia content that produces in conventional stripping processing procedure.The gas outlet that the top of stripping tower 4 arranges is connected with the air inlet on absorption tower 5.The gas outlet at 5 tops, absorption tower is connected with air blast 3.The absorption waste gas producing from absorption tower 5 enters in stripping tower 4 again through the pressurization of air blast 3, uses as stripping gas.
The liquid outlet on absorption tower 5 is connected with induced crystallization groove 6.The brilliant mouth that goes out of induced crystallization groove 6 is connected with centrifuge 7.The solid material outlet of centrifuge 7 is connected with vibrated fluidized bed.After being connected with the liquid outlet of induced crystallization groove 6, the liquid outlet of centrifuge 7 is connected with the inlet of ammonium sulfate liquor groove 8.For storing from the crystalline mother solution of centrifuge 7 and 6 generations of induced crystallization groove.The liquid outlet of ammonium sulfate liquor groove 8 is connected with absorption pump 9.The liquid outlet of absorption pump 9 is connected with the spraying layer 560 at 5 tops, absorption tower.
The processing procedure of ammonia nitrogen waste water is as follows: first ammonia nitrogen waste water enters in waste water regulating tank 1 and regulates pH value with lime or liquid caustic soda.First ammonia nitrogen waste water needs to regulate pH value so that wherein contained ammonia nitrogen as much as possible with NH
3form exists.Can adopt waste water regulating tank 1 to regulate.After preferably regulating, the pH value of waste water is 10.0～13.0.This is because in the time of the pH of waste water < 10.0, NH
3breadth coefficient in ammonia nitrogen is less, and it is lower that the ammonia nitrogen refuse after stripping in waste water is removed efficiency.When wastewater pH > 13.0, regulate the reagent cost of pH value of waste water higher.
Regulate waste water after pH value through the pressurized transport of spray pump 2 spray thrower to stripping tower 4 inner tops, evenly sprinkling and under.Open air blast 3.While operation at the beginning, can first pass into air as stripping gas.Waste water enters stripping tower 4 inside and on filler, forms moisture film.The stripping air-flow (as air) rising at the bottom of moisture film and tower comes in contact mass transfer, and the ammonia nitrogen in waste water enters in stripping tail gas.Enter 4 bottoms, absorption tower containing the stripping tail gas of ammonia, be absorbed that tower top sprays and lower ammonia absorption liquid absorbs, generation saturated ammonium sulfate solution.The absorption waste gas leaving from 5 tops, absorption tower enters air blast 3 and again enters in stripping tower 4, as stripping gas at stripping tower 4 internal operations.Form circulation.In this device, gas can be realized and recycling, and stripping process is airtight all the time.Adopt sealing and circulating stripping technology, absorb tail gas replaces air as stripping air-flow, avoid the repeated multiple times stripping tower that enters of airborne carbon dioxide, cause in stripping tower and form calcium carbonate accumulation and fouling.
The processing of stripping waste gas is undertaken by preceding method.
The deamination waste water leaving from stripping tower 4 enters waste water regulating tank 1 again.Circulation enters in stripping tower 4 and carries out stripping processing again, to reduce the ammonia content in deamination waste water.Making blow-off method remove ammonia nitrogen can be for the treatment of containing the higher waste water of ammonia nitrogen amount.Water outlet when ammonia-nitrogen content is 200～500mg/L in deamination waste water after treatment.
That leaves from absorption tower 5 enters and in induced crystallization groove 6, carries out crystallization treatment containing ammonium liquid.Saturated ammonium sulfate solution enters the induced crystallization groove 6 of liquid containing ammonium sulfate crystal seed, under the induced crystallization effect of crystal seed, saturated ammonium sulfate solution can be in groove direct crystallization.Crystal is deposited to induced crystallization groove 6 bottoms and regularly discharges.
Processing by follow-up centrifuge 7 separates produced ammonia sulfate crystal with crystalline mother solution.The crystalline mother solution producing in the interior unnecessary crystalline mother solution of induced crystallization groove 6 and centrifuge 7 enters in ammonium sulfate liquor groove 8.After the ratio of crystalline mother solution and the concentrated sulfuric acid regulates in ammonium sulfate liquor groove 8, again enter that absorption tower 5 is interior to be used as absorption liquid.
Embodiment
In following examples and comparative example, material used and equipment are commercially available.
Embodiment 1
Adopt equipment as shown in Figure 4 to process.Wastewater source is in ammonium tungstate crystalline mother solution, and wastewater flow is 8.0m
3/ hour, the about 7000mg/L of ammonia nitrogen in waste water concentration.
Regulate pH value: with lime adjusting pH value of waste water to 12.0.
Stripping: waste water is in continuous stripping processing procedure, and water outlet ammonia nitrogen concentration is stabilized in 370mg/L left and right, has no scale formation in stripping tower 5.Absorb circulation of tail gas and enter the interior also replaces air of stripping tower 5 as stripping air-flow.
Absorb: stripping tail gas is absorbed by the mixed liquor of 98% the concentrated sulfuric acid and ammonium sulfate (crystalline mother solution).Absorption liquid is that the concentrated sulfuric acid and crystalline mother solution are 15kg: 1m by mass volume ratio
3, the solid content of crystalline mother solution is 40%.Having no obvious ammonium sulfate crystallization and clogging at the bottom of the absorption tower without plus seed and in outlet conduit.Tail gas and containing ammonium liquid is absorbed.
Crystallization: enter and carry out crystallization treatment in induced crystallization groove containing ammonium liquid.In crystalline mother solution, acidity is 5mmol/L.In groove, the solid content of crystal seed is 40%, and mixing speed is 40rpm.Obtain obtaining ammonium sulfate product through super-dry after ammonia sulfate crystal.Ammonium sulfate product output reaches 192.5kg/ hour, in ammonium sulfate product, moisture is 1.69%, nitrogen content is 20.84%, and free acid concentration is 0.15%, and product quality reaches the quality requirement of certified products in " ammonium sulfate national standard (GBT535-1995) ".
Embodiment 2
Be with the difference of embodiment 1: while regulating pH value, the pH value of nitrogen waste water is adjusted to 10.0; Absorption liquid is that the concentrated sulfuric acid and crystalline mother solution are 8kg: 1m by mass volume ratio
3; Concentrated sulfuric acid concentration is 81%; In crystalline mother solution, crystal seed solid content is 60%; In crystalline mother solution, acidity is 2mmol/L; In crystallisation step, mixing speed is 30rpm.
Embodiment 3
Be with the difference of embodiment 1: while regulating pH value, the pH value of nitrogen waste water is adjusted to 13.0; Absorption liquid is that the concentrated sulfuric acid and crystalline mother solution are by mass volume ratio 20kg: 1m
3; Concentrated sulfuric acid concentration is 98%; In crystalline mother solution, crystal seed solid content is 20%; In crystalline mother solution, acidity is 10mmol/L; In crystallisation step, mixing speed is 60rpm.
Comparative example 1:
Wastewater source is in ammonium tungstate crystalline mother solution, and wastewater flow is 8.0m
3/ hour, the about 7000mg/L of ammonia nitrogen in waste water concentration, device therefor and technological process are referring to Fig. 1～4.The gas that the difference of equipment is to enter in stripping tower 4 is air, but not absorbs tail gas.With lime adjusting pH value of waste water to 12.0, absorb tail gas and do not enter stripping tower, additional air is as stripping air-flow.Waste water is after stripping is processed, and water outlet ammonia nitrogen concentration is down to 400mg/L.Along with the increase of stripping time, water outlet ammonia nitrogen concentration constantly increases, and stripping efficiency reduces gradually, and the continuous operation stability of stripping process is not good.Find after testing, stripping process operation is after 8 hours, and obvious scale formation all appears in the Ta Bi of stripping tower and tower base plate, and foulant is precipitation of calcium carbonate.
Comparative example 2
Wastewater source is in ammonium tungstate crystalline mother solution, and wastewater flow is 8.0m
3/ hour, the about 7000mg/L of ammonia nitrogen in waste water concentration, device therefor and technological process are referring to Fig. 1～4.Regulate pH value of waste water to 12.0 with lime, absorb circulation of tail gas and enter stripping tower replaces air as stripping air-flow.Waste water is in continuous stripping processing procedure, and water outlet ammonia nitrogen concentration is stabilized in 370mg/L left and right, has no scale formation in stripping tower.Stripping tail gas is absorbed by 30% dilute sulfuric acid and the mixed liquor of ammonium sulfate.In control flume, the solid content of crystal seed is 0%, and mixing speed is 40rpm.The degree of supersaturation of ammonium sulfate does not reach crystallization requirement, and therefore directly crystallization from induced crystallization groove, can only obtain ammonia sulfate crystal by the mode of heating evaporation, reclaims energy consumption higher.
Comparative example 3
Be that with the difference of comparative example 2 solid content of crystalline mother solution is 60%.
Comparative example 4
Wastewater source is in ammonium tungstate crystalline mother solution, and wastewater flow is 8.0m
3/ hour, the about 7000mg/L of ammonia nitrogen in waste water concentration, device therefor and technological process are referring to Fig. 1～4.Regulate pH value of waste water to 12.0 with lime, absorb circulation of tail gas and enter stripping tower replaces air as stripping air-flow.Waste water is in continuous stripping processing procedure, and water outlet ammonia nitrogen concentration is stabilized in 370mg/L left and right, has no scale formation in stripping tower.Stripping tail gas is absorbed by 98% the concentrated sulfuric acid and the mixed liquor of ammonium sulfate.Absorption liquid is that the concentrated sulfuric acid and crystalline mother solution are 30kg: 1m by mass volume ratio
3, in control flume, the solid content of crystal seed is 40%, mixing speed is 40rpm.The degree of supersaturation of ammonium sulfate is far away higher than its crystallization requirement, and therefore ammonium sulfate, in absorption tower and induced crystallization groove, crystallization occurs simultaneously.Crystallization processes operation is after 0.5 hour, and the tower base plate on absorption tower occurs that thickness is the ammonia sulfate crystal of 10cm, and absorbing tower bottom outlet pipeline stops up simultaneously, and absorption technique cannot normally carry out.
From above embodiment 1～3 and comparative example 1～3 contrast, for adopting absorption liquid provided by the invention, can effectively avoid the problem because ammonium sulfate crystallization is separated out in the absorption tower that adopts concentrated sulfuric acid absorption ammonium sulfate often to occur.The gas that blow-off method processing obtains can be processed by conventional method, widened the scope of application of blow-off method.
From comparative example 1, if do not adopt equipment provided by the invention to carry out stripping processing, easily cause to produce precipitation of calcium carbonate in stripping tower and stop stripping to remain valid to carry out.
From comparative example 2～3, if do not add the concentrated sulfuric acid in absorption liquid, in follow-up crystallization process, do not heat and cannot produce ammonium sulfate by direct crystallization.Even if reaching requirement of the present invention, the solid content of crystalline mother solution also still cannot realize object of the present invention.Illustrate that the present invention adopts the concentrated sulfuric acid to coordinate the effect that could effectively bring into play absorption liquid with crystalline mother solution.
From comparative example 4, if not in scope provided by the invention, cannot ensureing the ammonium liquid that contains producing in absorption tower, the proportion of composing of absorption liquid there is not crystallization ammonium sulfate on absorption tower.
These are only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.All spirit of the present invention and former within, any amendment of doing, be equal to replacement, improvement etc., within all should being included in protection scope of the present invention.
Claims (9)
1. an ammonia stripping exhaust gas treating method, is characterized in that, comprises the following steps:
1) absorb: described stripping tail gas is passed in absorption liquid, and tail gas and containing ammonium liquid is absorbed;
2) crystallization: pass in crystalline mother solution and carry out crystallization containing ammonium liquid described, obtain ammonia sulfate crystal;
Described absorption liquid is that the concentrated sulfuric acid and described crystalline mother solution are 8～20kg: 1m by mass volume ratio
3the mixed liquor being mixed to form;
In described crystalline mother solution, crystal seed solid content is 20～60%.
2. method according to claim 1, is characterized in that, in described crystalline mother solution, the solid content of crystal seed is 20～40%.
3. method according to claim 1, is characterized in that, the acidity of described crystalline mother solution is 2～10mmol/L.
4. method according to claim 1, is characterized in that, the concentration > 80% of the described concentrated sulfuric acid.
5. method according to claim 1, is characterized in that, described crystallisation step carries out under the condition stirring, and mixing speed is 30～60rpm.
6. method according to claim 1, is characterized in that, described ammonia sulfate crystal obtains ammonium sulfate product after dehydrating.
7. a nitrogen-containing wastewater processing method, is characterized in that, comprises the following steps:
1) stripping: regulate after the pH value of described ammonia nitrogen waste water, after stripping air-blowing is de-, produce ammonia stripping tail gas and deamination waste water;
2) described ammonia stripping tail gas is processed by the method described in any one in claim 1～6, produced and absorb tail gas;
Described absorption tail gas enters in described stripping step as stripping gas.
8. method according to claim 7, is characterized in that, the pH value of described ammonia nitrogen waste water is adjusted to 10.0～13.0.
9. one kind for the ammonia nitrogen sewage treatment equipment of method as claimed in claim 8 or 9, it is characterized in that, described ammonia nitrogen sewage treatment equipment comprises: waste water regulating tank (1), stripping tower (4), absorption tower (5), induced crystallization groove (6);
The liquid outlet of described waste water regulating tank (1) is connected with the inlet of described stripping tower (4), and the liquid outlet of described stripping tower (4) is connected with the inlet of described waste water regulating tank (1);
The gas outlet of described stripping tower (4) is connected with the air inlet of described absorption tower (5), the liquid outlet on described absorption tower (5) is connected with described induced crystallization groove (6), and the gas outlet of described absorption tower (5) is connected with the air inlet of described stripping tower (4);
The mother liquor outlet of described induced crystallization groove (6) is connected with the absorption liquid import of described absorption tower (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410355370.7A CN104117280A (en) | 2014-07-24 | 2014-07-24 | Ammonia stripping tail gas treatment method, ammonia-nitrogen wastewater treatment method and equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410355370.7A CN104117280A (en) | 2014-07-24 | 2014-07-24 | Ammonia stripping tail gas treatment method, ammonia-nitrogen wastewater treatment method and equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104117280A true CN104117280A (en) | 2014-10-29 |
Family
ID=51763052
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410355370.7A Pending CN104117280A (en) | 2014-07-24 | 2014-07-24 | Ammonia stripping tail gas treatment method, ammonia-nitrogen wastewater treatment method and equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104117280A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106241928A (en) * | 2016-08-15 | 2016-12-21 | 陕西华源矿业有限责任公司 | A kind of high ammonia-nitrogen wastewater processes technique and system |
| CN106348374A (en) * | 2016-08-31 | 2017-01-25 | 河北源清环保科技有限公司 | Deamination treating method and treating device for waste water |
| CN106698791A (en) * | 2017-01-04 | 2017-05-24 | 安徽国星生物化学有限公司 | Crystallization treatment process for ammonium salt in paraquat wastewater |
| CN109081492A (en) * | 2018-09-10 | 2018-12-25 | 盛发环保科技（厦门）有限公司 | A kind of technique and realization device of the reuse of desulfurization wastewater recycling |
| CN112250131A (en) * | 2020-09-23 | 2021-01-22 | 陕西华源矿业有限责任公司 | Ammonia nitrogen wastewater treatment method |
| CN112794339A (en) * | 2020-12-25 | 2021-05-14 | 中国科学院城市环境研究所 | Method and device for recovering ammonia in liquid |
| CN113087267A (en) * | 2021-04-30 | 2021-07-09 | 大连海事大学 | High ammonia nitrogen waste liquid purification process |
| CN114074998A (en) * | 2021-11-16 | 2022-02-22 | 中国科学院城市环境研究所 | Pretreatment method and system for recovering pipeline scaling prevention cooperative resources |
| CN115738352A (en) * | 2022-11-27 | 2023-03-07 | 浙江鑫旺钒业控股有限公司 | Crystallization tank and method for extracting ammonium sulfate and reusing ammonium sulfate in vanadium precipitation by adopting same |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203382515U (en) * | 2013-05-14 | 2014-01-08 | 武汉百富环保工程有限公司 | Ammonia recovery system based on saturation method |
| CN103894048A (en) * | 2014-04-18 | 2014-07-02 | 中石化南京工程有限公司 | Method for treating low-concentration ammonia-containing tail gas |
-
2014
- 2014-07-24 CN CN201410355370.7A patent/CN104117280A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203382515U (en) * | 2013-05-14 | 2014-01-08 | 武汉百富环保工程有限公司 | Ammonia recovery system based on saturation method |
| CN103894048A (en) * | 2014-04-18 | 2014-07-02 | 中石化南京工程有限公司 | Method for treating low-concentration ammonia-containing tail gas |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106241928A (en) * | 2016-08-15 | 2016-12-21 | 陕西华源矿业有限责任公司 | A kind of high ammonia-nitrogen wastewater processes technique and system |
| CN106348374A (en) * | 2016-08-31 | 2017-01-25 | 河北源清环保科技有限公司 | Deamination treating method and treating device for waste water |
| CN106348374B (en) * | 2016-08-31 | 2023-09-26 | 河北源清环保科技有限公司 | Deamination treatment method and treatment device for wastewater |
| CN106698791A (en) * | 2017-01-04 | 2017-05-24 | 安徽国星生物化学有限公司 | Crystallization treatment process for ammonium salt in paraquat wastewater |
| CN109081492A (en) * | 2018-09-10 | 2018-12-25 | 盛发环保科技（厦门）有限公司 | A kind of technique and realization device of the reuse of desulfurization wastewater recycling |
| CN112250131A (en) * | 2020-09-23 | 2021-01-22 | 陕西华源矿业有限责任公司 | Ammonia nitrogen wastewater treatment method |
| CN112794339A (en) * | 2020-12-25 | 2021-05-14 | 中国科学院城市环境研究所 | Method and device for recovering ammonia in liquid |
| CN113087267A (en) * | 2021-04-30 | 2021-07-09 | 大连海事大学 | High ammonia nitrogen waste liquid purification process |
| CN114074998A (en) * | 2021-11-16 | 2022-02-22 | 中国科学院城市环境研究所 | Pretreatment method and system for recovering pipeline scaling prevention cooperative resources |
| CN114074998B (en) * | 2021-11-16 | 2023-11-10 | 中国科学院城市环境研究所 | Pretreatment method and system for preventing pipeline scaling and recovering cooperative resources |
| CN115738352A (en) * | 2022-11-27 | 2023-03-07 | 浙江鑫旺钒业控股有限公司 | Crystallization tank and method for extracting ammonium sulfate and reusing ammonium sulfate in vanadium precipitation by adopting same |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104117280A (en) | Ammonia stripping tail gas treatment method, ammonia-nitrogen wastewater treatment method and equipment | |
| CN105060545B (en) | A kind of system and method for sofening treatment Desulphurization for Coal-fired Power Plant waste water | |
| CN105254084B (en) | A kind of bipolar membrane electrodialysis treatment method and device of desulfurization wastewater | |
| US5707514A (en) | Water treating method and apparatus treating waste water by using ion exchange resin | |
| US20080308505A1 (en) | System and Process for Removal of Phosphorous and Ammonia from Aqueous Streams | |
| CN100393636C (en) | Process for treating waste water of high concentration containing phosphorus | |
| CN109384332A (en) | A kind of method of coal burning flue gas desulfurization wastewater treatment | |
| CN106277419A (en) | The method and apparatus that a kind of ammonia nitrogen waste water processes | |
| CN104058548A (en) | Denitrification, desalination and recycling process of stainless steel cold rolling acidic waste water | |
| CN104591435A (en) | Treatment method for industrial wastewater | |
| CN104743746A (en) | Method and device for treating wastewater of iron oxide red | |
| CN204874164U (en) | Zero release processing system of desulfurization waste water | |
| US20090026141A1 (en) | Effluent treatment process | |
| CN105502765A (en) | System and method for treating desulfurization waste water and recycling resources | |
| CN111547919A (en) | Sintering plant desulfurization wastewater resource zero-discharge process and system | |
| CN105347592A (en) | Recycling zero-emission treatment process for desulfurization wastewater | |
| CN105461136A (en) | System and method for comprehensive treatment of wastewater of thermal power plant and recovery of chemical resources | |
| CN103086558A (en) | Treatment method of copper chloride hydroxide production wastewater | |
| CN206985809U (en) | A kind of phenylhydrazine hydrochloride waste water deaminizing workshop section mixing feeding device | |
| CN203877954U (en) | MAP-synthesis-based turbulence-state dephosphorization device | |
| CN104211106B (en) | A kind of carbonated rare earth preparation method not producing ammonia nitrogen waste water | |
| CN206901925U (en) | The device of novel desulphurization wastewater treatment | |
| CN105777221B (en) | Method for preparing organic carbon fertilizer from high-concentration lysine fermentation waste liquid | |
| CN108128829A (en) | Taurine waste water zero discharge treatment process and taurine wastewater zero discharge processing unit | |
| US11453606B2 (en) | Process and plant for purification of waste from zootechnical sources |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20141029 |