CN100429157C - Method for treating ammonia nitrogen wastewater - Google Patents
Method for treating ammonia nitrogen wastewater Download PDFInfo
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- CN100429157C CN100429157C CNB2005101174302A CN200510117430A CN100429157C CN 100429157 C CN100429157 C CN 100429157C CN B2005101174302 A CNB2005101174302 A CN B2005101174302A CN 200510117430 A CN200510117430 A CN 200510117430A CN 100429157 C CN100429157 C CN 100429157C
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Abstract
This invention relates to a method for treating ammonia nitrogen wastewater, especially high-concentration ammonia nitrogen wastewater produced during manufacture of oil-refinery catalyst. The method comprises: (1) adjusting the pH value of the wastewater, and solid-liquid separating to remove suspended matters and dissolved Si2+, Al3+ and their compounds; (2) adding Ca2+ to form CaSO4 precipitate, and solid-liquid separating to reduce acidic matters in the wastewater; (3) adding CO32- to form CaCO3 precipitate, and solid-liquid separating to remove Ca2+ in the wastewater; (4) steam-stripping for deamination, and performing biochemical treatment so that wastewater reaches state discharge standards. The method can solve the problems of low effect on removing suspended matters and dissolved Si2+, Al3+ and their compounds, scaling and column blockage during steam-stripping process, and the need for a large amount of alkali added, and can improve wastewater treatment effect.
Description
Technical field
The present invention relates to a kind of processing method of industrial waste water, especially a kind of treatment process of high-concentration ammonia nitrogenous wastewater.
Background technology
Ammonia nitrogen is a kind of water surrounding to be had the pollution substance that has a strong impact on, and mainly shows as: make body eutrophication, promote algae reproduction, the dissolved oxygen in the mass consumption water causes organism in water death, water body fouling etc.Ammonia nitrogen concentration in all strict restriction waste water in countries in the world, the emission standard that China adopts at present be " waste water comprehensive discharge standard " (GB8978-1996), this standard enters the waters according to waste water difference is divided into two-stage with the ammonia nitrogen emission standard: primary standard ammonia nitrogen emission concentration is less than or equal to 15mg/L, and secondary standard ammonia nitrogen emission concentration is less than or equal to 25mg/L.
The method of handling ammonia nitrogen waste water at present is more, mainly contains: air stripping method, exchange resin method, break point chlorination, membrane filter method, chemical precipitation method and biological process etc.
Air stripping method at first transfers to alkalescence with waste water, makes NH wherein
4 +Ion changes amino molecule into, removes ammonia through stripping then; Because the concentration of ammonia is lower, not easy to be recycled in the stripping gas, directly discharging can cause secondary pollution.Exchange resin method, break point chlorination and membrane filter method are owing to be vulnerable to the interference of other pollutent in the waste water, poor processing effect, processing cost height.Chemical precipitation method utilizes ammonia and phosphoric acid salt, magnesium oxide reaction to generate the magnesium ammonium phosphate (MgNH that is insoluble in water
4PO
4) remove the ammonia nitrogen in the waste water; Magnesium ammonium phosphate can be used as fertilizer of crops, but the magnesium ammonium phosphate that this method obtains often contains the deleterious material of farm crop, can't utilize.
Biological process is a main method of handling low-concentration ammonia-nitrogen waste water at present.To the waste water of the lower concentration of ammonia nitrogen concentration below 300mg/L, general direct employing biological process is handled (anaerobic denitrifying--aerobic nitrification); To the intermediate concentration waste water of ammonia nitrogen concentration at 300～1000mg/L, because of its ammonia nitrogen concentration to production by biological toxigenicity and restraining effect, general at first the ammonia nitrogen concentration of waste water is diluted to below the 300mg/L, adopt biological process to handle then; To the high-concentration ammonia nitrogenous wastewater of ammonia nitrogen concentration more than 1000mg/L, generally adopt the ammonia in the steam stripped method recovery waste water.
Ammonia nitrogen waste water treatment method of the present invention is mainly handled the high-concentration ammonia nitrogenous wastewater that produces in the oil refining catalyst production.Oil refining catalyst is used for petroleum refining process, and adopting rare earth NaY type and rare earth NaX type zeolite usually is raw material, with (NH
4)
2SO
4Or NH
4Cl is to the Na in the zeolite
+Exchange, generate NH
4Y or NH
4X type oil refining catalyst.In the production process of oil refining catalyst, can produce a large amount of factory effluents, be characterized in: except that containing ammonia nitrogen, also contain ion and colloidal compound that tiny suspended substance of a large amount of particles and dissolved contain silicon and aluminium in the waste water.
In the prior art, Chinese patent CN1367147A discloses a kind of high-concentration ammonia nitrogen waste water treatment method, this method at first adds unslaked lime and calcium peroxide in waste water, through stirring, aeration, add sodium hydroxide and calcium perborate, through stirring, aeration, add aluminium salt or molysite flocculation agent, through stirring, aeration, add polymeric flocculant at last, stir after settlement separate.This method has not only been wasted resource, and has been caused secondary pollution because the ammonia nitrogen in the waste water directly enters atmosphere.
In the prior art, Chinese patent CN1078872C discloses the recoverying and utilizing method of suspended substance in a kind of catalyst production waste water, this method is utilized the solid materials in the millipore filtration technology recovery ammonia nitrogen waste water, but do not have to reclaim the ammonia nitrogen that is dissolved in the waste water, the ammonia nitrogen waste water of high density can not directly discharge.
In conjunction with above prior art, this type of wastewater treatment method mainly contains two kinds at present: a kind of method is that waste water is at first removed suspended substance through precipitation, adds sodium hydroxide then, reclaims ammonia through stripping; Another method is at first by membrane filtration removal suspended substance, to add sodium hydroxide then, through stripping recovery ammonia.
There is following problem in aforesaid method:
One, the precipitator method are removed suspended substance, because particle is tiny, the suspended substance sedimentation effect is poor, and the sial material that is dissolved in the waste water can not precipitate removal, and filler fouling and stifled tower take place easily for suspended substance and easily become dirty sial material to enter stripping tower.
Two, membrane filter method is removed suspended substance, because the particle of suspended substance is tiny and waste water in the thickness character of colloidal compound, filtering membrane stops up easily, and micro-filtration and ultra-filtration membrane can not remove dissolved sial ion and compound thereof, and filler fouling and stifled tower take place when stripping equally easily.
Three, can be for ammonia nitrogen is converted into by isolating ammonium hydroxide of stripping and ammonia, waste water needed to transfer to alkalescence before stripping, and general 1 ton of above-mentioned waste water of stripping need add sodium hydroxide 20～25g kilogram, and the cost that adds alkali is higher.
Summary of the invention
Prior art exists in order to solve: suspended substance removal weak effect, dissolved sial material are brought stripping process into and are caused cost that fouling and stifled tower, stripping deamination add alkali than problems such as height, and treatment process of the present invention is achieved in that
The ammonia nitrogen waste water that the present invention handles, containing wastewater from catalyst and molecular sieve waste water composition in mainly producing by oil refining catalyst.Wherein containing wastewater from catalyst is from the Catalyst Production device, and its suspended substance is that 500～3000mg/L, ammonia nitrogen are 50～500mg/L; The molecular sieve alkaline waste water is from the NaY crystallization mother liquor and the washing water of molecular sieve device, and its suspended substance is 300～500mg/L; Acidic zeolite waste water is from the exchange and the wash filtrate of molecular sieve device, and its suspended substance is that 1000～1200mg/L, ammonia nitrogen are 5000～10000mg/L.Generally be acid after above-mentioned waste water mixes, the dissolved matter in the waste water comprises: ammonia nitrogen, SO
4 2-, SiO
2, Al
3+And Na
+Deng, the main component of suspended substance is: SiO
2And Al (OH)
3Deng.
This treatment process may further comprise the steps successively:
A. remove sial: add alkali in described waste water, making its pH is 5.0～10.5; Pass through solid-liquid separation then, obtain parting liquid.
The alkali that adds is preferably calcium oxide, calcium hydroxide or sodium hydroxide; Make the pH of waste water be preferably 6.5～9.0.Regulate suitable pH value, deliquescent sial ion and compound thereof are resolved in the waste water comes out, and forms suspended substance; Generally speaking, the concentration of suspension of regulating the preceding waste water of pH value is 500～2000mg/L, and the concentration of suspension of regulating pH value back waste water reaches 1000～3000mg/L.
The method of solid-liquid separation is more, preferably adopts the method for flocculation sediment; Flocculation agent can be selected the known product of the industry, preferably adopts polymeric flocculant--and polyacrylamide is or/and polymerize aluminum chloride; Wherein, the concentration of polyacrylamide is 2～30mg/L, and preferred concentration is 4～10mg/L, and the concentration of polymerize aluminum chloride is 10～100mg/L, and preferred concentration is 20～60mg/L; Flocculation temperature is 10～40 ℃, and preferred flocculation temperature is 15～35 ℃.
In waste water, add flocculation agent, under suitable temperature, stir, leave standstill, make fine particle thing and original suspended substance of separating out in the waste water be condensed into larger particles, after precipitation was removed, the total concn of sial ion and compound thereof was reduced to 0.5～60mg/L in the parting liquid.
B. remove SO
4 2-: in parting liquid, add Ca
2+, the Ca of adding
2+With SO in the parting liquid
4 2-Mol ratio be 0.5: 1～3: 1; Pass through solid-liquid separation then, obtain parting liquid.
Preferably, in parting liquid, add calcium oxide or calcium hydroxide; The Ca that adds
2+With SO in the parting liquid
4 2-Mol ratio be preferably 0.5: 1～1.5: 1; The method of solid-liquid separation is more, preferably adopts sedimentary method.
Remove SO
4 2-Reaction formula be:
Through above-mentioned reaction, SO
4 2-With Ca
2+Generated water-fast calcium sulfate precipitation, the ammonium sulfate in the waste water is converted into can be by isolating ammonium hydroxide of stripping and ammonia.Precipitation is removed the acidic substance SO in the waste water
4 2-, be equivalent to before stripping, add sodium hydroxide and (remove a mole SO
4 2-Be equivalent to add the sodium hydroxide of a mole), that has reduced subsequent step stripping deamination adds the alkali cost.But, the Ca of adding
2+Amount is too much brought subsequent process into, can increase to remove Ca
2+Cost.Take all factors into consideration and add Ca
2+Cost, remove Ca
2+The alkali charge that reduces in cost and the stripping process is selected appropriate C a
2+With SO
4 2-Mol ratio.Through precipitation, the SO in the parting liquid
4 2-Reduce to 1000～20000mg/L by 10000～60000mg/L.
C. remove Ca
2+: in parting liquid, add CO
3 2-, the CO of adding
3 2-With Ca in the parting liquid
2+Mol ratio be 1: 1～10: 1; Pass through solid-liquid separation then, obtain parting liquid.
Preferably, in parting liquid, add yellow soda ash; The CO that adds
3 2-With Ca in the parting liquid
2+Mol ratio be preferably 2: 1～6: 1; The method of solid-liquid separation is more, preferably adopts the method for flocculation sediment; Flocculation agent can be selected the known product of the industry, preferably adopts polymeric flocculant--and polyacrylamide is or/and polymerize aluminum chloride; Wherein, the concentration of polyacrylamide is 2～30mg/L, and preferred concentration is 4～10mg/L, and the concentration of polymerize aluminum chloride is 10～100mg/L, and preferred concentration is 20～60mg/L; Flocculation temperature is 10～40 ℃, and preferred flocculation temperature is 15～35 ℃.
Removing SO
4 2-Parting liquid in contain the Ca of 200～1000mg/L
2+, Ca
2+Fouling and stifled tower can take place when the stripping deamination equally, utilize CO
3 2-And Ca
2+Reaction generates precipitation of calcium carbonate, removes the Ca in the parting liquid
2+Through flocculation sediment, Ca in the parting liquid
2+Concentration is reduced to 5～100mg/L.
D. stripping deamination: add alkali in parting liquid, making its pH is 9.5～13.0; Carry out stripping then and handle, obtain stripping liquid and reclaim ammonia.
The alkali that adds is preferably sodium hydroxide.Preferably, adopt stripping tower to carry out stripping and handle, above the import of stripping tower waste water, be provided with and remove the mist section; The distance of removing mist section and waste water import is preferably 0.1～0.5 meter; Stripping tower remove the mist section and stripping section is a packing section, filler is preferably regular type filler.
The reaction formula of deamination process is:
Remove NH
3Method more, wherein stripping takes off NH
3Simple efficient.The pH that regulates parting liquid is to alkalescence, and its ammonia nitrogen is converted into can be by isolating ammonium hydroxide of stripping and ammonia.
Stripping process is many to carry out in stripping tower, and stripping tower has stripping section, also rectifying section can be arranged, and rectifying section plays the effect except that mist simultaneously.The form of stripping tower can have various, for example tray column and packing tower; Filler can use bulk type filler or regular type filler, adopts efficient structured packing, help improving stripping section and tower still separating effect, reduced the concentration of ammonia nitrogen in the stripping liquid.The stripping cat head obtains reclaiming ammonia, can be back to use the Preparation of Catalyst system; Contain Na in the ammonia nitrogen waste water that the present invention handles
+, and in wastewater treatment process, added and contain Na
+Material, contain Na if reclaim in the ammonia
+Can influence its reuse; In stripping process, the Na in the waste water
+Mainly enter recovery ammonia, be provided with on stripping tower top and remove the mist section, can reduce the generation of entrainment phenomenon, reduce the Na that reclaims in the ammonia by the entrainment phenomenon
+Concentration.
Through stripping, the ammonia nitrogen concentration of tower still stripping liquid is the Na of 10～300mg/L, recovered overhead ammonia
+Concentration is 1～20mg/L.
E. add carbon compound in the stripping liquid of steps d, making the nitrogen carbon mol ratio of stripping liquid is 1: 1～1: 10, carries out aerobic biochemical then and handles.
The carbon compound that adds is preferably yellow soda ash or/and sodium bicarbonate makes the nitrogen carbon mol ratio of stripping liquid be preferably 1: 3～1: 7.
Ammonia nitrogen concentration is 10～300mg/L in the stripping liquid, and biochemical treatment can further reduce the ammonia nitrogen concentration in the waste water, realizes standard wastewater discharge.Biochemical process can adopt the bio anaerobic denitrification--and the aerobic nitrification treatment process, the carbon source of biochemical reaction can be used the inorganic carbide compound, as yellow soda ash, sodium bicarbonate, replaces organic carbon source, reduces the cost of biochemical treatment.After the biochemical treatment, the ammonia nitrogen concentration of draining reaches discharging standards less than 15mg/L.
One of treatment process of the present invention comparatively embodiment preferred be:
Contain ammonia nitrogen and SO in the described waste water
4 2-, Al
3+, SiO
2, this treatment process may further comprise the steps successively:
A. remove sial: add at least a in calcium oxide, calcium hydroxide and the sodium hydroxide in described waste water, making its pH is 6.5～9.0; Adopt the method for flocculation sediment to carry out solid-liquid separation then, obtain parting liquid; Wherein, flocculation agent is a polyacrylamide or/and polymerize aluminum chloride, and the concentration of flocculation agent is 4～70mg/L, and flocculation temperature is 15～35 ℃;
B. remove SO
4 2-: in parting liquid, add calcium oxide or calcium hydroxide, the Ca of adding
2+With SO in the parting liquid
4 2-Mol ratio be 0.5: 1～1.5: 1; Adopt sedimentary method to carry out solid-liquid separation then, obtain parting liquid;
C. remove Ca
2+: in parting liquid, add yellow soda ash, the CO of adding
3 2-With Ca in the parting liquid
2+Mol ratio be 2: 1～6: 1; Adopt the method for flocculation sediment to carry out solid-liquid separation then, obtain parting liquid; Wherein, flocculation agent is a polyacrylamide or/and polymerize aluminum chloride, and the concentration of flocculation agent is 4～70mg/L, and flocculation temperature is 15～35 ℃;
D. stripping deamination: add sodium hydroxide in parting liquid, making its pH is 9.5～13.0; Adopt stripping tower to carry out stripping then and handle, obtain stripping liquid and reclaim ammonia; Wherein, be provided with above the import of stripping tower waste water and remove the mist section, the waste water import is 0.1～0.5 meter with the distance of removing the mist section; Stripping tower remove the mist section and stripping section is a packing section, filler adopts regular type filler;
E. add yellow soda ash in the stripping liquid of steps d or/and sodium bicarbonate, making the nitrogen carbon mol ratio of stripping liquid is 1: 3～1: 7, carries out aerobic biochemical then and handles.
Treatment process of the present invention, by regulating the pH of waste water, dissolved silicon aluminum ion and compound thereof are separated out, from waste water through flocculation sediment, suspended substance and dissolved silicon aluminum ion and compound thereof are removed substantially in the waste water, problems such as fouling and stifled tower when having avoided the stripping deamination; Utilize Ca
2+With the SO in the waste water
4 2-Reaction generates the solid sulphuric acid calcium deposit, and that has reduced the stripping deamination adds the alkali cost; Through biochemical treatment, the wastewater to reach standard discharging standards.
Description of drawings
Fig. 1 is the schematic flow sheet of ammonia nitrogen waste water treatment method.
Fig. 2 is the structural representation of stripping tower.
Embodiment
Be described in further detail technical scheme of the present invention below in conjunction with embodiment, protection scope of the present invention is not limited to following embodiment.
Embodiment 1
Remove suspended substance and dissolved silicon aluminum material.
A kind of refining catalytic agent production waste water contains dissolved SiO in the waste water
2And Al
3+And suspended substance, the main component of suspended substance is SiO
2And Al (OH)
3, Al in the waste water
3+Concentration be 323.4mg/L, SiO
2Concentration be 124.4mg/L.
Add sodium hydroxide in waste water, making its pH value is 6.0; Add the flocculation agent polyacrylamide then, its concentration is 10mg/L; Through flocculation sediment, Al in the waste water
3+Concentration be 0.49mg/L, SiO
2Concentration be 40.5mg/L.
Embodiment 2～14
Remove suspended substance and dissolved silicon aluminum material.
Change kind, the pH of adjusting, the concentration of flocculation agent, the flocculation temperature of alkali, other are with embodiment 1, and wastewater treatment the results are shown in Table 1.
Table 1
Embodiment 15
Remove acidic substance SO
4 2-
A kind of refining catalytic agent production waste water, behind removal suspended substance and the dissolved silicon aluminum material, the SO of waste water
4 2-Concentration is 43200mg/L.
In waste water, add calcium hydroxide, the Ca of adding
2+With SO
4 2-The mole be 0.5: 1, through the precipitation, SO in the waste water
4 2-Concentration be 19150mg/L.
Embodiment 16～21
Remove acidic substance SO
4 2-
Change the Ca that contains that adds
2+Material, Ca
2+With SO
4 2-Mol ratio, other are with embodiment 15, wastewater treatment the results are shown in Table 2.
Table 2
Embodiment 22
Remove Ca
2+
A kind of refining catalytic agent production waste water is removed acidic substance SO
4 2-After, Ca in the waste water
2+Concentration is 458.7mg/L.
In waste water, add yellow soda ash, form precipitation of calcium carbonate; The CO that adds
3 2-With Ca
2+Mol ratio be 1: 1; In waste water, add polyacrylamide 8mg/L and polymerize aluminum chloride 20mg/L, through flocculation sediment, Ca in the waste water
2+Concentration be 99.6mg/L.
Embodiment 23～26
Remove Ca
2+
Change flocculant concentration, flocculation temperature, CO
3 2-With Ca
2+Mol ratio, other are with embodiment 22, wastewater treatment the results are shown in Table 3.
Table 3
Embodiment 27
The stripping deamination.
A kind of refining catalytic agent production waste water is removed Ca
2+After, ammonia nitrogen concentration is 5379mg/L in the waste water.
Adopt stripping tower stripping deamination; Stripping tower has stripping section [2] and removes mist section [1], stripping section [2] and remove mist section [1] and use regular type filler; Waste pipe [4] import is positioned at except that under the mist section [1], and vapour pipe [5] import is positioned under the tower bottoms face [3], and its opening direction down.
The stripping tower diameter is 0.20 meter, the height of stripping section [2] is 1.00 meters, and the height that removes mist section [1] is 0.15 meter, and the tower bottoms degree of depth is 0.30 meter, vapour pipe [5] import is positioned at 1/2 place of the tower bottoms degree of depth, and waste pipe [4] import is 0.30 meter with the distance of removing mist section [1].
Add sodium hydroxide in waste water, making its pH is 9.5.Behind the stripping, the ammonia nitrogen concentration of stripping liquid is 86mg/L at the bottom of the tower, the Na of recovered overhead ammonia
+Concentration is 2.2mg/L.
Embodiment 28
The stripping deamination.
The stripping tower structure is identical with embodiment 27.The ammonia nitrogen concentration of waste water is 3651mg/L, and it is 13.0 that adding sodium hydroxide makes the pH of waste water.Behind the stripping, the ammonia nitrogen concentration of stripping liquid is 69mg/L at the bottom of the tower, the Na of recovered overhead ammonia
+Concentration is 1.4mg/L.
Embodiment 29
Biochemical treatment.
A kind of refining catalytic agent production waste water, behind the stripping deamination, the ammonia nitrogen concentration of stripping liquid is 135mg/L.
Add yellow soda ash and sodium bicarbonate in waste water, making the nitrogen carbon mol ratio of waste water is 1: 4; Adopt aerobic process to carry out biochemical treatment, the treatment time is 8 hours.
The ammonia nitrogen concentration of handling the back bio-chemical effluent is 13mg/L, reaches discharging standards.
Embodiment 30～33
Biochemical treatment.
Change ammonia nitrogen concentration, nitrogen carbon molar ratio, the biochemical treatment time of stripping liquid, other are with embodiment 27, and wastewater treatment the results are shown in Table 4.
Table 4
| The biochemical treatment time (hour) | Nitrogen carbon mol ratio | The ammonia nitrogen concentration (mg/L) of biochemical water inlet | The ammonia nitrogen concentration of bio-chemical effluent (mg/L) | |
| Embodiment 30 | 8 | 1∶1 | 135 | 10.5 |
| Embodiment 31 | 6 | 1∶6 | 96 | 9.0 |
| Embodiment 32 | 6 | 1∶8 | 127 | 11.3 |
| Embodiment 33 | 6 | 1∶10 | 173 | 13.8 |
Claims (13)
1, a kind of method for treating ammonia-nitrogen wastewater contains ammonia nitrogen and SO in the described waste water
4 2-, Al
3+, SiO
2, this treatment process may further comprise the steps successively:
A. remove sial: add alkali in described waste water, making its pH is 5.0～10.5; Pass through solid-liquid separation then, obtain parting liquid;
B. remove SO
4 2-: in parting liquid, add Ca
2+, the Ca of adding
2+With SO in the parting liquid
4 2-Mol ratio be 0.5: 1～3: 1; Pass through solid-liquid separation then, obtain parting liquid;
C. remove Ca
2+: in parting liquid, add CO
3 2-, the CO of adding
3 2-With Ca in the parting liquid
2+Mol ratio be 1: 1～10: 1; Pass through solid-liquid separation then, obtain parting liquid;
D. stripping deamination: add alkali in parting liquid, making its pH is 9.5～13.0; Carry out stripping then and handle, obtain stripping liquid and reclaim ammonia.
2, method for treating ammonia-nitrogen wastewater according to claim 1 is characterized in that:
Among the step a, the alkali of adding is at least a in calcium oxide, calcium hydroxide and the sodium hydroxide; The pH that makes waste water is 6.5～9.0; Solid-liquid separation adopts the method for flocculation sediment.
3, method for treating ammonia-nitrogen wastewater according to claim 2 is characterized in that:
The flocculation agent of flocculation sediment is a polyacrylamide or/and polymerize aluminum chloride, and the concentration of flocculation agent is 2～130mg/L, and flocculation temperature is 10～40 ℃.
4, method for treating ammonia-nitrogen wastewater according to claim 3 is characterized in that:
The concentration of described flocculation agent is 4～70mg/L, and flocculation temperature is 15～35 ℃.
5, method for treating ammonia-nitrogen wastewater according to claim 1 is characterized in that:
Among the step b, in parting liquid, add calcium oxide or calcium hydroxide; The Ca that adds
2+With SO in the parting liquid
4 2-Mol ratio be 0.5: 1～1.5: 1; Solid-liquid separation adopts sedimentary method.
6, method for treating ammonia-nitrogen wastewater according to claim 1 is characterized in that:
Among the step c, in parting liquid, add yellow soda ash; The CO that adds
3 2-With Ca in the parting liquid
2+Mol ratio be 2: 1～6: 1; Solid-liquid separation adopts the method for flocculation sediment.
7, method for treating ammonia-nitrogen wastewater according to claim 6 is characterized in that:
The flocculation agent of flocculation sediment is a polyacrylamide or/and polymerize aluminum chloride, and the total concn of flocculation agent is 2～130mg/L, and flocculation temperature is 10～40 ℃.
8, method for treating ammonia-nitrogen wastewater according to claim 7 is characterized in that:
The total concn of described flocculation agent is 4～70mg/L, and flocculation temperature is 15～35 ℃.
9, method for treating ammonia-nitrogen wastewater according to claim 1 is characterized in that:
In the steps d, described alkali is sodium hydroxide; Adopt stripping tower to carry out stripping and handle, above the import of stripping tower waste water, be provided with and remove the mist section.
10, method for treating ammonia-nitrogen wastewater according to claim 9 is characterized in that:
The distance of removing mist section and waste water import is 0.1～0.5 meter; Stripping tower remove the mist section and stripping section is a packing section, filler adopts regular type filler.
11, according to the described method for treating ammonia-nitrogen wastewater of one of claim 1～10, it is characterized in that:
Add carbon compound in the stripping liquid of steps d, making the nitrogen carbon mol ratio of stripping liquid is 1: 1～1: 10, carries out aerobic biochemical then and handles.
12, method for treating ammonia-nitrogen wastewater according to claim 11 is characterized in that:
Described carbon compound is a yellow soda ash or/and sodium bicarbonate, and described nitrogen carbon mol ratio is 1: 3～1: 7.
13, a kind of method for treating ammonia-nitrogen wastewater contains ammonia nitrogen and SO in the described waste water
4 2-, Al
3+, SiO
2, this treatment process may further comprise the steps successively:
A. remove sial: add at least a in calcium oxide, calcium hydroxide and the sodium hydroxide in described waste water, making its pH is 6.5～9.0; Adopt the method for flocculation sediment to carry out solid-liquid separation then, obtain parting liquid; Wherein, flocculation agent is a polyacrylamide or/and polymerize aluminum chloride, and the concentration of flocculation agent is 4～70mg/L, and flocculation temperature is 15～35 ℃;
B. remove SO
4 2-: in parting liquid, add calcium oxide or calcium hydroxide, the Ca of adding
2+With SO in the parting liquid
4 2-Mol ratio be 0.5: 1～1.5: 1; Adopt sedimentary method to carry out solid-liquid separation then, obtain parting liquid;
C. remove Ca
2+: in parting liquid, add yellow soda ash, the CO of adding
3 2-With Ca in the parting liquid
2+Mol ratio be 2: 1～6: 1; Adopt the method for flocculation sediment to carry out solid-liquid separation then, obtain parting liquid; Wherein, flocculation agent is a polyacrylamide or/and polymerize aluminum chloride, and the concentration of flocculation agent is 4～70mg/L, and flocculation temperature is 15～35 ℃;
D. stripping deamination: add sodium hydroxide in parting liquid, making its pH is 9.5～13.0; Adopt stripping tower to carry out stripping then and handle, obtain stripping liquid and reclaim ammonia; Wherein, be provided with above the import of stripping tower waste water and remove the mist section, the waste water import is 0.1～0.5 meter with the distance of removing the mist section; Stripping tower remove the mist section and stripping section is a packing section, filler adopts regular type filler;
E. add yellow soda ash in the stripping liquid of steps d or/and sodium bicarbonate, making the nitrogen carbon mol ratio of stripping liquid is 1: 3～1: 7, carries out aerobic biochemical then and handles.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US10815132B2 (en) | 2017-04-21 | 2020-10-27 | China Petroleum & Chemical Corporation | Apparatus and method for treating waste water containing ammonium salts |
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