CN101891316B - Process for treating nitrogen-containing wastewater by ion exchange and reclaiming ammonium nitrate - Google Patents
Process for treating nitrogen-containing wastewater by ion exchange and reclaiming ammonium nitrate Download PDFInfo
- Publication number
- CN101891316B CN101891316B CN201010223219XA CN201010223219A CN101891316B CN 101891316 B CN101891316 B CN 101891316B CN 201010223219X A CN201010223219X A CN 201010223219XA CN 201010223219 A CN201010223219 A CN 201010223219A CN 101891316 B CN101891316 B CN 101891316B
- Authority
- CN
- China
- Prior art keywords
- nitrogen
- exchange resin
- strongly acidic
- weakly
- basic anion
- 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.)
- Expired - Fee Related
Links
Images
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention discloses a process for treating nitrogen-containing wastewater by ion exchange and reclaiming ammonium nitrate, and belongs to the technical field of environmental protection and wastewater treatment. The process is characterized in that: a strong acid cation exchanger and a weak alkali anion exchanger are connected in series to realize denitrification of the nitrogen-containing wastewater of a nitrogen fertilizer plant; the process is used for treating the high-concentration ammonia nitrogen and median-concentration nitrate nitrogen containing wastewater of the nitrogen fertilizer plant; strong acid cation exchange resin and weak alkali anion exchange resin are regenerated by adopting nitric acid and aqueous ammonia respectively; and the regenerated waste liquid ammonium nitrate is evaporated and concentrated to reclaim the ammonium nitrate. Compared with the traditional wastewater denitrification method, the process can remove ammonia nitrogen and nitrate nitrogen from the wastewater at the same time, reclaim the ammonium nitrate and recycle production water, does not produce secondary pollution, reclaims products from the pollutants, has obvious environmental benefit and economic benefit, and is a new path for treating the high-concentration ammonia nitrogen and median-concentration nitrate nitrogen containing wastewater of the nitrogen fertilizer plant.
Description
Technical field
A kind of treating nitrogen-containing wastewater by ion exchange of the present invention also reclaims the technology of an ammonium nitrate, belongs to environment protection and technical field of waste water processing.Specifically; Be to adopt strongly acidic cation exchanger-weakly-basic anion interchanger to connect to realize the processing of nitrogen fertilizer plant's nitrogenous effluent; Accomplish the removal of ammonia nitrogen and nitrate nitrogen in nitrogen fertilizer plant's nitrogenous effluent respectively with strongly acidic cation exchanger and weakly-basic anion interchanger; Strongly acidic cationic exchange resin and weakly basic anion exchange resin after exchange is handled adopt nitric acid and ammoniacal liquor to regenerate respectively, and regeneration waste liquid is an ammonium nitrate solution, can reclaim an ammonium nitrate through carrying after dense.
Background technology
Wastewater from nitrogenous fertilizer industry derives from phlegma, washing water and the system leak water etc. in nitrogen fertilizer plant's production process.The waste water composition is complicated, contains the ammonia nitrogen of high density.In addition, in do the phlegma that processing and manufacturing process that raw material carries out chemical fertilizer such as urea, an ammonium nitrate produces with synthetic ammonia, also contain in the nitrate nitrogen of concentration.Nitrate reduction in the tap water forms nitrite ion, and it can make the oxidation of divalent in the denatured hemoglobin molecule become ferric iron.The denatured hemoglobin non-reversibility ground that forms combines oxygen, lacks NADH-denatured hemoglobin enzyme system in the discontented trimestral infants, therefore is prone to suffer from methemoglobinemia, and nitrate salt also can be transformed into " three cause " material NSC 223080 in human body.The method of nitrogen fertilizer plant's nitrogenous effluent denitrogenation mainly contains at present: methods such as chemical precipitation method, ammonia stripping, stripping and biological denitrificaion.But the above two can only remove the ammonia nitrogen in the waste water, can not remove nitrate nitrogen.The biological denitrificaion method comprises biological nitration and denitrification, though can remove nitrate nitrogen, is not suitable for the wastewater from nitrogenous fertilizer industry of treatment of high concentration ammonia nitrogen.Major cause is: wastewater from nitrogenous fertilizer industry contains ammonia nitrogen in high density, suppresses the growth of nitrifier, under aerobic condition, is difficult to ammonia nitrogen is oxidized to nitrite and nitrate salt.In addition, carbonaceous organic material seldom is difficult to provide the biological denitrification process required carbon source in the wastewater from nitrogenous fertilizer industry, thereby influences the effect of biological denitrification bacterium.Therefore, biological denitrificaion method water outlet ammonia nitrogen and nitrate nitrogen all are difficult to up to standard.Specifically:
I, chemical precipitation method are to point to add phosphoric acid and Natural manganese dioxide formation magnesium ammonium phosphate sediment (MAP) in the waste water that contains ammonia nitrogen in high density, and this method can only be removed the ammonia nitrogen in the waste water, can not remove the nitrate nitrogen in the waste water, and the chemical precipitation method medicament is costly.
II, ammonia stripping and vaporizing extract process are after adding alkali raising pH to 9～11 in the sensing waste water, NH in the water
4 +Become molecular state ammonia, with reaching stripping denitrogenation purpose in air or the steam feeding water.The requirement of this technology alkali is big, and GWR is 3500～4000: 1 during air stripping, and power consumption is very big.The ammonia that stripping goes out causes secondary pollution to atmosphere, and noise is very big, and can not remove the nitrate nitrogen in the waste water.
III, biological denitrificaion method comprise biological nitration and denitrification.Biological nitration is meant under aerobic condition, through nitrite bacteria, ammonia nitrogen is oxidized to nitrite earlier, under the effect of Nitromonas, nitrite is converted into nitrate salt subsequently, reach nitrated fully, 1.0mg (NH
3-N)/and L just needs the dissolved oxygen of 4.6mg/L, and waste water oxygenic aeration power consumption is big, and this process receives Influence of Temperature very big.Wastewater from nitrogenous fertilizer industry contains ammonia nitrogen in high density, suppresses the growth of biological nitration bacterium, thereby even under aerobic condition, also be difficult to ammonia nitrogen is oxidized to nitrite and nitrate salt.
Denitrification is meant under anoxia condition, by the effect of denitrifying bacteria, with NO
3 -And NO
2 -Be reduced to N
2Process, the electron donor of this process is various carbon sources, in the wastewater from nitrogenous fertilizer industry carbonaceous organic material seldom, so biological denitrification process need replenish enough carbon sources, this is very expensive.The low temperature nitrification efficiency is very low simultaneously, and operational management is complicated, and the excess sludge of biological denitrificaion produces secondary pollution.
Summary of the invention
A kind of treating nitrogen-containing wastewater by ion exchange of the present invention and the purpose that reclaims an ammonium nitrate technology are; To the defective of art breading nitrogen fertilizer plant nitrogenous effluents such as chemical precipitation method, ammonia stripping, stripping and biological denitrificaion, a kind of strongly acidic cation exchanger that proposes effectively processing nitrogen fertilizer plant nitrogenous effluent is removed the ion-exchange treatment process that ammonia nitrogen-weakly-basic anion interchanger is removed nitrate nitrogen.Water outlet ammonia nitrogen and nitrate nitrogen after wastewater from nitrogenous fertilizer industry is handled reaches in " ammonia synthesizing industry pollution discharge standard " (GB 13458-2001) and the quality of groundwater standard III class tap water respectively to the requirement (GB/T14848-93) of nitrate nitrogen.Thereby the technical scheme of two-stage ion exchange process of the strongly acidic cation exchanger-weakly-basic anion interchanger of nitrogen fertilizer plant's nitrogenous effluent of a kind of treatment of high concentration ammonia nitrogen and middle concentration nitrate nitrogen is disclosed; Cationic, anionic exchange resin after exchange is handled adopts nitric acid and ammoniacal liquor to regenerate respectively; Regeneration waste liquid is an ammonium nitrate solution, can reclaim an ammonium nitrate through carrying after dense.
A kind of treating nitrogen-containing wastewater by ion exchange of the present invention also reclaims the technology of an ammonium nitrate; It is characterized in that adopting strongly acidic cation exchanger-weakly-basic anion interchanger to connect and realize the processing of nitrogenous effluent; Accomplish the removal of ammonia nitrogen and nitrate nitrogen in the nitrogenous effluent respectively with strongly acidic cation exchanger and weakly-basic anion interchanger; Strongly acidic cationic exchange resin and weakly basic anion exchange resin after exchange is handled adopt nitric acid and ammoniacal liquor to regenerate respectively; Regeneration waste liquid is an ammonium nitrate solution; Through putting forward the technology that can reclaim an ammonium nitrate after dense, this technical process is composed in series by strongly acidic cation exchanger 2 and weakly-basic anion interchanger 4, adopts flocculation and filters pre-treatment and remove suspended solids and algae in the waste water; The organism in the waste water is removed in the charcoal absorption pre-treatment; Get into strongly acidic cation exchanger 2 successively through pretreated nitrogen fertilizer plant nitrogenous effluent 1, strongly acidic cation exchanger water outlet 3 gets into 4 water outlets afterwards of weakly-basic anion interchanger, and concrete steps are:
I. the strongly acidic cationic exchange resin in the strongly acidic cation exchanger 2 lost efficacy the back with nitric acid regeneration, and regeneration waste liquid is an an ammonium nitrate; 15～30 ℃ of operations down of water temperature, water inlet pH value is 6～8; The exchange flow velocity is 4～20m/h, nitric acid regenerated liquid concentration 10～30%, and regeneration velocity 4～10m/h, positive and negative wash speed is got 15～20m/h, and the positive and negative time of washing is got 20～30min; Strongly acidic cationic exchange resin in the strongly acidic cation exchanger 2 is that functional group is sulfonic group-SO
3The domestic and imported strongly acidic cationic exchange resin of H, described these ion exchange resin are: D001, D61,001 * 7,001 * 4, D72,742, JK008, D631, Amberjet 1200Na, Amberlite 200C Na or Amberlite IR120Na;
II. the weakly basic anion exchange resin in the weakly-basic anion interchanger 4 lost efficacy the back with ammoniacal liquor regeneration, and regeneration waste liquid also is an an ammonium nitrate; 15～30 ℃ of operations down of water temperature, water inlet pH value is 6～8; The exchange flow velocity is 4～20m/h, ammoniacal liquor regenerated liquid concentration 5～20%, and regeneration velocity 4～10m/h, positive and negative wash speed is got 15～20m/h, and the positive and negative time of washing is got 20～30min; Weakly basic anion exchange resin in the weakly-basic anion interchanger 4 is that functional group is respectively primary amino-CH
2NH
2, secondary amino group-CH
2NHCH
3Or uncle amino-CH
2N (CH
3)
2The domestic and imported weakly basic anion exchange resin, described these ion exchange resin are: D370, D301
f, D301, D380,710-A, 710-B, 301, D306, D113, D336 or Amberlite IRA96RF;
III. nitrogen fertilizer plant's nitrogenous effluent water outlet ammonia nitrogen of handling through I reaches " ammonia synthesizing industry pollution discharge standard " (GB 13458-2001); The water outlet nitrate nitrogen of handling through II reaches in the quality of groundwater standard III class tap water to the requirement (GB/T14848-93) of nitrate nitrogen; Remake boiler water-filling, cooling tower raw make up water and other water of productive use for nitrogen fertilizer plant; Realized the recycle of water; An ammonium nitrate that the while regeneration waste liquid reclaims after evaporation concentration returns production technique, has realized the utilization again of waste liquid.
A kind of treating nitrogen-containing wastewater by ion exchange of the present invention also reclaims the advantage and the purposes of the technology of an ammonium nitrate:
The present invention adopts the placed in-line ion exchange process of strongly acidic cation exchanger-weakly-basic anion interchanger to handle nitrogen fertilizer plant's nitrogenous effluent; Simpler than biological denitrification process flow process; Processing efficiency receives Influence of Temperature to receive Influence of Temperature little than biological denitrificaion simultaneously; Operational management is flexible, does not produce secondary pollution.Treat effluent ammonia nitrogen and nitrate nitrogen reach in " ammonia synthesizing industry pollution discharge standard " (GB 13458-2001) and the quality of groundwater standard III class tap water respectively to the requirement (GB/T14848-93) of nitrate nitrogen; Remake boiler water-filling, cooling tower raw make up water and other water of productive use for nitrogen fertilizer plant; Reach the recycle purpose of water, solve the outstanding problem of present short water supply.Remove the ammonia nitrogen in the waste water with strongly acidic cation exchanger; Remove the nitrate nitrogen in the waste water with the weakly-basic anion interchanger, strongly acidic cationic exchange resin and weakly basic anion exchange resin after exchange is handled adopt nitric acid and ammoniacal liquor to regenerate respectively, and regeneration waste liquid is ammonium nitrate solution; Can reclaim an ammonium nitrate through carrying after dense; Realized the utilization again of waste liquid, turned waste into wealth to have tangible environmental benefit and economic benefit.
Description of drawings
Fig. 1 strongly acidic cation exchanger-weakly-basic anion interchanger series process flow
Among the figure: the 1-water inlet
2-strongly acidic cation exchanger (employing strongly acidic cationic exchange resin)
The water outlet of 3-strongly acidic cation exchanger
4-weakly-basic anion exchange interchanger (employing weakly basic anion exchange resin)
The 5-water outlet
6-strongly acidic cation exchanger nitric acid regenerated liquid
7-weakly-basic anion exchange interchanger ammoniacal liquor regenerated liquid
8-regeneration waste liquid an ammonium nitrate
The 9-evaporation concentration reclaims an ammonium nitrate device
Embodiment:
Embodiment 1:
Ion exchange resin adopts strongly acidic cationic exchange resin D001 and weakly basic anion exchange resin D370.
Strongly acidic cation exchanger: 15 ℃ of operations down of water temperature, water inlet pH value is 6; The exchange flow velocity is 4m/h, nitric acid regenerated liquid concentration 10%, and regeneration velocity is 4m/h, and positive and negative wash speed is got 15m/h, and the positive and negative time of washing is got 20min;
The weakly-basic anion interchanger: 15 ℃ of operations down of water temperature, water inlet pH value is 6; The exchange flow velocity is 4m/h, ammoniacal liquor regenerated liquid concentration 5%, and regeneration velocity is 4m/h, and positive and negative wash speed is got 15m/h, and the positive and negative time of washing is got 20min.
Embodiment 2:
Ion exchange resin adopts strongly acidic cationic exchange resin D001 and weakly basic anion exchange resin D370.
Strongly acidic cation exchanger: 15 ℃ of operations down of water temperature, water inlet pH value is 7; The exchange flow velocity is 4m/h, nitric acid regenerated liquid concentration 20%, and regeneration velocity is 4m/h, and positive and negative wash speed is got 15m/h, and the positive and negative time of washing is got 20min;
The weakly-basic anion interchanger: 15 ℃ of operations down of water temperature, water inlet pH value is 7; The exchange flow velocity is 4m/h, ammoniacal liquor regenerated liquid concentration 15%, and regeneration velocity is 4m/h, and positive and negative wash speed is got 15m/h, and the positive and negative time of washing is got 20min.
Embodiment 3:
Ion exchange resin adopts strongly acidic cationic exchange resin D001 and weakly basic anion exchange resin D370.
Strongly acidic cation exchanger: 15 ℃ of operations down of water temperature, water inlet pH value is 8; The exchange flow velocity is 6m/h, nitric acid regenerated liquid concentration 30%, and regeneration velocity is 5m/h, and positive and negative wash speed is got 15m/h, and the positive and negative time of washing is got 20min;
The weakly-basic anion interchanger: 15 ℃ of operations down of water temperature, water inlet pH value is 8; The exchange flow velocity is 6m/h, ammoniacal liquor regenerated liquid concentration 20%, and regeneration velocity is 5m/h, and positive and negative wash speed is got 15m/h, and the positive and negative time of washing is got 20min.
Embodiment 4:
Ion exchange resin adopts strongly acidic cationic exchange resin D61 and weakly basic anion exchange resin D301
f
Strongly acidic cation exchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 6; The exchange flow velocity is 6m/h, nitric acid regenerated liquid concentration 10%, and regeneration velocity is 5m/h, and positive and negative wash speed is got 15m/h, and the positive and negative time of washing is got 25min;
The weakly-basic anion interchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 6; The exchange flow velocity is 6m/h, ammoniacal liquor regenerated liquid concentration 5%, and regeneration velocity is 5m/h, and positive and negative wash speed is got 15m/h, and the positive and negative time of washing is got 25min.
Embodiment 5:
Ion exchange resin adopts strongly acidic cationic exchange resin D61 and weakly basic anion exchange resin D301
f
Strongly acidic cation exchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 7; The exchange flow velocity is 8m/h, nitric acid regenerated liquid concentration 20%, and regeneration velocity is 6m/h, and positive and negative wash speed is got 15m/h, and the positive and negative time of washing is got 25min;
The weakly-basic anion interchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 7; The exchange flow velocity is 8m/h, ammoniacal liquor regenerated liquid concentration 15%, and regeneration velocity is 6m/h, and positive and negative wash speed is got 15m/h, and the positive and negative time of washing is got 25min.
Embodiment 6:
Ion exchange resin adopts strongly acidic cationic exchange resin D61 and weakly basic anion exchange resin D301
f
Strongly acidic cation exchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 8; The exchange flow velocity is 10m/h, nitric acid regenerated liquid concentration 30%, and regeneration velocity is 8m/h, and positive and negative wash speed is got 15m/h, and the positive and negative time of washing is got 25min;
The weakly-basic anion interchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 8; The exchange flow velocity is 10m/h, ammoniacal liquor regenerated liquid concentration 20%, and regeneration velocity is 8m/h, and positive and negative wash speed is got 15m/h, and the positive and negative time of washing is got 25min.
Embodiment 7:
Ion exchange resin adopts strongly acidic cationic exchange resin 001 * 7 and weakly basic anion exchange resin D301.
Strongly acidic cation exchanger: 30 ℃ of operations down of water temperature, water inlet pH value is 6; The exchange flow velocity is 12m/h, nitric acid regenerated liquid concentration 10%, and regeneration velocity is 8m/h, and positive and negative wash speed is got 18m/h, and the positive and negative time of washing is got 30min;
The weakly-basic anion interchanger: 30 ℃ of operations down of water temperature, water inlet pH value is 6; The exchange flow velocity is 12m/h, ammoniacal liquor regenerated liquid concentration 5%, and regeneration velocity is 8m/h, and positive and negative wash speed is got 18m/h, and the positive and negative time of washing is got 30min.
Embodiment 8:
Ion exchange resin adopts strongly acidic cationic exchange resin 001 * 7 and weakly basic anion exchange resin D301.
Strongly acidic cation exchanger: 30 ℃ of operations down of water temperature, water inlet pH value is 7; The exchange flow velocity is 12m/h, nitric acid regenerated liquid concentration 20%, and regeneration velocity is 9m/h, and positive and negative wash speed is got 18m/h, and the positive and negative time of washing is got 30min;
The weakly-basic anion interchanger: 30 ℃ of operations down of water temperature, water inlet pH value is 7; The exchange flow velocity is 12m/h, ammoniacal liquor regenerated liquid concentration 15%, and regeneration velocity is 9m/h, and positive and negative wash speed is got 18m/h, and the positive and negative time of washing is got 30min.
Embodiment 9:
Ion exchange resin adopts strongly acidic cationic exchange resin 001 * 7 and weakly basic anion exchange resin D301.
Strongly acidic cation exchanger: 30 ℃ of operations down of water temperature, water inlet pH value is 8; The exchange flow velocity is 14m/h, nitric acid regenerated liquid concentration 30%, and regeneration velocity is 9m/h, and positive and negative wash speed is got 18m/h, and the positive and negative time of washing is got 30min;
The weakly-basic anion interchanger: 30 ℃ of operations down of water temperature, water inlet pH value is 8; The exchange flow velocity is 14m/h, ammoniacal liquor regenerated liquid concentration 20%, and regeneration velocity is 9m/h, and positive and negative wash speed is got 18m/h, and the positive and negative time of washing is got 30min.
Embodiment 10:
Ion exchange resin adopts strongly acidic cationic exchange resin 001 * 4 and weakly basic anion exchange resin D380.
Strongly acidic cation exchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 6; The exchange flow velocity is 14m/h, nitric acid regenerated liquid concentration 10%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min;
The weakly-basic anion interchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 6; The exchange flow velocity is 14m/h, ammoniacal liquor regenerated liquid concentration 5%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min.
Embodiment 11:
Ion exchange resin adopts strongly acidic cationic exchange resin 001 * 4 and weakly basic anion exchange resin D380.
Strongly acidic cation exchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 7; The exchange flow velocity is 16m/h, nitric acid regenerated liquid concentration 20%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min;
The weakly-basic anion interchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 7; The exchange flow velocity is 16m/h, ammoniacal liquor regenerated liquid concentration 15%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min.
Embodiment 12:
Ion exchange resin adopts strongly acidic cationic exchange resin 001 * 4 and weakly basic anion exchange resin D380.
Strongly acidic cation exchanger: 30 ℃ of operations down of water temperature, water inlet pH value is 8; The exchange flow velocity is 16m/h, nitric acid regenerated liquid concentration 30%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min;
The weakly-basic anion interchanger: 30 ℃ of operations down of water temperature, water inlet pH value is 8; The exchange flow velocity is 16m/h, ammoniacal liquor regenerated liquid concentration 20%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min.
Embodiment 13:
Ion exchange resin adopts strongly acidic cationic exchange resin D72 and weakly basic anion exchange resin 710-A.
Strongly acidic cation exchanger: 15 ℃ of operations down of water temperature, water inlet pH value is 6; The exchange flow velocity is 18m/h, nitric acid regenerated liquid concentration 20%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min;
The weakly-basic anion interchanger: 15 ℃ of operations down of water temperature, water inlet pH value is 6; The exchange flow velocity is 18m/h, ammoniacal liquor regenerated liquid concentration 15%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min.
Embodiment 14:
Ion exchange resin adopts strongly acidic cationic exchange resin D72 and weakly basic anion exchange resin 710-A.
Strongly acidic cation exchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 7; The exchange flow velocity is 18m/h, nitric acid regenerated liquid concentration 30%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min;
The weakly-basic anion interchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 7; The exchange flow velocity is 18m/h, ammoniacal liquor regenerated liquid concentration 20%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min.
Embodiment 15:
Ion exchange resin adopts strongly acidic cationic exchange resin D72 and weakly basic anion exchange resin 710-A.
Strongly acidic cation exchanger: 30 ℃ of operations down of water temperature, water inlet pH value is 8; The exchange flow velocity is 20m/h, nitric acid regenerated liquid concentration 30%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min;
The weakly-basic anion interchanger: 30 ℃ of operations down of water temperature, water inlet pH value is 8; The exchange flow velocity is 20m/h, ammoniacal liquor regenerated liquid concentration 20%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min.
Embodiment 16:
Ion exchange resin adopts strongly acidic cationic exchange resin 742 and weakly basic anion exchange resin 710-B.
Strongly acidic cation exchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 6; The exchange flow velocity is 20m/h, nitric acid regenerated liquid concentration 30%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min;
The weakly-basic anion interchanger: 25 ℃ of operations down of water temperature, water inlet pH value is 6; The exchange flow velocity is 20m/h, ammoniacal liquor regenerated liquid concentration 20%, and regeneration velocity is 10m/h, and positive and negative wash speed is got 20m/h, and the positive and negative time of washing is got 30min.
Claims (1)
1. a treating nitrogen-containing wastewater by ion exchange and reclaim the technology of an ammonium nitrate; It is characterized in that adopting strongly acidic cation exchanger-weakly-basic anion interchanger to connect and realize the processing of nitrogenous effluent; Accomplish the removal of ammonia nitrogen and nitrate nitrogen in the nitrogenous effluent respectively with strongly acidic cation exchanger and weakly-basic anion interchanger; Strongly acidic cationic exchange resin and weakly basic anion exchange resin after exchange is handled adopt nitric acid and ammoniacal liquor to regenerate respectively; Regeneration waste liquid is an ammonium nitrate solution; Through putting forward the technology that can reclaim an ammonium nitrate after dense, this technical process is composed in series by strongly acidic cation exchanger (2) and weakly-basic anion interchanger (4), adopts flocculation and filters pre-treatment and remove suspended solids and algae in the waste water; The organism in the waste water is removed in the charcoal absorption pre-treatment; Get into strongly acidic cation exchanger (2) successively through pretreated nitrogen fertilizer plant nitrogenous effluent (1), strongly acidic cation exchanger water outlet (3) gets into weakly-basic anion interchanger (4) water outlet afterwards, and concrete steps are:
I. the strongly acidic cationic exchange resin in the strongly acidic cation exchanger (2) lost efficacy the back with nitric acid regeneration, and regeneration waste liquid is an an ammonium nitrate; 15～30 ℃ of operations down of water temperature, water inlet pH value is 6～8; The exchange flow velocity is 4～20m/h, nitric acid regenerated liquid concentration 10～30%, and regeneration velocity 4～10m/h, positive and negative wash speed is got 15～20m/h, and the positive and negative time of washing is got 20～30min; Strongly acidic cationic exchange resin in the strongly acidic cation exchanger (2) is that functional group is sulfonic group-SO
3The domestic and imported strongly acidic cationic exchange resin of H, described these ion exchange resin are: D001, D61,001 * 7,001 * 4, D72,742, JK008, D631, Amberjet 1200Na, Amberlite 200C Na or Amberlite IR120Na;
II. the weakly basic anion exchange resin in the weakly-basic anion interchanger (4) lost efficacy the back with ammoniacal liquor regeneration, and regeneration waste liquid also is an an ammonium nitrate; 15～30 ℃ of operations down of water temperature, water inlet pH value is 6～8; The exchange flow velocity is 4～20m/h, ammoniacal liquor regenerated liquid concentration 5～20%, and regeneration velocity 4～10m/h, positive and negative wash speed is got 15～20m/h, and the positive and negative time of washing is got 20～30min; Weakly basic anion exchange resin in the weakly-basic anion interchanger (4) is that functional group is respectively primary amino-CH
2NH
2, secondary amino group-CH
2NHCH
3Or uncle amino-CH
2N (CH
3)
2The domestic and imported weakly basic anion exchange resin, described these ion exchange resin are: D370, D301
f, D301, D380,710-A, 710-B, 301, D306, D113, D336 or Amberlite IRA96RF;
III. nitrogen fertilizer plant's nitrogenous effluent water outlet ammonia nitrogen of handling through I reaches " ammonia synthesizing industry pollution discharge standard " (GB 13458-2001); The water outlet nitrate nitrogen of handling through II reaches in the quality of groundwater standard III class tap water to the requirement (GB/T14848-93) of nitrate nitrogen; Remake boiler water-filling, cooling tower raw make up water and other water of productive use for nitrogen fertilizer plant; Realized the recycle of water; An ammonium nitrate that the while regeneration waste liquid reclaims after evaporation concentration returns production technique, has realized the utilization again of waste liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010223219XA CN101891316B (en) | 2010-07-07 | 2010-07-07 | Process for treating nitrogen-containing wastewater by ion exchange and reclaiming ammonium nitrate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010223219XA CN101891316B (en) | 2010-07-07 | 2010-07-07 | Process for treating nitrogen-containing wastewater by ion exchange and reclaiming ammonium nitrate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101891316A CN101891316A (en) | 2010-11-24 |
| CN101891316B true CN101891316B (en) | 2012-06-06 |
Family
ID=43100696
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010223219XA Expired - Fee Related CN101891316B (en) | 2010-07-07 | 2010-07-07 | Process for treating nitrogen-containing wastewater by ion exchange and reclaiming ammonium nitrate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101891316B (en) |
Families Citing this family (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102259039B (en) * | 2011-05-20 | 2013-01-09 | 中国水利水电科学研究院 | Method for quickly activating exchanger by using alkali and acid at different times and device used by same |
| WO2013090448A1 (en) * | 2011-12-13 | 2013-06-20 | Ecolab Usa Inc. | Integrated acid regeneration of ion exchange resins for industrial applications |
| CN102531253A (en) * | 2012-03-06 | 2012-07-04 | 中国海洋大学 | Method and process for implementing resource utilization of nitrate-polluted underground water |
| CN102874986B (en) * | 2012-10-19 | 2015-05-13 | 上海化学试剂研究所 | Treatment method for wastewater containing organic matters during production of N-phenyl maleimide |
| CN103449627B (en) * | 2013-03-15 | 2015-02-25 | 广州汉泰环境技术有限公司 | Wastewater treatment method |
| CN103318918B (en) * | 2013-05-14 | 2016-01-13 | 武汉百富环保工程有限公司 | A kind of method of purifying and recovering ammonia gas |
| CN103638994A (en) * | 2013-12-03 | 2014-03-19 | 日照鲁信金禾生化有限公司 | Method for treating anion exchange resin by using ammonia water |
| CN105314758A (en) * | 2014-07-15 | 2016-02-10 | 苏州林源自动化设备有限公司 | Novel reclaimed water processing and reusing device |
| CN104163526B (en) * | 2014-08-28 | 2016-07-06 | 清华大学 | A kind of pH that regulates strengthens the method for nitrosamine precursor in ion exchange removal water |
| CN104496100B (en) * | 2014-11-24 | 2016-07-06 | 四川泸天化股份有限公司 | The ammonia nitrogen waste water recovery and treatment method produced in nitric acid/Ammonium Nitrate |
| CN105039136B (en) * | 2015-07-10 | 2017-08-04 | 重庆大学 | Self-adapting type microalgae photobiological reaction system and method |
| CN109052742B (en) * | 2016-01-19 | 2021-08-03 | 青岛大学 | Method for decoloring printing wastewater and recovering nitrogen |
| CN106904769B (en) * | 2017-04-28 | 2022-04-12 | 南京环保产业创新中心有限公司 | Method for integrated adsorption and desorption liquid application for removing total nitrogen pollutants in wastewater |
| CN107244771B (en) * | 2017-08-15 | 2021-04-09 | 扬州大学 | Method and system for advanced treatment of nitrate and nitrite mixed wastewater |
| CN112358009B (en) * | 2020-10-19 | 2022-04-01 | 广州雅居乐固体废物处理有限公司 | Method for treating wastewater by using ion exchange column |
| CN112811502B (en) * | 2021-01-06 | 2022-06-24 | 贵州大学 | Ammonia nitrogen wastewater treatment and recovery equipment and use method |
| CN115057552B (en) * | 2022-06-23 | 2023-06-02 | 先导薄膜材料有限公司 | Concentration method of low-concentration ammonium nitrate wastewater |
| CN115353249B (en) * | 2022-10-20 | 2023-02-03 | 山东金泽水业科技有限公司 | Wastewater treatment process for recovering high-purity sodium bicarbonate by carbon dioxide solidification |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101648738A (en) * | 2008-09-16 | 2010-02-17 | 王方 | Electro-deionization method and electro-deionization device for recycling ammonia nitrogen waste water |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5450476A (en) * | 1977-09-29 | 1979-04-20 | Shin Meiwa Ind Co Ltd | Method and apparatus for removing nitric acid nitrogen |
| JPH06269776A (en) * | 1993-03-16 | 1994-09-27 | Penta Ocean Constr Co Ltd | Device for removing ammoniacal nitrogen in water |
-
2010
- 2010-07-07 CN CN201010223219XA patent/CN101891316B/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101648738A (en) * | 2008-09-16 | 2010-02-17 | 王方 | Electro-deionization method and electro-deionization device for recycling ammonia nitrogen waste water |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101891316A (en) | 2010-11-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101891316B (en) | Process for treating nitrogen-containing wastewater by ion exchange and reclaiming ammonium nitrate | |
| CN103466893B (en) | Sewage recycling comprehensive treatment system | |
| CN106242163B (en) | A kind of processing method of percolate embrane method concentrate | |
| KR20130003522A (en) | Treatment system for waste water | |
| CN104261596A (en) | Method for removing nitrate nitrogen from effluents of sewage plant with resin and method for treating resin regenerating liquid | |
| CN104176824A (en) | Ammonium nitrate wastewater biochemical treatment device and operation method thereof | |
| CN104341066B (en) | The advanced treating of a kind of industry standard discharge waste water and reclaiming system and method | |
| CN204125291U (en) | A kind of Waste Water Treatment | |
| CN101423314A (en) | High efficiency denitrification, phosphorus removal and phosphorus resource recovery composite for urban sewage | |
| CN110921832B (en) | High ammonia nitrogen wastewater treatment device and method | |
| CN112093981A (en) | Sewage treatment device and process for synchronously and efficiently removing pollutants and comprehensively recycling pollutants | |
| Eliassen et al. | Removal of nitrogen and phosphorus from waste water | |
| CN105461136B (en) | A kind of waste water of heat-engine plant integrated treatment and chemical resource recovery system and method | |
| CN214360828U (en) | Sewage treatment device for synchronously removing high-efficiency pollutants and comprehensively recycling pollutants | |
| CN104528989B (en) | A kind of high ammonia-nitrogen wastewater processes ammonia recovery system | |
| CN109626692A (en) | Contain high concentration sodium sulfate, small organic molecule method for waste water and equipment for handling | |
| CN104803511A (en) | High ammonia-nitrogen wastewater treatment device and treatment method | |
| CN205974184U (en) | Processing system of landfill leachate embrane method concentrate | |
| CN210193483U (en) | Device and system for efficiently removing total nitrogen through iron-carbon catalytic reduction | |
| CN214360829U (en) | High-efficient nitrogen recovery unit of sewage | |
| CN100395192C (en) | Treatment method of waste water arising from process of extracting ganglioside from animal brain tissue | |
| CN113480098A (en) | Separated type MAP-anaerobic membrane distillation biological reaction mariculture wastewater treatment system | |
| CN112093980B (en) | Efficient nitrogen recovery device and process for sewage | |
| CN103319027B (en) | Device and method for treatment and recovery of nitrogen and phosphorus in wastewater by utilizing seawater desalination concentrate | |
| CN205222915U (en) | Thermal power plant's waste water integrated treatment and chemical resources recovery system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120606 Termination date: 20130707 |