CN102838246B - Method for treating ammonia-nitrogen wastewater by thermal decomposition and application of method - Google Patents
Method for treating ammonia-nitrogen wastewater by thermal decomposition and application of method Download PDFInfo
- Publication number
- CN102838246B CN102838246B CN201210331553.6A CN201210331553A CN102838246B CN 102838246 B CN102838246 B CN 102838246B CN 201210331553 A CN201210331553 A CN 201210331553A CN 102838246 B CN102838246 B CN 102838246B
- Authority
- CN
- China
- Prior art keywords
- ammonia
- ammonia nitrogen
- waste water
- tower
- combination
- 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.)
- Active
Links
Landscapes
- Physical Water Treatments (AREA)
- Removal Of Specific Substances (AREA)
Abstract
The invention relates to a method for treating ammonia-nitrogen wastewater by thermal decomposition. The method comprises the steps as follows: thermally decomposing ammonia-nitrogen pollutants in the ammonia-nitrogen wastewater into ammonia gas or nitrogen gas under the heating condition by adding auxiliary materials such as carbonate and bicarbonate based on a characteristic of low thermal stability of ammonium salts such as ammonium carbonate and ammonium bicarbonate so as to remove ammonia and nitrogen with low consumption and high efficiency, adding a small amount of alkali (such as sodium hydroxide) into the thermally decomposed ammonia-nitrogen wastewater so as to deeply remove the ammonia and the nitrogen, and discharging with standards or recycling for production after wastewater treatment; and absorbing ammonia-containing mixed steam generated after thermal decomposition so as to prepare ammonia water or ammonia salt products. Compared with a conventional ammonia-nitrogen treatment process, alkali consumption can be greatly reduced, the ammonia-nitrogen resource efficiency is high, and high-efficiency and low-consumption application value is showed in an industrial scale application of the ammonia-nitrogen wastewater.
Description
Technical field
The present invention relates to a kind of ammonia nitrogen waste water treatment method, particularly relate to a kind of method of utilizing thermal decomposition process ammonia nitrogen waste water.
Background technology
Ammonia nitrogen is one of pollutent main in China's water body, and its harm is to cause body eutrophication, causes the deterioration of ecotope.In ammonia nitrogen waste water, ammonia nitrogen pollutant is present in waste water with ammonium root, free state amino molecule form, and the treatment process of having reported mainly comprises biochemical process and physico-chemical process.Patent CN1380260A discloses a kind of method of biological process processing chemical fertilizer ammonia nitrogen waste water, by biological nitration, anti-nitration reaction, ammonia nitrogen waste water is processed to first discharge standard; Patent CN101229944A discloses a kind of method of biological process processing ammonia nitrogen waste water, adopts anaerobism-anoxic-aerobic combination art breading ammonia nitrogen waste water.
Because the ammonia nitrogen waste water of the industries such as nonferrous metallurgy, chemical industry, biological fermentation is dense, ammonia and nitrogen pollution substrate concentration reaches the waste water of 4500～80000mg/L, and inorganic salt concentration is higher, be difficult to use general biological method processing, therefore often adopt physical chemistry method to process.Patent CN102060406A discloses a kind of method of blow-off method processing ammonia nitrogen waste water, by packing tower, the ammonia-nitrogen desorption in waste water absorption is reclaimed; Patent CN101161596A discloses a kind of method of non-ferrous metals processing containing ammonia and sulfate radical waste water of processing, and has proposed carry out removing of ammonia and realize ammoniacal liquor resource utilization and reclaim with rectifying tower.
In above-mentioned physical chemistry method, generally need to use alkali that ammonia nitrogen waste water is adjusted to suitable pH, that is, ammonium radical ion is combined with hydroxide radical and forms the amino molecule of free state, then realize removing of ammonia nitrogen by physical chemistry methods such as stripping, rectifying, strippings.These methods have obtained certain effect, and part has entered industrial application, but when in the situation that ammonia nitrogen concentration is higher, pH is not high, regulate pH will consume a large amount of alkali, also can produce a large amount of precipitations of hydroxide simultaneously.
Except alkaline consumption cost, but because the content of the materials such as calcium, magnesium and heavy metal in trade effluent is higher, when deamination, wastewater pH need to be adjusted to alkalescence, more easily cause the precipitation fouling of calcium magnesium, therefore the problem that easily causes column internals to stop up in deamination equipment running process, thereby cause the frequent cleaning of stopping of needs, be difficult for long-term stable operation.
The generation of alkaline consumption cost and solid particulate has limited steady running and the widespread use of above-mentioned deamination technology, therefore develops a kind of ammonia nitrogen waste water treatment method effective, that alkaline consumption is few and has important practical significance.
Summary of the invention
For the deficiencies in the prior art, high in order to solve existing ammonia nitrogenous wastewater treatment technology alkaline consumption cost, and equipment adds for a long time alkali and moves the problems such as easy fouling, the present invention proposes a kind of method of utilizing pyrolysis to process ammonia nitrogen waste water first, efficiently, low consumption, simple to operate, be easy to industrialization, and the nitrogen that resourcebility reclaims in ammonia nitrogen waste water is prepared as ammonia/ammonium salt product.
Described method comprises: the ammonia nitrogen pollutant in ammonia nitrogen waste water is converted into heat decomposable ammonium salt, and ammonium salt described in thermal degradation, removes ammonia nitrogen in waste water, and accomplished ammonia nitrogen is processed waste water up to standard.The method of the invention is to utilize ammonium salt thermostability low, heats labile characteristic, reaches the object that removes ammonia nitrogen in waste water.
One embodiment of the invention comprise the following steps:
(1) enable to mix with ammonia nitrogen waste water with the auxiliary material of ammonia nitrogen waste water reaction generation ammonium salt;
(2) aqueous solution that heating steps (1) obtains, making ammonia nitrogen in solution and the anion binding of auxiliary material is ammonium salt generation pyrolysis, decomposes and obtains NH
3or N
2gas;
(3) in the aqueous solution obtaining in step (2), add alkali, realize degree of depth deamination, accomplished ammonia nitrogen is processed waste water up to standard.
Preferably, to obtain realize ammonia nitrogen process waste water up to standard discharge or reclaim for the production of.
Preferably, in described ammonia nitrogen waste water, ammonia nitrogen concentration is 600 ~ 100000mg/L, such as 601mg/L, 602mg/L, 603mg/L, 610mg/L, 700mg/L, 900mg/L, 1200mg/L, 1500mg/L, 2000mg/L, 5000mg/L, 10000mg/L, 120000mg/L, 150000mg/L, 20000mg/L, 50000mg/L, 80000mg/L, 90000mg/L, 95000mg/L, 98000mg/L, 99500mg/L, 99990mg/L, 99998mg/L, 99999mg/L etc.; More preferably 800 ~ 90000mg/L, is particularly preferably 1000 ~ 80000mg/L.
Described auxiliary material is the material that negatively charged ion is provided for there is the ammonium salt of thermolysis, described Optimization of Adjuvant be react with ammonia nitrogen generate can be under atmospheric pressure state ,≤400 DEG C of thermolysiss generation NH
3or N
2the acidic oxide, acid, salt of acid ammonium salt, positive ammonium salt or organic ammonium salt in a kind or the combination of at least 2 kinds, more preferably react with ammonia nitrogen generate can be under atmospheric pressure state ,≤350 DEG C of thermolysiss generation NH
3or N
2acid ammonium salt, the acidic oxide of positive ammonium salt or organic ammonium salt, acid, 1 kind or the combination of at least 2 kinds in salt, bisulfate ion more preferably can be provided, bicarbonate radical, chlorine root, nitrate radical, dichromate ion, carbonate, 1 kind or acid and/or the salt of at least 2 kinds in acetate, for example: sulfuric acid, carbonic acid, hydrochloric acid, nitric acid, dichromic acid, carbonic acid, the combination of in acetic acid a kind or at least 2 kinds and/or with the combination of its salt, bisulfate ion more preferably can be provided, bicarbonate radical, chlorine root, nitrate radical, dichromate ion, carbonate, 1 kind or the combination of at least 2 kinds in the soluble salt of acetate, further preferably sulfuric acid hydrogen sodium again, sodium bicarbonate, saleratus, sodium carbonate, salt of wormwood, 1 kind or the combination of at least 2 kinds in sal enixum, particularly preferably sodium bicarbonate and/or sodium carbonate., correspondingly, the ammonium salt generating is preferably can be under atmospheric pressure state ,≤400 DEG C of thermolysiss generate NH
3or N
2acid ammonium salt, positive ammonium salt, organic ammonium salt in a kind or the combination of at least 2 kinds, more preferably can be under atmospheric pressure state ,≤350 DEG C of thermolysiss generate NH
3or N
2acid ammonium salt, positive ammonium salt or organic ammonium salt, more preferably monoammonium sulfate, bicarbonate of ammonia, ammonium chloride, ammonium nitrate, ammonium dichromate, volatile salt, 1 kind or the combination of at least 2 kinds in ammonium acetate, for example monoammonium sulfate, the combination of bicarbonate of ammonia, ammonium chloride, the combination of ammonium nitrate, bicarbonate of ammonia, ammonium chloride, the combination of ammonium nitrate, ammonium dichromate, volatile salt, the combination of ammonium acetate, ammonium nitrate, ammonium dichromate, the combination of volatile salt, ammonium nitrate, ammonium dichromate, volatile salt, the combination of ammonium acetate, monoammonium sulfate, bicarbonate of ammonia, ammonium chloride, the combination of ammonium nitrate etc., further preferably sulfuric acid hydrogen ammonium again, bicarbonate of ammonia, 1 kind or the combination of at least 2 kinds in volatile salt, particularly preferably bicarbonate of ammonia and/or volatile salt.
The addition of described auxiliary material is more than or equal to ammonia nitrogen in waste water and reacts aequum, and one of ordinary skill in the art can determine according to the ammonia nitrogen concentration in waste water.
Preferably, described in step (1), be mixed into a kind or the combination of at least 2 kinds in stirring, line-blending, the mixing of deammoniation tower sparger, concussion, ultrasonic, jet mixing, a kind or the combination of at least 2 kinds during preferably stirring, line-blending, deammoniation tower sparger mix.
The temperature and pressure of the described pyrolysis of step (2) is determined according to the thermostability of generated ammonium salt; Preferably, the described pyrolysis of step (2) carries out in deammoniation tower; The described deammoniation tower of step (2) is the equipment that a class can realize gas-liquid separation, is preferably tower, more preferably a kind in packing tower, tray column or deamination stripping tower; Preferably, the operating pressure of the deammoniation tower described in step (2) is-0.20MPa ~ 2.0MPa that more preferably-0.18MPa ~ 1.8MPa, is particularly preferably-0.15MPa ~ 1.5MPa.
Preferably, the described type of heating of step (2) is electrically heated, heat-conducting oil heating or steam heating.
The described heating terminal temperature of step (2) is more than the heat decomposition temperature of ammonium salt of generation.One of ordinary skill in the art can determine according to the expertise of its grasp.
Preferably, the described degree of depth deamination of step (3) carries out in deammoniation tower; The described deammoniation tower of step (3) is the equipment that a class can realize gas-liquid separation, is preferably tower, more preferably a kind in packing tower, tray column or deamination stripping tower.
Preferably, the described alkali of step (3) is oxyhydroxide or basic oxide, more preferably sodium hydroxide, potassium hydroxide, calcium hydroxide, hydrated barta, barium oxide, calcium oxide, sodium oxide, 1 kind or the combination of at least 2 kinds in potassium oxide, the typical but non-limiting example of described combination comprises the combination of sodium hydroxide and potassium hydroxide, the combination of calcium hydroxide and hydrated barta, barium oxide, the combination of calcium oxide and sodium oxide, sodium hydroxide, the combination of potassium hydroxide and potassium oxide, calcium hydroxide, barium oxide, the combination of calcium oxide and sodium oxide, potassium hydroxide, calcium hydroxide, hydrated barta, the combination of barium oxide and calcium oxide, sodium hydroxide, potassium hydroxide, calcium hydroxide, the combination of sodium oxide and potassium oxide etc., be particularly preferably a kind or the combination of at least 2 kinds in sodium hydroxide, lime, calcium hydroxide.
Field prior art under the parameters of the described degree of depth deamination of step (3) is set to, for example disclosed method of patent CN102060406A, one of ordinary skill in the art can determine according to the knowledge of its grasp.
Preferably, the mixing steam that described ammonium salt thermolysis generates contains NH
3time, reclaim ammonia and be prepared as ammoniacal liquor or ammonium salt product; Preferably, described in, be recovered as and will contain NH
3mixing steam absorb and be prepared as ammoniacal liquor or ammonium salt product by absorption condensation and/or carbonization; Described carbonization absorbs instigates NH
3and CO
2in water, react, make carbonated aqueous ammonia, generate bicarbonate of ammonia.
Ammonia nitrogen waste water treatment method of the present invention can be used for sanitary wastewater and ammonia nitrogen in industrial waste water processing.
Compared with prior art, the present invention has the following advantages:
(1) the method for the invention is processed ammonia nitrogen by thermolysis process, does not need to consume alkali in thermal decomposition process, saves a large amount of alkaline consumption costs, reduces the solid particulate/sedimentary generation in deamination process simultaneously, ensures equipment continuous and steady operation;
(2) auxiliary material of the present invention is common salt, with low cost, and the negatively charged ion of auxiliary material and ammonium root knot close after heat and be decomposed into gas, does not increase the salt concn of waste water, and follow-up use film or other advanced treatment devices are given security;
(3) ammonia nitrogen pollutant of the present invention is after pyrolysis removes, the gas phase producing is generally ammonia, ammonia can be recovered as ammoniacal liquor product by absorption, or with synchronize the carbon dioxide absorption carbonization that the decomposites ammonium salt product such as be bicarbonate of ammonia, the ammonia nitrogen resource utilization efficiency of present method is high;
(4) method of thermal decomposition process ammonia nitrogen waste water of the present invention and other combination of unit operations, can be used as the technology of single processing ammonia nitrogen waste water or the pre-treating technology equipment as other degree of depth deamination technology, that the present invention invests is little, running cost is low, operational stability is high.
Brief description of the drawings
Fig. 1 is the schema of an embodiment of the method for thermal decomposition process ammonia nitrogen waste water of the present invention.
Embodiment
For ease of understanding the present invention, it is as follows that the present invention enumerates embodiment.Those skilled in the art should understand, described embodiment helps to understand the present invention, should not be considered as concrete restriction of the present invention.
Embodiment 1
Ammonia nitrogen concentration is the ammonia nitrogen waste water of 28000mg/L; In the ratio of 110g/L, auxiliary material technical grade sodium carbonate solid is added in ammonia nitrogen waste water; After stirring in hybrid reactor, by mixing solutions with being pumped in rectifying stripping tower; Rectifying stripping tower uses steam heating, and the service temperature in tower is 105 DEG C, and mixing solutions enters after rectifying stripping tower, and the carbonate in water and ammonium root knot merge generation pyrolysis, produces carbonic acid gas, ammonia G&W after reaction.
After thermolysis, ammonium root reaction decomposes in ammonia nitrogen waste water is ammonia, a small amount of ammonia is absorbed as the amino molecule of free state by waste water, in the amino molecule of this part absorption and waste water, original free state amino molecule is removed by stripping in rectifying stripping tower, water outlet ammonia nitrogen concentration≤15mg/L at the bottom of tower;
Overhead vapours is the mixing steam of ammonia, carbonic acid gas, water, and this part steam, through absorption, condensation, forms the mixing solutions of ammoniacal liquor and bicarbonate of ammonia; Mixing solutions is by absorbing carbon dioxide, and carbonization is prepared as bicarbonate of ammonia.
Embodiment 2
Ammonia nitrogen concentration is the ammonia nitrogen waste water of 600mg/L; In the ratio of 3.1g/L, by auxiliary material technical grade NaHSO
4h
2o solid adds in ammonia nitrogen waste water; After ultrasonic mixing, by mixing solutions with being pumped in packing tower; Service temperature in tower is 220 DEG C, and mixing solutions enters packing tower, and the bisulfate ion in water and ammonium root knot merge generation pyrolysis, produces ammonia G&W after reaction.
After thermolysis, ammonium root reaction decomposes in ammonia nitrogen waste water is ammonia, a small amount of ammonia is absorbed as the amino molecule of free state by waste water, in the amino molecule of this part absorption and waste water, original free state amino molecule is removed in packing tower, water outlet ammonia nitrogen concentration≤12mg/L at the bottom of tower;
Overhead vapours is the mixing steam of ammonia, water, and this part steam, through absorption, condensation, forms ammonia soln.
Embodiment 3
Ammonia nitrogen concentration is the ammonia nitrogen waste water of 100000mg/L; In the ratio of 380g/L, auxiliary material technical grade saleratus solid is added in ammonia nitrogen waste water; After stirring in hybrid reactor, by mixing solutions with being pumped in rectifying stripping tower; Rectifying stripping tower uses steam heating, and the service temperature in tower is 100 DEG C, and mixing solutions enters after rectifying stripping tower, and the bicarbonate radical in water and ammonium root knot merge generation pyrolysis, produces carbonic acid gas, ammonia G&W after reaction.
After thermolysis, ammonium root reaction decomposes in ammonia nitrogen waste water is ammonia, a small amount of ammonia is absorbed as the amino molecule of free state by waste water, in the amino molecule of this part absorption and waste water, original free state amino molecule is removed by stripping in rectifying stripping tower, water outlet ammonia nitrogen concentration≤16mg/L at the bottom of tower;
Overhead vapours is the mixing steam of ammonia, carbonic acid gas, water, and this part steam, through absorption, condensation, forms the mixing solutions of ammoniacal liquor and bicarbonate of ammonia; Mixing solutions is by absorbing carbon dioxide, and carbonization is prepared as bicarbonate of ammonia.
Embodiment 4
Ammonia nitrogen concentration is the ammonia nitrogen waste water of 90000mg/L; In the ratio of 200g/L, auxiliary material technical grade acetic acid is added in ammonia nitrogen waste water; After stirring in hybrid reactor, by mixing solutions with being pumped in rectifying stripping tower; Rectifying stripping tower uses steam heating, and the service temperature in tower is 130 DEG C, and mixing solutions enters after rectifying stripping tower, and the acetate in water and ammonium root knot merge generation pyrolysis, produces ammonia G&W after reaction.
After thermolysis, ammonium root reaction decomposes in ammonia nitrogen waste water is ammonia, a small amount of ammonia is absorbed as the amino molecule of free state by waste water, in the amino molecule of this part absorption and waste water, original free state amino molecule is removed by stripping in rectifying stripping tower, water outlet ammonia nitrogen concentration≤14mg/L at the bottom of tower;
Overhead vapours is the mixing steam of ammonia, water, and this part steam, through absorption, condensation, forms ammoniacal liquor.
Embodiment 5
Ammonia nitrogen concentration is the ammonia nitrogen waste water of 900mg/L; In the ratio of 5g/L, auxiliary material technical grade sal enixum solid is added in ammonia nitrogen waste water; Jet mixing evenly after, by mixing solutions with being pumped in rectifying stripping tower; Rectifying stripping tower uses steam heating, and the service temperature in tower is 225 DEG C, and mixing solutions enters after rectifying stripping tower, and the bisulfate ion in water and ammonium root knot merge generation pyrolysis, produces ammonia G&W after reaction.
After thermolysis, ammonium root reaction decomposes in ammonia nitrogen waste water is ammonia, a small amount of ammonia is absorbed as the amino molecule of free state by waste water, in the amino molecule of this part absorption and waste water, original free state amino molecule is removed by stripping in rectifying stripping tower, water outlet ammonia nitrogen concentration≤11mg/L at the bottom of tower;
Overhead vapours is the mixing steam of ammonia, water, and this part steam, through absorption, condensation, forms ammonia soln.
Applicant's statement, the present invention illustrates detailed process equipment and process flow process of the present invention by above-described embodiment, but the present invention is not limited to above-mentioned detailed process equipment and process flow process, do not mean that the present invention must rely on above-mentioned detailed process equipment and process flow process and could implement.Person of ordinary skill in the field should understand, any improvement in the present invention, and the selections of the equivalence replacement to the each raw material of product of the present invention and the interpolation of ancillary component, concrete mode etc., within all dropping on protection scope of the present invention and open scope.
Claims (22)
1. a method of processing ammonia nitrogen waste water, comprising: the ammonia nitrogen pollutant in ammonia nitrogen waste water is converted into heat decomposable ammonium salt, and ammonium salt described in thermal degradation, removes ammonia nitrogen in waste water, and accomplished ammonia nitrogen is processed waste water up to standard;
Described method comprises:
(1) enable to mix with ammonia nitrogen waste water with the auxiliary material of ammonia nitrogen waste water reaction generation ammonium salt;
In described ammonia nitrogen waste water, ammonia nitrogen concentration is 600～100000mg/L; Described auxiliary material be react with ammonia nitrogen generate can be under atmospheric pressure state ,≤400 DEG C of thermolysiss generate NH
3or N
2the acidic oxide, acid, salt of ammonium salt in a kind or the combination of at least 2 kinds;
(2) aqueous solution that heating steps (1) obtains, making ammonia nitrogen in solution and the anion binding of auxiliary material is ammonium salt generation pyrolysis, decomposes and obtains NH
3or N
2gas; Absorb and be prepared as ammoniacal liquor or ammonium salt product by absorption condensation and/or carbonization decomposing the mixing steam obtaining; Described pyrolysis carries out in deammoniation tower; The operating pressure of described deammoniation tower is-0.20MPa～2.0MPa;
(3) in the aqueous solution obtaining in step (2), add alkali, realize degree of depth deamination, accomplished ammonia nitrogen is processed waste water up to standard.
2. the method for claim 1, is characterized in that, to obtain realize ammonia nitrogen process waste water up to standard discharge or reclaim for the production of.
3. the method for claim 1, is characterized in that, in described ammonia nitrogen waste water, ammonia nitrogen concentration is 800～90000mg/L.
4. method as claimed in claim 3, is characterized in that, in described ammonia nitrogen waste water, ammonia nitrogen concentration is 1000～80000mg/L.
5. the method for claim 1, is characterized in that, described auxiliary material be react with ammonia nitrogen generate can be under atmospheric pressure state ,≤350 DEG C of thermolysiss generate NH
3or N
2the acidic oxide, acid, salt of ammonium salt in a kind or the combination of at least 2 kinds.
6. method as claimed in claim 5, is characterized in that, described auxiliary material is for providing a kind or the combination of at least 2 kinds in acid and/or the salt of bisulfate ion, bicarbonate radical, chlorine root, nitrate radical, dichromate ion, carbonate, acetate.
7. method as claimed in claim 6, is characterized in that, described auxiliary material is for providing a kind or the combination of at least 2 kinds in the soluble salt of bisulfate ion, bicarbonate radical, chlorine root, nitrate radical, dichromate ion, carbonate, acetate.
8. method as claimed in claim 7, is characterized in that, described auxiliary material is a kind or the combination of at least 2 kinds in sodium pyrosulfate, sodium bicarbonate, saleratus, sodium carbonate, salt of wormwood, sal enixum.
9. method as claimed in claim 8, is characterized in that, described auxiliary material is sodium bicarbonate and/or sodium carbonate.
10. method as claimed in claim 1 or 2, is characterized in that, the described hybrid mode of step (1) is a kind or the combination of at least 2 kinds in stirring, line-blending, the mixing of deammoniation tower sparger, concussion, ultrasonic, jet mixing.
11. methods as claimed in claim 10, is characterized in that, the described hybrid mode of step (1) is a kind or the combination of at least 2 kinds in stirring, line-blending, the mixing of deammoniation tower sparger.
12. the method for claim 1, is characterized in that, the described deammoniation tower of step (2) is tower.
13. methods as claimed in claim 12, is characterized in that, described deammoniation tower is a kind in packing tower, tray column or deamination stripping tower.
14. the method for claim 1, is characterized in that, the operating pressure of described deammoniation tower is-0.18MPa～1.8MPa.
15. methods as claimed in claim 14, is characterized in that, the operating pressure of described deammoniation tower is-0.15MPa～1.5MPa.
16. methods as claimed in claim 1 or 2, is characterized in that, the described type of heating of step (2) is electrically heated, heat-conducting oil heating or steam heating.
17. methods as claimed in claim 1 or 2, is characterized in that, the described degree of depth deamination of step (3) carries out in deammoniation tower.
18. methods as claimed in claim 17, is characterized in that, the described deammoniation tower of step (3) is tower.
19. methods as claimed in claim 18, is characterized in that, described deammoniation tower is a kind in packing tower, tray column or deamination stripping tower.
20. methods as claimed in claim 1 or 2, is characterized in that, the described alkali of step (3) is oxyhydroxide or basic oxide.
21. methods as claimed in claim 20, is characterized in that, described alkali is a kind or the combination of at least 2 kinds in sodium hydroxide, potassium hydroxide, calcium hydroxide, hydrated barta, barium oxide, calcium oxide, sodium oxide, potassium oxide.
22. methods as claimed in claim 21, is characterized in that, described alkali is a kind or the combination of 2 kinds in sodium hydroxide, calcium hydroxide.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210331553.6A CN102838246B (en) | 2012-09-07 | 2012-09-07 | Method for treating ammonia-nitrogen wastewater by thermal decomposition and application of method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210331553.6A CN102838246B (en) | 2012-09-07 | 2012-09-07 | Method for treating ammonia-nitrogen wastewater by thermal decomposition and application of method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102838246A CN102838246A (en) | 2012-12-26 |
| CN102838246B true CN102838246B (en) | 2014-08-20 |
Family
ID=47366014
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210331553.6A Active CN102838246B (en) | 2012-09-07 | 2012-09-07 | Method for treating ammonia-nitrogen wastewater by thermal decomposition and application of method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102838246B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP7092530B2 (en) * | 2018-03-23 | 2022-06-28 | 月島環境エンジニアリング株式会社 | Ammonia stripping treatment device for wastewater containing acidic components and ammonia and its method |
| CN113479985B (en) * | 2021-08-04 | 2022-07-29 | 中南大学 | Method for transformation deamination of ammonia nitrogen wastewater |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1623924A (en) * | 2003-12-04 | 2005-06-08 | 中国科学院生态环境研究中心 | Process for removing ammonia of treating waste water containing high contentrition ammonia |
| CN101148301A (en) * | 2007-08-21 | 2008-03-26 | 南京大学 | Method for removing ammonia and nitrogen from coking wastewater |
-
2012
- 2012-09-07 CN CN201210331553.6A patent/CN102838246B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1623924A (en) * | 2003-12-04 | 2005-06-08 | 中国科学院生态环境研究中心 | Process for removing ammonia of treating waste water containing high contentrition ammonia |
| CN101148301A (en) * | 2007-08-21 | 2008-03-26 | 南京大学 | Method for removing ammonia and nitrogen from coking wastewater |
Non-Patent Citations (2)
| Title |
|---|
| 张书军等.磷酸铵镁沉淀法脱氨机理、应用及沉淀剂循环.《环境污染治理技术与设备》.2006,第7卷(第7期),第129页第2.1节第1-2行. |
| 磷酸铵镁沉淀法脱氨机理、应用及沉淀剂循环;张书军等;《环境污染治理技术与设备》;20060731;第7卷(第7期);第129页第2.1节第1-2行 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102838246A (en) | 2012-12-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP3885039A1 (en) | Graphite-like carbon nitride doped modified microsphere catalyst, and preparation method therefor and application thereof | |
| CN105854542B (en) | A method of purification nitrogen-containing oxide tail gas | |
| WO2009024014A1 (en) | Method for removing ammonia from coking waste water | |
| WO2011082507A1 (en) | Resource utilization and harmless treatment for cyanide tailing ore pulp | |
| CN103771679B (en) | A kind of sewage sludge energy-saving dewatering and heavy metal efficient removal cooperative processing method | |
| CN102503016A (en) | Device and method for treating ammonia nitrogen wastewater, recycling ammonia and preparing ammonium sulfate | |
| CN108033592B (en) | Treatment method of high ammonia nitrogen wastewater | |
| CN110697824A (en) | Ammonia nitrogen remover and preparation method thereof | |
| CN105502765A (en) | System and method for treating desulfurization waste water and recycling resources | |
| CN108191056B (en) | Desulfurization and denitrification method for desulfurization and denitrification wastewater and ammonia nitrogen wastewater | |
| CN102838246B (en) | Method for treating ammonia-nitrogen wastewater by thermal decomposition and application of method | |
| CN104860465B (en) | Double-tower catalysis thermal-coupling reflux deamination method and deamination device thereof | |
| CN103496777A (en) | Pretreatment method of ammonia-nitrogen wastewater | |
| CN203820581U (en) | High-concentration coking desulfurization waste liquid treatment device | |
| CN102502880B (en) | Utilize the method that acid-washing waste acid produces iron series water purifier | |
| CN102351340A (en) | Recovery treatment process for molybdenum-containing acidic wastewater in the process of ammonium molybdate production | |
| CN105967396A (en) | Method for treating manganese-containing wastewater | |
| CN211004912U (en) | Wastewater treatment system | |
| US10814273B2 (en) | Method for simultaneously removing SO2 and NOX in flue gas | |
| CN103819039A (en) | High-concentration coking desulphurization waste liquid treating apparatus and method for catalytic treatment of high-concentration coking desulphurization waste liquid by using waste heat of coking | |
| CN105668755B (en) | A kind of method of the resource utilization vanadium extracting waste water production hydrocarbon denitrfying agent of ammonia- | |
| CN102489291B (en) | Method for preparing expanded graphite load nanometer bismuth vanadate photochemical catalyst | |
| CN101734813A (en) | Technology for recovering ammonium sulfate by waste acid pickle generated in process of producing cyanuric acid and equipment therefor | |
| CN104276685A (en) | Process for recovering ammonia from wastewater containing ammonia nitrogen | |
| CN113479985B (en) | Method for transformation deamination of ammonia nitrogen wastewater |
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 |