CN103922442A - Method for efficiently enriching ammonia nitrogen ions in water based on membrane and electrode - Google Patents
Method for efficiently enriching ammonia nitrogen ions in water based on membrane and electrode Download PDFInfo
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- CN103922442A CN103922442A CN201410140918.6A CN201410140918A CN103922442A CN 103922442 A CN103922442 A CN 103922442A CN 201410140918 A CN201410140918 A CN 201410140918A CN 103922442 A CN103922442 A CN 103922442A
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Abstract
The invention relates to a method for efficiently enriching ammonia nitrogen ions in water based on a membrane and an electrode, and belongs to the technical field of water treatment. The method for efficiently enriching ammonia nitrogen in wastewater is characterized by comprising the following steps: introducing raw water; connecting a membrane assembly C, setting the flow and stirring; connecting a power supply and setting the current; setting an electrode submerging form and the shape and thickness of the electrode; setting an extraction stopping time ratio and cleaning a membrane assembly; putting into running once again. By adopting the method, ammonia nitrogen in water can be enriched efficiently and organic matters can be separated in a single treatment unit, the defect of insufficient denitrification carbon source in the existing nitrification/denitrification process and a deformation process thereof (such as an oxidation ditch and a BAF (Biological Aerated Filter)) for treating low C/N wastewater and the defect of poor existing NH4<+1> separating and enriching efficiency are overcome, and the problems of oxidation of organic matters in an electrochemical treatment system and insufficient denitrification carbon source are solved. Moreover, the device structure is simple, and convenience is brought to practical operation and running.
Description
Technical field
The invention belongs to water-treatment technology field, relate in particular to a kind of method based on ammonia nitrogen ion in film and electrode efficiently concentrating water.
Background technology
C/N is the important factor in order of nitration denitrification process.In theory, in denitrification process, in stoichiometry, needed C/N is 2.86, but the C/N needing in the denitrification process system of report is much larger than 2.86, even reaches more than 11.When wastewater treatment, the nitrification/denitrification process of actual motion and modification technique thereof (as oxidation ditch process, SBR technique, BAF technique etc.), often because carbon source deficiency adds organic carbon source or develop new carbon source, thereby improve C/N, reach denitrification effect, this has increased running cost virtually, and, in electro-chemical systems, organism is not all for denitrification denitrogenation process, and the problem that this has also caused denitrifying carbon source deficiency, makes denitrification effect not good.
Contriver finds when carrying out biological denitrificaion research, if by the NH in waste water
4 +carry out respectively enrichment with separated with organism, and by the NH of enrichment
4 +be respectively used to follow-up nitrification and denitrification process with the organism of separating, can effectively utilize carbon source to realize high-efficiency biological denitrification, if yet separation and concentration efficiency is low, ammonia nitrogen can not be effectively separated with organism, denitrification denitrogenation efficiency will reduce, therefore for reaching good nitric efficiency, need to improve ammonia nitrogen concentration effect, raising ammonia nitrogen concentration effect effectively separatedly plays vital effect for nitric efficiency with organic.Contriver finds when testing for this reason, and the quality of concentration effect and water flooding per-cent (the water flooding degree of depth/height surfaces) have much relations, need further study.
At present, NH
4 +the method of separation and concentration mainly contains the methods such as absorption and ion exchange method, membrane absorption method and electrodialysis.Absorption and ion exchange method (as zeolite, ion exchange resin), can separated concentrated NH
4 +, but exist loading capacity limited, often adsorption efficiency is low.Chemical regeneration easily causes secondary pollution problems, so zeolite process denitrogenation is at present mainly for nitrogenous not high water bodys such as micro-polluted riverway water, landscape water, second pond water outlets.Electroosmose process be often used to the to raise pigs NH of waste water
4 +enrichment, the method has advantages of that less energy-consumption, efficiency are high, but cannot realize organism and NH
4 +separated.In electrochemica biological treatment process, the nascent oxygen oxidation of organic compounds often generating because of electrolysis water causes carbon source not enough, cannot meet the requirement of follow-up denitrification process to C/N simultaneously.Therefore, raising ammonia nitrogen enrichment and separating organic matters efficiency are most important for denitrification effect.
Summary of the invention
The object of the invention is the problem of processing low C/N waste water denitrifying carbon source deficiency for nitrification/denitrification process and the modification technique (as oxidation ditch, BAF etc.) thereof of existing processing waste water, and existing NH
4 +the deficiency of method for separating and concentrating and defect, and the electrolysate oxidation of organic compounds of electro-chemical systems causes carbon source to reduce problem, a kind of method based on ammonia nitrogen ion in film and electrode efficiently concentrating water is provided, the method is separation of organic substances enrichment ammonia nitrogen fully, and water outlet ammonia nitrogen is concentrated, and organism obtains separation, and then realized the enrichment of ammonia nitrogen and separating organic matters, and this device is for single treatment unit, simple in structure, easy handling operation.
Object of the present invention is achieved through the following technical solutions:
A kind of method based on ammonia nitrogen ion in film and electrode efficiently concentrating water, it is characterized in that: this device comprises uncovered apparatus for separating ammonia nitrogen, be placed on membrane module C, electrode and agitator in apparatus for separating ammonia nitrogen, water outlet peristaltic pump, tensimeter, intake pump, water inlet pipe, rising pipe, water outlet, power supply, wire, the time relay; The water outlet of membrane module C is connected successively with rising pipe, tensimeter and water outlet peristaltic pump, and is subject to the control of the time relay; Agitator blades is positioned at membrane module C bottom; The two poles of the earth of electrode are connected with power supply respectively through wire, and the two poles of the earth are placed on membrane module C both sides; Water outlet is positioned at apparatus for separating ammonia nitrogen top; Intake pump taps into water pipe, and water inlet pipe end is positioned at apparatus for separating ammonia nitrogen, and near apparatus for separating ammonia nitrogen bottom; Membrane module C forms by cationic exchange membrane, ultra-filtration membrane or microfiltration membrane with the back up pad of diversion trench and hole, and one of cationic exchange membrane, ultra-filtration membrane or microfiltration membrane are separately positioned on back up pad both sides.
Electrode described in the present invention adopts the tabular or netted ferroelectric utmost point.
The invention provides a kind of ammonia nitrogen enrichment, separating organic matters method of utilizing said apparatus, its step comprises:
(1) former water is introduced: former water, after intake pump supercharging, enters in apparatus for separating ammonia nitrogen;
(2) membrane module C connection, flow set and stirring: membrane module C is immersed in apparatus for separating ammonia nitrogen, its water outlet is connected successively with rising pipe, tensimeter and water outlet peristaltic pump, and controlled by the time relay, opens water outlet peristaltic pump, adjustment flow is 1.2-3.9ml/min, through rising pipe water outlet.Meanwhile, agitator is put into apparatus for separating ammonia nitrogen membrane module C bottom and carry out micro-stirring, prevent that oxygen from too much dissolving in oxidation of organic compounds in waste water;
(3) power supply connects and current settings: the two poles of the earth of electrode are connected with power supply respectively through wire, and by anode over against cationic exchange membrane, negative electrode is over against ultra-filtration membrane, opening power, adjusting to electric current is 0-0.25A, and remains unchanged;
(4) setting of water flooding form and electrode shape: the different electrode of tabular or netted thickness is fixed on to membrane module C both sides, and electrode is positioned in reactor with different depth of immersions such as 20%-100%, and remain unchanged;
(5) pumping time is set and membrane module C cleaning: water outlet peristaltic pump, under the control of the time relay, water outlet is that intermittent water outlet is that water outlet peristaltic pump pumping time is 10 minutes: 0-8 minute, in operating process, should make membrane module under standard atmosphere pressure, be 15kpa, when tensimeter indication numerical value surpasses 15kpa, need clean membrane module C.
After being cleaned, membrane module C can again put into operation.Whole process is flowed out from rising pipe by the ammonia nitrogen of enrichment, and separated organism flows out from water outlet, and then it is separated to have realized ammonia nitrogen.
A method based on ammonia nitrogen ion in film and electrode efficiently concentrating water, its principle is:
(1) membrane module forms and working mechanism:
Membrane module C forms by cationic exchange membrane, ultra-filtration membrane with the back up pad of diversion trench and hole, ultra-filtration membrane in membrane module C can allow water molecules to see through to enter between ultra-filtration membrane and back up pad, the water molecules seeing through enters between back up pad and cationic exchange membrane by the hole of back up pad, make cationic exchange membrane both sides be the aqueous solution, because cationic exchange membrane has positively charged ion (as NH
4 +) selection perviousness, NH
4 +the quantity that enters into membrane module C within the unit time has determined concentration effect.
(2) under electric field action, improve ammonia nitrogen enrichment:
NH in waste water
4 +under the effect of electrical forces, to movable cathode, by cationic exchange membrane, enter and in membrane module, obtain enrichment method, and the quality of concentration effect depends on that the unit time enters NH in membrane module
4 +quantity, strength of electric field is larger, enters the NH of membrane module in the unit time
4 +quantity is more, and concentration effect is better, and has direct relation in the form of flooding and the strength of electric field of same current lower electrode, and this is because when electrode surfaces, and it is large that the resistance of whole electrode becomes, and makes strength of electric field become large, NH
4 +the quantity that enters into membrane module within the unit time increases, NH
4 +concentration effect strengthens.
(3) reduce organic oxidation, realize separating organic matters:
As everyone knows, the reaction of electrode materials Different electrodes is different.When adopting inert material, at anode, will produce the nascent oxygen that a large amount of oxidation capacities are strong by brine electrolysis, by oxidation operation, cause denitrifying carbon source not enough.The present invention is usingd iron as anode, and principal reaction process is as follows:
Anodic reaction is: Fe-2e → Fe
2+
Water molecules ionization: H
2o → OH
-+ H
+
Cathodic reaction: 2H
++ 2e → H
2↑
The Fe that in solution, OH-and anode produce
2+reaction: Fe
2++ 2OH → Fe (OH)
2,
Newly-generated Fe (OH)
2easily oxidized, generate Fe (OH)
3, and Fe (OH)
3can increase the settling property of mud, the Fe that anode produces simultaneously
2+to band, color base group has good decolorizing effect.As can be seen here, using iron during as anode, organism also has neither part nor lot in reaction and is consumed, and can maintain a higher concentration, for follow-up denitrification process has guaranteed carbon source, and then realizes separating organic matters.
The present invention compared with prior art, has the following advantages and outstanding effect:
(1) improve NH
4 +separation and concentration effect, focuses on the effect of electrode
The problem low for C/N in sanitary sewage, carbon source is not enough, before organism is not by biological decomposition, by organism and NH
4 +separated and by NH
4 +enrichment, for the competition of follow-up nitrifying process elimination heterotrophic microorganism and Autotrophic nitrification bacterium, for denitrification process provides effective carbon source, seems particularly important so improve ammonia nitrogen concentration effect.The present invention is in order to strengthen separation and concentration effect, the impact of the form of flooding of having studied electrode on concentration effect, the form of flooding of electrode is for improving the impact of ammonia nitrogen concentration effect significantly, ammonia nitrogen concentration effect can be up to more than 100%, and when comparing conventional electrodes and all flooding, ammonia nitrogen accumulation rate has improved 50% left and right.And the electrode part that surfaces, water-immersed electrode area diminishes, and has saved electrode materials.
(2) using iron plate or iron net as anode, in galvanization, on anode, iron plate loses electronics becomes ferrous ion and dissolves in water: Fe-2e → Fe
2+, and under the conditions such as stirring, finally generate Fe (OH)
3, and the Fe (OH) generating
3can improve the settling property of mud, in this process, the organism in apparatus for separating ammonia nitrogen can be not oxidized, for follow-up denitrification process provides effective carbon source, realized ammonia nitrogen with organic effective separated.
(3) this invention is usingd scrap iron as electrode, is applied to municipal wastewater and other low C/N wastewater treatments, is a kind of practicability and effectiveness and economy wastewater treatment means easily.For following providing convenience property of practical engineering application and the use value.
(4) whole apparatus structure is simple, is convenient to actually operating operation.
Accompanying drawing explanation
Fig. 1 is ammonia nitrogen enriching apparatus schematic diagram in a kind of water provided by the invention.
Fig. 2 is ammonia nitrogen enriching method operation schematic diagram in a kind of water provided by the invention.
Fig. 3 is a kind of membrane module C schematic diagram provided by the invention.
Fig. 4 is the back up pad schematic diagram of a kind of membrane module C provided by the invention.
Fig. 5 is ammonia nitrogen accumulation rate schematic diagram after ammonia nitrogen enriching apparatus.
In figure: 1-intake pump 2-water inlet pipe 3-apparatus for separating ammonia nitrogen 4-power supply 5-wire 6-electrode 7-agitator 8-membrane module C9-tensimeter 10-water outlet peristaltic pump 11-time relay 12-rising pipe 13-water outlet 14-back up pad 15-ultra-filtration membrane or microfiltration membrane 16-cationic exchange membrane 17-membrane module C water outlet 18-diversion trench 19-hole
Embodiment
Below in conjunction with accompanying drawing 1,2,3,4 and embodiment, explain detailedly, further to understand the present invention.
A kind of membrane module C8(Fig. 3 of the present invention, Fig. 4), by cationic exchange membrane 16, ultra-filtration membrane or microfiltration membrane 15 with the back up pad 14 of diversion trench 18 and hole 19, form; Cationic exchange membrane 16 and ultra-filtration membrane or microfiltration membrane 15 are separately fixed at the two sides of back up pad 14.
In order to make experiment effect reach better, the cationic exchange membrane that cationic exchange membrane 16 of the present invention is CMS for the model that provides from Japanese astom, ultra-filtration membrane 15 for the aperture providing from the auspicious clean spy in Nanjing be that 0.1 μ m, membrane flux are 18.75-20.83L/m
2.h ultra-filtration membrane.
In a kind of water provided by the present invention, ammonia nitrogen enriching apparatus (Fig. 1) comprises uncovered apparatus for separating ammonia nitrogen 3, be placed on membrane module C8, agitator 7 and electrode 6 in apparatus for separating ammonia nitrogen 3, intake pump 1, water inlet pipe 2, power supply 4, wire 5, tensimeter 9, water outlet peristaltic pump 10, the time relay 11, rising pipe 12, water outlet 13; The water outlet of membrane module C8 is connected successively with rising pipe 12, tensimeter 9 and water outlet peristaltic pump 10, and is subject to the control of the time relay 11; Agitator blades is positioned at membrane module C8 bottom; The two poles of the earth of electrode 6 are connected with power supply 4 respectively through wire 5, adopt anode over against cationic exchange membrane 16, and negative electrode is over against ultra-filtration membrane 15; Water outlet 13 is positioned at apparatus for separating ammonia nitrogen 3 tops; Intake pump 1 taps into water pipe 2, and water inlet pipe end is positioned at apparatus for separating ammonia nitrogen 3, and near apparatus for separating ammonia nitrogen 3 bottoms.
Fig. 2 has represented ammonia nitrogen enriching apparatus running status in water, and concrete steps are:
(1) former water is introduced: former water, after intake pump 1 supercharging, enters in apparatus for separating ammonia nitrogen 3 through water inlet pipe 2.
(2) membrane module C connection, flow set and stirring: membrane module C8 is immersed in apparatus for separating ammonia nitrogen 3, its water outlet 17 is connected successively with rising pipe 12, tensimeter 9 and water outlet peristaltic pump 10, and be subject to the control of the time relay 11, open water outlet peristaltic pump 10, adjust discharge and be 1.45-4.15ml/min and constantly adjust rotating speed that to maintain water flow constant, through rising pipe 12 water outlets.Meanwhile, agitator 7 is put into apparatus for separating ammonia nitrogen 3 operation, its agitating vane is positioned at membrane module C8 bottom.Due to the stirring of agitator 7, the concentration of ammonia nitrogen in reactor is uniform substantially.
(3) power supply connects and current settings: the two poles of the earth of electrode 6 are connected with power supply 4 respectively through wire 5, and by anode over against cationic exchange membrane 16, negative electrode is over against ultra-filtration membrane 15, opening power 4, adjustment electric current is 0.0-0.25A, and remains unchanged.Ultra-filtration membrane 15 in membrane module C8 can allow water molecules to see through to enter between ultra-filtration membrane 15 and back up pad 14, the water molecules seeing through enters between back up pad 14 and cationic exchange membrane 16 by the hole 19 of back up pad 14, make cationic exchange membrane 16 both sides be the aqueous solution, because cationic exchange membrane 16 has (as NH
4 +) select perviousness, under impressed current effect, NH in the unit time
4 +the quantity that enters membrane module C8 increases, and enters the ion of membrane module C8, can enter into rapidly the water seeing through from ultra-filtration membrane 15, forms the ammonia nitrogen concentrated solution of high density, and then makes ammonia nitrogen obtain enrichment; Meanwhile, because two kinds of membrane pore size are very little, organism is difficult to enter in membrane module C8, and then has realized separating organic matters.
(4) setting of water flooding form and electrode shape: tabular or mesh electrode 6 are fixed on to membrane module C8 both sides, and electrode is positioned in reactor with different depth of immersions such as 20%-100%, and remain unchanged;
(5) pumping time is set and membrane module C cleaning: water outlet peristaltic pump 10, under the control of the time relay 11, water outlet is that intermittently sexual type water outlet is that water outlet peristaltic pump pumping time is 10 minutes: 0-8 minute, in operating process, should make membrane module under standard atmosphere pressure, be 15kpa, when tensimeter indication numerical value surpasses 15kpa, need clean membrane module C.
(6) again put into operation: after membrane module C8 is cleaned, can again put into operation.Whole process is flowed out from rising pipe 12 by the ammonia nitrogen of enrichment, and separation of organic substances flows out from water outlet 13, and then has realized ammonia nitrogen enrichment with organic separated.
Result:
1) little experiment:
Example 1 is when former water is general sanitary sewage, and its main water-quality guideline is: COD=467.3mg/L, NH
4 +-N=64.63mg/L; Operational condition is: water outlet peristaltic pump pumping time is 10 minutes: 5 minutes, flooding velocity is 9.5ml/min, membrane module C water flow is 4.8ml/min, in electrode immersion water, the degree of depth is 100%, when electric current is 0.2A, after ammonia nitrogen enriching apparatus, the leading indicator of film water outlet can reach: COD=70.73mg/L, NH
4 +-N=65mg/L, the separation rate that ammonia nitrogen accumulation rate is 0.57%, COD is 81.72%.
Example 2 is when former water is general sanitary sewage, and its main water-quality guideline is: COD=468.8mg/L, NH
4 +-N=57.73mg/L; Operational condition is: water outlet peristaltic pump pumping time is 10 minutes: 5 minutes, flooding velocity is 9.5ml/min, membrane module C water flow is 4.8ml/min, in electrode immersion water, the degree of depth is 80%, when electric current is 0.2A, after ammonia nitrogen enriching apparatus, the leading indicator of film water outlet can reach: COD=199.4mg/L, NH
4 +-N=78.95mg/L, the separation rate that ammonia nitrogen accumulation rate is 36.77%, COD is 56.25%.
Example 3 is when former water is general sanitary sewage, and its main water-quality guideline is: COD=465mg/L, NH
4 +-N=57mg/L; Operational condition is: water outlet peristaltic pump pumping time is 10 minutes: 5 minutes, flooding velocity is 9.5ml/min, membrane module C water flow is 4.8ml/min, in electrode immersion water, the degree of depth is 60%, when electric current is 0.2A, after ammonia nitrogen enriching apparatus, the leading indicator of film water outlet can reach: COD=200.7mg/L, NH
4 +-N=81.14mg/L, the separation rate that ammonia nitrogen accumulation rate is 42.35%, COD is 56.25%.
Example 4 is when former water is general sanitary sewage, and its main water-quality guideline is: COD=476.3mg/L, NH
4 +-N=60.88mg/L; Operational condition is: water outlet peristaltic pump pumping time is 10 minutes: 5 minutes, flooding velocity is 9.5ml/min, membrane module C water flow is 4.8ml/min, in electrode immersion water, the degree of depth is 40%, when electric current is 0.2A, after ammonia nitrogen enriching apparatus, the leading indicator of film water outlet can reach: COD=222.7mg/L, NH
4 +-N=89.87mg/L, the separation rate that ammonia nitrogen accumulation rate is 47.62%, COD is 53.25%.
Example 5 is when former water is general sanitary sewage, and its main water-quality guideline is: COD=467.25mg/L, NH
4 +-N=56.39mg/L; Operational condition is: water outlet peristaltic pump pumping time is 10 minutes: 5 minutes, flooding velocity is 9.5ml/min, membrane module C water flow is 4.8ml/min, in electrode immersion water, the degree of depth is 20%, when electric current is 0.2A, after ammonia nitrogen enriching apparatus, the leading indicator of film water outlet can reach: COD=206.2mg/L, NH
4 +-N=98.36mg/L, the separation rate that ammonia nitrogen accumulation rate is 74.43%, COD is 55.87%.
Example 6 is when former water is general sanitary sewage, and its main water-quality guideline is: COD=456mg/L, NH
4 +-N=72.52mg/L; Operational condition is: adopt iron net as electrode, (iron network parameters: the wide 22.5cm thickness of long 45.5cm 1mm) water outlet peristaltic pump pumping time is 10 minutes: 5 minutes, flooding velocity is 9.5ml/min, membrane module C water flow is 4.8ml/min, in electrode immersion water, the degree of depth is 60%, when electric current is 0.2A, after ammonia nitrogen enriching apparatus, the leading indicator of film water outlet can reach: COD=120.4mg/L, NH
4 +-N=103.58mg/L, the separation rate that ammonia nitrogen accumulation rate is 47.62%, COD is 53.25%.
Example 7 is when former water is general sanitary sewage, and its main water-quality guideline is: COD=402.5mg/L, NH
4 +-N=64.15mg/L; Operational condition is: adopt iron plate as electrode, (iron plate parameter: the wide 22.5cm thickness of long 45.5cm 2mm) water outlet peristaltic pump pumping time is 10 minutes: 5 minutes, flooding velocity is 9.5ml/min, membrane module C water flow is 4.8ml/min, in electrode immersion water, the degree of depth is 60%, when electric current is 0.2A, after ammonia nitrogen enriching apparatus, the leading indicator of film water outlet can reach: COD=117.4mg/L, NH
4 +-N=102.73mg/L, the separation rate that ammonia nitrogen accumulation rate is 60.13%, COD is 70.84%.
Example 8 is when former water is general sanitary sewage, and its main water-quality guideline is: COD=416.5mg/L, NH
4 +-N=101.39mg/L; Operational condition is: adopt iron plate as electrode, (iron plate parameter: the wide 22.5cm thickness of long 45.5cm 1mm) water outlet peristaltic pump pumping time is 10 minutes: 5 minutes, flooding velocity is 9.5ml/min, membrane module C water flow is 4.8ml/min, in electrode immersion water, the degree of depth is 60%, when electric current is 0.2A, after ammonia nitrogen enriching apparatus, the leading indicator of film water outlet can reach: COD=145.25mg/L, NH
4 +-N=101.39mg/L, the separation rate that ammonia nitrogen accumulation rate is 42.90%, COD is 65.1%.
2) continuous service test result:
Example 1 is when former water is general sanitary sewage, and its main water-quality guideline is: COD=346.1mg/L, NH
4 +-N=37.20mg/L; Operational condition is: water outlet peristaltic pump is taken out and stopped than being 10:5, and flooding velocity is 9.5ml/min, and membrane module C water flow is 4.8ml/min, in electrode immersion water, the degree of depth is 40%, when electric current is 0.2A, after ammonia nitrogen enriching apparatus, the leading indicator of film water outlet can reach: COD=189.6mg/L, NH
4 +-N=78.45mg/L, the rejection that ammonia nitrogen accumulation rate is 110.87%, COD is 45.22%.
Example 2 is when former water is general sanitary sewage, and its main water-quality guideline is: COD=344.6mg/L, NH
4 +-N=32.47mg/L; Operational condition is: water outlet peristaltic pump is taken out and stopped than being 10:5, flooding velocity is 9.5ml/min, membrane module C water flow is 4.8ml/min, organism water flow is 4.7ml/min, in electrode immersion water, the degree of depth is 40%, when electric current is 0.2A, after ammonia nitrogen enriching apparatus, the leading indicator of film water outlet can reach: COD=133.9mg/L, NH
4 +-N=73.45mg/L, the rejection that ammonia nitrogen accumulation rate is 126.20%, COD is 61.14%.
Example 3 is when former water is general sanitary sewage, and its main water-quality guideline average is to move continuously 13 days: COD=350mg/L, NH
4 +-N=50mg/L; Operational condition is: water outlet peristaltic pump is taken out and stopped than being 10:5, electric current is 0.2A, flooding velocity is 9.5ml/min, membrane module C water flow is 4.8ml/min, organism water flow is 4.7ml/min, in electrode immersion water, the degree of depth is respectively 40% with conventional electrodes while all flooding, and after ammonia nitrogen enriching apparatus, ammonia nitrogen accumulation rate respectively as shown in Figure 5.
Claims (1)
1. the method based on ammonia nitrogen ion in film and electrode efficiently concentrating water, apply as lower device: this device comprises uncovered apparatus for separating ammonia nitrogen, is placed on membrane module C, electrode and agitator in apparatus for separating ammonia nitrogen, water outlet peristaltic pump, tensimeter, intake pump, water inlet pipe, rising pipe, water outlet, power supply, wire, the time relay; The water outlet of membrane module C is connected successively with rising pipe, tensimeter and water outlet peristaltic pump, and is subject to the control of the time relay; Agitator blades is positioned at membrane module C bottom; The two poles of the earth of electrode are connected with power supply respectively through wire, and the two poles of the earth are placed on membrane module C both sides; Water outlet is positioned at apparatus for separating ammonia nitrogen top; Intake pump taps into water pipe, and water inlet pipe end is positioned at apparatus for separating ammonia nitrogen, and near apparatus for separating ammonia nitrogen bottom; Membrane module C by cationic exchange membrane, ultra-filtration membrane or microfiltration membrane and with the back up pad of diversion trench and hole form, one of cationic exchange membrane, ultra-filtration membrane or microfiltration membrane be separately positioned on back up pad both sides;
The method comprises the steps:
(1) former water is introduced: former water, after intake pump supercharging, enters in apparatus for separating ammonia nitrogen;
(2) membrane module C connection, flow set and stirring: membrane module C is immersed in apparatus for separating ammonia nitrogen, its water outlet is connected successively with rising pipe, tensimeter and water outlet peristaltic pump, and be subject to the control of the time relay, open water outlet peristaltic pump, adjustment flow is 1.2-3.9ml/min, through rising pipe water outlet; Meanwhile, agitator is put into apparatus for separating ammonia nitrogen operation, its agitating vane is positioned at membrane module C bottom and stirs;
(3) power supply connects and current settings: the two poles of the earth of electrode are connected with power supply respectively through wire, and by anode over against cationic exchange membrane, negative electrode is over against ultra-filtration membrane, opening power, adjusting to electric current is 0.05-0.25A, and remains unchanged;
(4) setting of water flooding form: electrode is fixed on to membrane module C both sides, and electrode be take to depth of immersion in 20%-80% is positioned over reactor, and remain unchanged;
(5) pumping time is set and membrane module C cleaning: water outlet peristaltic pump, under the control of the time relay, water outlet is that intermittent water outlet is that water outlet peristaltic pump pumping time is 10 minutes: 1-8 minute, in operational process, make membrane module in service pressure, lower than 15kpa, when tensimeter indication numerical value surpasses 15kpa, need clean membrane module C.
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| CN107162190A (en) * | 2017-06-16 | 2017-09-15 | 北京工业大学 | A kind of IEM UF nitrogen enrichment Prepositive denitrification nitrification denitrogenation method and device |
| CN111892224A (en) * | 2020-08-07 | 2020-11-06 | 重庆大学 | Ammonia nitrogen wastewater treatment system and method based on south of road dialysis and osmotic distillation coupling |
| CN112161969A (en) * | 2020-10-23 | 2021-01-01 | 中国科学院合肥物质科学研究院 | Method and system for detecting content of metal ions in different forms |
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| CN111892224A (en) * | 2020-08-07 | 2020-11-06 | 重庆大学 | Ammonia nitrogen wastewater treatment system and method based on south of road dialysis and osmotic distillation coupling |
| CN111892224B (en) * | 2020-08-07 | 2023-02-07 | 重庆大学 | Ammonia-nitrogen wastewater treatment system and method based on south crossing dialysis and osmotic distillation coupling |
| CN112161969A (en) * | 2020-10-23 | 2021-01-01 | 中国科学院合肥物质科学研究院 | Method and system for detecting content of metal ions in different forms |
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