CN203877946U - Immersed membrane/electrode-based system for separating ammonia nitrogen in water - Google Patents
Immersed membrane/electrode-based system for separating ammonia nitrogen in water Download PDFInfo
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- CN203877946U CN203877946U CN201420172129.6U CN201420172129U CN203877946U CN 203877946 U CN203877946 U CN 203877946U CN 201420172129 U CN201420172129 U CN 201420172129U CN 203877946 U CN203877946 U CN 203877946U
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Abstract
The utility model relates to an immersed membrane/electrode-based system for separating ammonia nitrogen in water, belonging to the field of water treatment. The system comprises an ammonia nitrogen separator, a membrane component C arranged in the ammonia nitrogen separator, an electrode, a stirrer, a water outlet peristaltic pump, a pressure meter, a water inlet pump, a water inlet pipe, a water outlet pipe, a water outlet, a power supply, wires and a time relay, wherein the water outlet of the membrane component C is sequentially connected with the water outlet pipe, pressure meter and water outlet peristaltic pump, and the membrane component C is controlled by the time relay; stirrer blades are positioned on the lower part of the membrane component C; two poles of the electrode are respectively connected with the power supply through the wires, and arranged on both sides of the membrane component C; the water outlet is positioned on the upper part of the ammonia nitrogen separator; the water inlet pump is connected with the water inlet pipe; the tail end of the water inlet pipe is positioned in the ammonia nitrogen separator and is adjacent to the bottom of the ammonia nitrogen separator; and the electrode is fixed to both sides of the membrane component C, and is arranged in the reactor with the immersion depth of 20-80% and kept constant. The system solves the problem of insufficient denitrification carbon sources since organic matters are oxidized in the electrochemical treatment system, and is simple in structure.
Description
Technical field
The utility model belongs to water-treatment technology field.
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 purpose of this utility model is the problem of low C/N waste water denitrifying carbon source deficiency of processing for the nitrification/denitrification process of existing processing waste water and modification technique (as oxidation ditch, BAF etc.) thereof, 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.
A kind of based on ammonia nitrogen system in submerged membrane and electrode separation 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 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; 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.
The utility model 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 utility model 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) usining scrap iron as electrode, be 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
Ammonia nitrogen enriching apparatus schematic diagram in a kind of water that Fig. 1 provides for the utility model.
Ammonia nitrogen enriching method operation schematic diagram in a kind of water that Fig. 2 provides for the utility model.
A kind of membrane module C schematic diagram that Fig. 3 provides for the utility model.
The back up pad schematic diagram of a kind of membrane module C that Fig. 4 provides for the utility model.
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 utility model.
A kind of membrane module C8 of the present utility model (Fig. 3, Fig. 4), forms 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; 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 the cationic exchange membrane 16 that the utility model adopts 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 utility model, 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 0.05-0.25A, 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%-80%, 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: 1-8 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=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 2 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 3 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 4 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 5 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 6 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 7 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, 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=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, and flooding velocity is 9.5ml/min, and membrane module C water flow is 4.8ml/min, organism water flow is 4.7ml/min, and in electrode immersion water, the degree of depth is respectively 40% with conventional electrodes while all flooding.
Claims (1)
1. one kind based on ammonia nitrogen system in submerged membrane and electrode separation 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 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; 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420172129.6U CN203877946U (en) | 2014-04-10 | 2014-04-10 | Immersed membrane/electrode-based system for separating ammonia nitrogen in water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420172129.6U CN203877946U (en) | 2014-04-10 | 2014-04-10 | Immersed membrane/electrode-based system for separating ammonia nitrogen in water |
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| Publication Number | Publication Date |
|---|---|
| CN203877946U true CN203877946U (en) | 2014-10-15 |
Family
ID=51678470
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|---|---|---|---|
| CN201420172129.6U Expired - Fee Related CN203877946U (en) | 2014-04-10 | 2014-04-10 | Immersed membrane/electrode-based system for separating ammonia nitrogen in water |
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2014
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20211216 Address after: 100176 9th floor, block T2, Han's Square, yard 2, Ronghua South Road, Yizhuang Economic and Technological Development Zone, Daxing District, Beijing Patentee after: BEIJING BEIHUA ZHONGQING ENVIRONMENTAL ENGINEERING TECHNOLOGY CO.,LTD. Address before: 212009 room 2501, block a, twin towers, science and technology new town, No. 468, Dingmao wisdom Avenue, Zhenjiang City, Jiangsu Province Patentee before: ZHENJIANG QINGSHUI ENVIRONMENTAL SCIENCE & TECHNOLOGY Co.,Ltd. |
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| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20141015 |