CN105621536A - Film assembly and method for removing ammonia and nitrogen in garbage leachate - Google Patents
Film assembly and method for removing ammonia and nitrogen in garbage leachate Download PDFInfo
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- CN105621536A CN105621536A CN201610085521.0A CN201610085521A CN105621536A CN 105621536 A CN105621536 A CN 105621536A CN 201610085521 A CN201610085521 A CN 201610085521A CN 105621536 A CN105621536 A CN 105621536A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/02—Hollow fibre modules
- B01D63/025—Bobbin units
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/21—Specific headers, end caps
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
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- Hydrology & Water Resources (AREA)
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Abstract
The invention provides a film assembly and a method for removing ammonia and nitrogen in garbage leachate. By the aid of the film assembly and the method, shortcomings that the contents of ammonia and nitrogen in treated garbage outlet water exceed standards and the treatment cost is high after the quantities of the ammonia and the nitrogen are increased if garbage leachate is treated in the prior art can be overcome. The film assembly comprises a shell, a first end cover and a second end cover. The first end cover and the second end cover are respectively arranged at two ends of the shell, hollow film wires are arranged in the shell along the length direction of the shell and are arrayed at intervals, an acid absorption liquid outlet is formed in the second end cover, and an acid absorption liquid inlet is formed in the first end cover. The film assembly and the method have the advantages that the garbage leachate can be treated by the aid of the film assembly, and the garbage leachate treatment capacity can be improved as compared with film assemblies with identical specifications; liquid with different degrees of ammonia and nitrogen concentration can be obtained according to requirements, the high-concentration ammonia and the high-concentration nitrogen can be treated, the film assembly and the method are high in treatment efficiency, and precision requirements on pretreatment processes can be lowered.
Description
Technical field
The present invention relates to the processing method of ammonia nitrogen in percolate and device used
Background technology
At present, the process of ammonia nitrogen in percolate is generally adopted with the following method: blow-off method, nitrification and denitrification method, adopt above two method to process percolate and all there is bigger limitation, such as blow-off method not only inefficiency and easily cause local pollution or secondary pollution so that subsequent process environment protection burden weight; Nitration denitrification method reaches in 4000mg/L situation in ammonia nitrogen value will normal operation, therefore, the numerical value of influent ammonia nitrogen had restriction so that the requirement of garbage disposal liquid is high, need to compare strict pretreatment, therefore overall treatment efficiency relatively low under. Major part refuse landfill at present and garbage burning factory are in order to consider that investment and operating cost have employed biochemistry and add physico-chemical process. But adopt the ammonia nitrogen that biochemistry adds in physico-chemical process process percolate still to have following deficiency: annual May raises with temperature, diafiltration liquid measure increases sharply, ammonia-nitrogen content also improves rapidly, general ammonia-nitrogen content is all up to 3000-3500mg/L, have even up to more than 4000mg/L, the diafiltration liquid measure sharply increased and the ammonia-nitrogen content improved rapidly, ammonia-nitrogen content in refuse disposal system water outlet is exceeded standard, even makes refuse disposal system be subject to trauma. Such as, certain new district, city the first garbage burning factory early or mid May is analyzed result and shows influent ammonia nitrogen 3800--4100mg/L (originally design influent ammonia nitrogen 1300-1500mg/L), ammonia nitrogen in water outlet is about 80-200mg/L from the original content ammonia-nitrogen content that rises to up to standard so that in water outlet, ammonia-nitrogen content is defective. Owing in percolate, ammonia-nitrogen content raises, pH value in percolate is also raised accordingly, cause DTRO membranous system that from neutral 91-95%, the rejection of ammonia nitrogen is dropped to alkaline 85-90%, add the quantity of dense water in order to keep water outlet ammonia nitrogen up to standard, cause a ton water running expense grand mean cost and be increased sharply. Such as: process waste liquid 100 tons for every day, under normal circumstances, dense water is 15-20 ton, and after ammonia nitrogen raises, dense water becomes 25-30 ton, and the handling being equivalent to add 10 tons is used; Adopting above-mentioned existing ammonia nitrogen processing method, owing to ammonia nitrogen level content height is defective, environment still can be caused secondary pollution by the nitrogen contained in the process water of discharge.
For these reasons, industry is seeking a kind of to process the processing method of ammonia nitrogen in percolate always.
In order to solve above-mentioned technical problem, application number is 201110407074.3, name is called " a kind of garbage leachate processing technique based on novel ammonia nitrogen removal technology ", application publication number is the processing method that the Chinese invention patent application of CN102951745 discloses a kind of percolate, it utilizes the gas-water separation membranous system of hollow-fibre membrane or Flat Membrane composition that percolate is processed, its percolate enters into hollow fiber cavity and carries out ammonia nitrogen removal, it is sent to the doughnut outside absorption ammonia nitrogen of gas-water separation membrane module with the acid liquid that absorbs simultaneously, when adopting this method process ammonia nitrogen, owing to percolate flows in hollow-fibre membrane inner chamber, therefore the required precision of percolate is high, otherwise very easily block hollow-fibre membrane inner chamber, which not only improves the cost of garbage disposal, and reduce the efficiency of garbage disposal liquid, what have even cannot normal operation, especially when in percolate after temperature raises, ammonia nitrogen amount improves, the process of rubbish is not often reached the requirement of GB GB16889-2008.
Summary of the invention
The present invention is directed to when adopting prior art process percolate when after ammonia nitrogen amount increase in percolate, in the rubbish water outlet processed, ammonia-nitrogen content exceeds standard and processes deficiency costly, it is provided that a kind of percolate ammonia nitrogen removal device and percolate ammonia nitrogen removal method.
In order to solve above-mentioned technical problem, technical scheme provided by the invention is as follows:
A kind of percolate ammonia nitrogen removal membrane module, including housing, housing two ends are respectively arranged with end cap one and end cap two, it is provided with the film silk of hollow along the length direction of housing in housing, it is spaced between film silk, the outer surface at film silk two ends seals and is fixed in housing, end cap two is provided with acid and absorbs liquid outlet, end cap one is provided with acid and absorbs liquid import, film silk inner chamber two ends absorb liquid outlet respectively with acid and acid absorbs liquid entrance and connects, what be positioned at sealing place with housing of the film silk in the upper end of housing is arranged below waste liquid import, what be positioned at housing sealing place with film silk in the lower end of housing is provided above waste liquid outlet, the inner chamber between film silk and sealing place at two ends in housing respectively with waste liquid import and waste liquid outlet, on film silk wall, the length direction along film silk is provided with multiple weep hole, film silk inner chamber is connected with housing cavity by weep hole,
The waste liquid port of export is provided with current anti-deflection device and controls the pressure of the percolate of flowing in housing;
Described current anti-deflection device is water flow pressure detection and adjustment device;
Described current anti-deflection device is linked in sequence by electrodynamic valve, pressure transducer and electric control valve and forms, and electric control valve electrically connects with pressure transducer, electrodynamic valve one end be connected with waste liquid outlet;
The two ends of described film silk are sealed by glue and are fixed in housing;
Described weep hole is elongated hole, and its length direction is arranged along the length direction of film silk, and described weep hole is provided with turned-out flange;
Each film silk is vertically uniformly arranged in housing.
Another object of the present invention is, a kind of percolate ammonia nitrogen removal method is provided, percolate is processed by employing ammonia nitrogen removal membrane module, and after acid absorption liquid enters into intracavity in film silk by sour absorption liquid import, in film silk, intracavity flows and absorbs ammonia nitrogen, warp is exported outflow by acid absorption liquid; Percolate enters in housing via waste liquid import, flows between film silk after ammonia nitrogen is deviate from through being flowed out by percolate outlet.
Percolate ammonia nitrogen removal method, adopts aforesaid percolate ammonia nitrogen removal membrane module that percolate is processed;
Percolate pH value is 8-11, acid preferably absorbs the pH value of liquid less than or equal to 2, the pressure of percolate absorbs the pressure of liquid not higher than acid and acid can be made to absorb liquid and percolate flowing, acid absorbs flow quantity 210-350L/h, garbage filter flow quantity 250-350L/h, percolate and acid absorb the temperature of liquid be 10-50 DEG C, the TDS value of percolate is less than or equal to 35%;
The force value of percolate be 0.01-0.15MPa, acid absorb liquid force value be 0.02-0.15MPa.
Percolate is carried out ammonia nitrogen removal by the method adopting the present invention, owing to percolate flows outside film silk, and absorb the acid solution of ammonia nitrogen at film silk Bottomhole pressure, therefore NH_3-N treating ability improves, will not be detained because of the blocking of waste liquid, percolate flowing velocity is fast, amount of flow is big, hence in so that the ability that the membrane module of same specification processes percolate improves, not by the restriction of ammonia-nitrogen content in percolate, and the liquid of different ammonia nitrogen concentration can be obtained as requested, it is adaptable to the demand of the following process such as chemical fertilizer making. When the film silk assembly of employing present configuration and processing method carry out percolate process, ammonia nitrogen in high density can being processed, and treatment effeciency is high, when influent ammonia nitrogen index is beyond 50%, effluent index recovers normal in 5 minutes.
When adopting the inventive method and film silk assembly to process, membrane module is only needed to process, take up an area less, reduced investment, energy-saving effect obvious, than existing blow-off method, nitrification and denitrification method process the method for waste liquid ammonia nitrogen few take up an area minimizing more than half, economic operating cost 25--30%; The requirement system work low 0.02--0.1MPa of operating pressure, pretreatment and technological process are required simple, if water inlet filter device therefor precision 50 microns, percolate can be made to process be smoothed out, will not block, need the technology requirement of Filter Precision 5 microns well below prior art, therefore reduce the required precision of pretreating process, pretreating process is made easily to reach standard, of many uses. When ammonia nitrogen raises in waste liquid, can pass through to increase the amount of acid, make infiltration rate accelerate, increase alkali number, make free ammonia escape velocity accelerate. Whole treatment effeciency improves nearly one times.
Just the ammonia nitrogen in garbage disposal liquid can be made easily up to standard as long as the treatment plant for not reaching 2008 new standards by biochemical system process garbage filter ammonia nitrogen adds one-level film unit, little transformation is adopted to put into the ammonia nitrogen discharge capacity that just can make existing process system up to standard, therefore economic benefit and the equal highly significant of social benefit.
Accompanying drawing explanation
Fig. 1 is percolate ammonia nitrogen removal device example structure schematic diagram of the present invention.
Fig. 2 is percolate another example structure of ammonia nitrogen removal device of the present invention signal
Fig. 3 is embodiment of the present invention film silk structural representation;
Fig. 4 is single weep hole aperture example structure schematic diagram.
Description of reference numerals:
1-acid absorbs liquid outlet 2-waste liquid import 3-acid and absorbs liquid import 4-waste liquid outlet 5-electrodynamic valve 6-pressure transducer 7-electric control valve 8-film silk 9-housing 10-end cap one 11-end cap two 12-glue 13-weep hole 14-flange 15-union joint
Detailed description of the invention
Below in conjunction with accompanying drawing and detailed description of the invention, processing method of the present invention and percolate ammonia nitrogen handling arrangement used are described in detail as follows:
In the present invention, percolate ammonia nitrogen handling arrangement is percolate ammonia nitrogen removal device, it includes the film silk 8 of many hollows, holds the housing 9 of film silk 8, film silk 8 is disposed longitudinally in housing along housing 9, end cap 1 and end cap 2 11 it is respectively arranged with at the two ends of housing, being filled with glue 12 at the two ends of housing, glue is filled in the position at the two ends being positioned at housing of each film silk, is bonded together at the two ends of each bar film silk. Film silk wall is provided with weep hole 13, end cap 1 and end cap 2 11 closes off the two ends of housing. Being provided with acid on end cap 2 11 and absorb liquid outlet 1, be provided with acid and absorb liquid import 3 on end cap 1, the position being positioned at the lower section of glue above housing is provided with waste liquid import 2, and the position above being positioned at glue in the lower section of housing is provided with waste liquid outlet 4. 8 intervals of each film silk are arranged, and spacing distance is unrestricted, for considering the effective area of film silk assembly, it is preferred that be spaced apart 80-120 micron between film silk outer wall. The diameter of film silk endoporus is more big more favourable, but by the present situation of current film silk technology, film silk external diameter 400-500 micron, film silk wall thickness is 60-75 micron. Preferred weep hole 13 is slotted hole or elongated hole, longitudinally disposed along housing of length direction, can vertically tiltable, weep hole is provided with lip flange 14, and flange 14 turns up setting to film silk. Weep hole is evenly distributed in macroscopic situation, it is preferable that housing is cylindrical shape, and end cap one and end cap two all coordinate fixing connection with housing.
In the present invention, waste liquid import 2 and waste liquid outlet 4 are arranged on the body of housing 9, the passage of waste liquid circulation is formed between the outer surface of shell inner surface and film silk 8, waste liquid is made to flow between each film silk 8, the spacing of film silk outer wall can according to demand adjustment, therefore avoid the waste liquid blocking to film silk inner chamber, therefore, the waste liquid of big flow can be processed; Acid absorbs liquid import 3 and acid absorbs liquid outlet 1 and is separately positioned on end cap one and the end cap two at housing two ends, enter the acid in housing and absorb the liquid passage with film silk inner chamber for circulation, acid solution is made to flow in film silk inner chamber, in film silk inner chamber, the acid solution of flowing can pass through the ammonia nitrogen contained in the rubbish waste liquid of the outer flowing of weep hole 13 absorbing film silk 8, ammonia nitrogen enters into intracavity and acid in film silk and combines formation ammonium salt with acid solution intracavity flowing in film silk, absorbs liquid outlet 3 discharge from acid. In the process, acid absorbs the travelling power providing activity that liquid is ammonia nitrogen, makes ammonia nitrogen enter into intracavity in film silk, and in film silk, the acid solution of intracavity is owing to the weep hole arranged on film silk wall is thus without flowing outside film silk inner chamber. In the present invention, waste liquid import 2 and acid absorb liquid outlet 1 and are arranged on same one end of housing 9, and waste liquid outlet 4 and acid absorb liquid import 3 and are arranged on the other end of housing, the flow direction making acid absorption liquid is contrary with the flow direction of waste liquid, form cross-flow, it is more beneficial for acid and absorbs the liquid absorption for ammonia nitrogen, improve the treatment effeciency of garbage disposal liquid.
As shown in Figure 2, in order to increase the stability of water flow pressure, the waste liquid port of export is provided with current anti-deflection device, in embodiments of the invention, this current anti-deflection device is linked in sequence is formed by electrodynamic valve 5, fluid power sensor 6 and electric control valve 7, and electric control valve 7 electrically connects with pressure transducer 6. Exported 4 pipes by electrodynamic valve 5 one end with waste liquid to be connected, electric control valve 7 receive pipeline pipe with waste liquid and be connected. Outlet at waste liquid arranges current anti-deflection device, the pressure of waste liquid in cavity is monitored, is adjusted according to pressure, make the pressure held stationary of waste liquid in the cavity of housing, so it is possible to prevent current deflection, it is ensured that acid absorbs liquid to the absorption of ammonia nitrogen in percolate and combination.
For convenience of fluid sealant, the end implementation of film silk is sealed and arrange percolate import and percolate outlet, be provided with union joint 15 at housing two ends and connect end cap one and end cap two.
Percolate ammonia nitrogen processing method of the present invention is as follows: acid absorbs liquid and absorbs liquid import 3 from acid and enter into the inner chamber of film silk 8 and flow at the interior intracavity of film silk 8, absorbing liquid outlet 1 through acid and flow out, percolate is flowed into the interior intracavity of housing 9 from waste liquid import 2, flowing between film silk 8 exports 4 outflows from waste liquid, under the acid Absorption to ammonia nitrogen, ammonia nitrogen enters into intracavity in film silk 8 by the weep hole 13 arranged on film silk wall, makes ammonia nitrogen be combined with acid absorption liquid and obtains ammonium salt. in this processing procedure, the better pH value of corresponding percolate is 9-11, preferred pH value is 10.5, acid preferably absorbs the pH value of liquid less than or equal to 2, the pH value being suitable for can provide good escape power for free ammonia, be conducive to ammonia nitrogen to combine with acid, improve the treatment effeciency of percolate. acid absorbs the force value of liquid and the pressure of percolate can guarantee that acid absorption liquid and percolate energy smooth flow are advisable, wherein the pressure outline of percolate absorbs the pressure of liquid lower than acid, force value such as percolate is 0.01-0.15MPa, it is 0.03-0.15Mpa that acid absorbs the force value of liquid, when the TDS of acid absorption liquid is higher than the TDS of waste liquid, in the infiltration acid absorption liquid that moisture in waste liquid can be as far as possible few, be conducive to the process to percolate, preferred acid absorbs flow quantity 210-350L/h, garbage filter flow quantity 250-350L/h, percolate and acid absorb the temperature of liquid and are 10-50 DEG C. overall condition by domestic and international percolate at present, adopt assembly of the invention and PROCESS FOR TREATMENT percolate for entering the COD value of film waste liquid, TDS value, ammonia-nitrogen content value does not all strictly limit, namely assembly of the invention and processing method can process all parts of the country throughout the year in percolate, the COD value of current domestic percolate, TDS value, ammonia-nitrogen content value basic condition is as follows: COD value is less than or equal to 50,000 milligrams per liter, TDS value is less than or equal to 35%, ammonia-nitrogen content value is less than or equal to 5,000 mg/litre, namely assembly of the invention and technique at least can process the percolate of These parameters content.
Methods and apparatus of the present invention is adopted to process percolate, the damage to membrane component can be reduced, it is mainly manifested in the acid resistance and oil resistivity that can significantly improve membrane component, such as oil resistivity up to 5mg/L, resistance to sulphuric acid content up to 50%, resistance to content of hydrochloric acid up to 20%, resistance to nitric acid content is up to 30%, the cleaning frequency of membrane component was obviously prolonged simultaneously, up to 6 months. Table 1 is the contrast of the oil resistivity of comparative example membrane component, acid resistance and cleaning frequency in the acid resistance of inventive film element, oil resistivity and cleaning frequency and prior art.
Methods and apparatus of the present invention is adopted to process percolate, the membrane component disposal ability for percolate can be improved, reduce the requirement to percolate, such as, enter the COD value of film waste liquid up to 50,000 mg/litre, TDS value up to 35%, the ammonia-nitrogen content value in percolate is unrestricted, therefore, it can process international and domestic existing any percolate.
Below, to adopt the inventive method and to adopt art methods and process percolate the technique of the comparison present invention and the beneficial effect that reaches are described in detail.
Embodiment 1
Adopting the film silk assembly of present configuration, film silk, its internal diameter of adopting diameter to be 500 microns are 350 microns, are spaced apart 80 microns between film silk and film silk. Percolate pH value is adjusted to 11, acid absorb liquid pH value be 2, garbage filter hydraulic coupling 0.01-0.15MPa, acid absorb the force value of liquid be 0.02-0.15MP, acid absorb flow quantity 350L/h, garbage filter flow quantity 250L/h, percolate and acid absorb the temperature of liquid be 10-50 DEG C, COD of waste leachate value less than or equal to 50,000 milligrams per liter, TDS value less than or equal to 35%, ammonia-nitrogen content value unrestricted. Treated percolate, its ammonia-nitrogen content is 15mg/L.
Embodiment 2
Film silk, its internal diameter of adopting diameter to be 450 microns are 300 microns, percolate pH value is 11, acid absorb liquid pH value be 1.5, to absorb the force value of liquid be that 0.09MP, acid absorb flow quantity 210L/h, garbage filter flow quantity 350L/h for garbage filter hydraulic coupling 0.07MPa, acid, all the other are with embodiment 1. Treated percolate, its ammonia-nitrogen content is 14mg/L.
Embodiment 3
Film silk, its internal diameter of adopting diameter to be 400 microns are 250 microns, percolate pH value is 11, acid absorb liquid pH value be 1, to absorb the force value of liquid be that 0.3MP, acid absorb flow quantity 280L/h, garbage filter flow quantity 300L/h for garbage filter hydraulic coupling 0.2MPa, acid, all the other are with embodiment 1. Treated percolate, its ammonia-nitrogen content is 12mg/L.
Comparative example 1
The name mentioned in background technology is adopted to be called that percolate is processed by apparatus and method disclosed in the Chinese invention patent that " a kind of garbage leachate processing technique based on novel ammonia nitrogen removal technology ", application publication number are CN102951745. The import of its rubbish filter filtrate is arranged on shell one end, and the outlet of percolate percolate is arranged on the other end of housing, and acid absorbs flowing between liquid film silk in housing.
Film silk, its internal diameter of adopting diameter to be 250 microns are 80 microns, COD of waste leachate value less than or equal to 30,000 mg/litre, TDS value less than or equal to 28%, ammonia-nitrogen content value is less than or equal to 3,000 mg/litre, when carrying out landfill leachate treatment, percolate is intracavity flowing in hollow fiber film thread, acid absorption liquid carries out ammonia nitrogen removal at the doughnut flows outside absorption ammonia nitrogen of gas-water separation membrane module, and all the other are with embodiment 1. Treated percolate, its ammonia-nitrogen content is 14mg/L. The import of acid and the import direction of percolate are reversed.
Comparative example 2
Film silk, its internal diameter of adopting diameter to be 350 microns are 175 microns, and COD of waste leachate value is less than or equal to 20,000 milligrams per liter, and all the other are with embodiment 2. Treated percolate, its ammonia-nitrogen content is 14mg/L.
Comparative example 3
Film silk, its internal diameter of adopting diameter to be 400 microns are 250 microns, percolate pH value is 10, acid absorb liquid pH value be 1.5, to absorb the force value of liquid be that 0.12MP, acid absorb flow quantity 280L/h, garbage filter flow quantity 300L/h for garbage filter hydraulic coupling 0.1MPa, acid, all the other are with embodiment 3. Treated percolate, its ammonia-nitrogen content is 14mg/L.
Table 1: for present invention process to percolate requirement, membrane component acid resistance, oil resistivity and cleaning frequency and prior art processes to percolate requirement, the oil resistivity of membrane component, acid resistance and the contrast table of cleaning frequency.
Be can be seen that by subordinate list, in present invention process, the thickness of film silk does not significantly affect for the disposal ability of the percolate of film silk assembly, and the requirement for percolate of the film silk internal diameter in film silk assembly and disposal ability are had obvious difference by prior art processes, along with the minimizing of film silk internal diameter is strict all the more to the requirement of SS and SDI value, the cleaning frequency of membrane component substantially increases.
The method of the present invention, requirement for SS and the SDI value of percolate is substantially better than prior art, and its cleaning frequency extends 30-40 times than the cleaning frequency of prior art, in prior art, often 2 hours about consuming time of membrane module of cleaning, therefore, can significantly shorten and clean the time used, significantly improve production efficiency. The method of the present invention all has significant reduction for the requirement of the water inlet ss suspended solid value of percolate, water inlet SDI value, it is, apparatus of the present invention and technique significantly improve for the disposal ability of percolate, achieves beyond thought technique effect. In processing method of the present invention, owing to the escape velocity of free ammonia is very fast, the weep hole on silk wall occurs without clogging.
Subordinate list
Claims (11)
1. a percolate ammonia nitrogen removal membrane module, including housing (9), housing (9) two ends are respectively arranged with end cap one (10) and end cap two (11), it is provided with the film silk (8) of hollow along the length direction of housing in housing, film silk is spaced between (8), the outer surface at film silk two ends seals and is fixed in housing (9), it is characterized in that, end cap two (11) is provided with acid and absorbs liquid outlet (1), end cap one (10) is provided with acid and absorbs liquid import (3), film silk (8) inner chamber two ends absorb liquid outlet respectively with acid and acid absorbs liquid entrance and connects, what be positioned at sealing place with housing of the film silk in the upper end of housing (9) is arranged below waste liquid import (2), what be positioned at housing sealing place with film silk in the lower end of housing is provided above waste liquid outlet (4), the inner chamber between film silk and sealing place at two ends in housing exports (4) with waste liquid import (2) and waste liquid respectively and connects, film silk wall is provided with multiple weep hole (13) along the length direction of film silk, film silk inner chamber is connected with housing cavity by weep hole (13).
2. the percolate ammonia nitrogen removal membrane module described in claim 1, it is characterised in that export (4) end at waste liquid and be provided with in current anti-deflection device control housing the pressure of the percolate flowed.
3. the percolate ammonia nitrogen removal membrane module described in claim 2, it is characterised in that described current anti-deflection device is water flow pressure detection and adjustment device.
4. the percolate ammonia nitrogen removal membrane module described in claim 3, it is characterized in that, described current anti-deflection device is linked in sequence is formed by electrodynamic valve (5), pressure transducer (6) and electric control valve (7), electric control valve electrically connects with pressure transducer, electrodynamic valve one end be connected with waste liquid outlet.
5. the percolate ammonia nitrogen removal membrane module described in claim 1, it is characterised in that the two ends of described film silk are sealed by glue and are fixed in housing (9).
6. the percolate ammonia nitrogen removal membrane module described in claim 1, it is characterized in that, described weep hole (13) is elongated hole, and its length direction is arranged along the length direction of film silk, and described weep hole (13) is provided with turned-out flange (14).
7. the percolate ammonia nitrogen removal membrane module described in claim 1, it is characterised in that each film silk is vertically uniformly arranged in housing.
8. a percolate ammonia nitrogen removal method, it is characterized in that, percolate is processed by employing ammonia nitrogen removal membrane module, and after acid absorption liquid enters into intracavity in film silk by sour absorption liquid import, in film silk, intracavity flows and absorbs ammonia nitrogen, warp is exported outflow by acid absorption liquid; Percolate enters in housing via waste liquid import, flows between film silk after ammonia nitrogen is deviate from through being flowed out by percolate outlet.
9. a kind of percolate ammonia nitrogen removal method described in claim 8, it is characterised in that adopt claim 1-7 one of every described percolate ammonia nitrogen removal membrane module that percolate is processed.
10. the percolate ammonia nitrogen removal method described in claim 8 or 9, it is characterized in that, percolate pH value is 8-11, acid preferably absorbs the pH value of liquid less than or equal to 2, the pressure of percolate absorbs the pressure of liquid not higher than acid and acid can be made to absorb liquid and percolate flowing, acid absorb flow quantity 210-350L/h, garbage filter flow quantity 250-350L/h, percolate and acid absorb the temperature of liquid be 10-50 DEG C, the TDS value of percolate is less than or equal to 35%.
11. the percolate ammonia nitrogen removal method described in claim 10, it is characterised in that the force value of percolate be 0.01-0.15MPa, acid absorb liquid force value be 0.02-0.15MPa.
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| US5122165A (en) * | 1990-07-10 | 1992-06-16 | International Environmental Systems, Inc. | Removal of volatile compounds and surfactants from liquid |
| CN101508500A (en) * | 2009-03-20 | 2009-08-19 | 厦门凯瑞尔数字环保科技有限公司 | Method for recycling ammonia nitrogen from garbage leachate by using film coagulate contact reactor |
| CN104211244A (en) * | 2013-06-03 | 2014-12-17 | 洁海瑞泉膜技术（北京）有限公司 | Method for gas membrane-process treatment of ammonia-containing feed liquid or wastewater with renewable absorbent and by-producted strong aqua ammonia |
| CN205381990U (en) * | 2016-01-30 | 2016-07-13 | 秦皇岛同力达环保能源股份有限公司 | Landfill leachate ammonia nitrogen removal device |
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