CN209242811U - A kind of processing unit of ammonia nitrogen waste water - Google Patents
A kind of processing unit of ammonia nitrogen waste water Download PDFInfo
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- CN209242811U CN209242811U CN201821759030.0U CN201821759030U CN209242811U CN 209242811 U CN209242811 U CN 209242811U CN 201821759030 U CN201821759030 U CN 201821759030U CN 209242811 U CN209242811 U CN 209242811U
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Abstract
The utility model provides a kind of processing unit of ammonia nitrogen waste water, described device includes waste water original pond I, waste water original pond II, pretreatment pool, stripping tower, absorption tower, mixing pit, ultrafiltration apparatus, ultrafiltrate storage tank, gaseous state membrane module, absorbing liquid reserve pool and ammonium salt storage tank, wherein, the pipeline being connected with the entrance in gaseous state membrane module shell is equipped with flowmeter and thermometer.The present apparatus realizes the continuous ammonia nitrogen removal processing of ammonia nitrogen waste water, and the simple process of ammonia nitrogen waste water processing is carried out using the device, and ammonia-nitrogen removal rate is high, and through gaseous state membrane module, treated that waste water meets discharge standard.In technical process, gaseous state membrane stability is good, will not generate the osmotic distillation of water, and gas film ammonia nitrogen removal process can continue to carry out, and is conducive to industrializing implementation.
Description
Technical field
The utility model belongs to ammonia nitrogen waste water process field more particularly to a kind of processing unit of ammonia nitrogen waste water.
Background technique
In recent years, with the rapid hair of the industries such as petrochemical industry, coal chemical industry, fine chemistry industry, chemical fertilizer, pharmacy, metallurgy, electronics
Exhibition is grown, and the day discharge amount of ammonia nitrogen waste water is constantly increasing.And the ammonia nitrogen in waste water is water eutrophication and environmental pollution
Important substance influences water quality and human health, while also resulting in the huge waste of resource.Therefore, national requirements nitrogen-containing wastewater
It needs to be removed using ammonia nitrogen removal technology, and can just be discharged after reaching " integrated wastewater discharge standard ".
Currently, the most common ammonia nitrogen removal technology has bioanalysis, stripping and vaporizing extract process, chemical precipitation method, break point chlorination method
With support air film method etc..Biochemical method effect stability does not generate secondary pollution, and both economical, but take up a large area,
The disadvantages of low temperature aging rate is low, more troublesome vulnerable to noxious material influence and operational management.Ammonia aeration, stripping process have process
Simply, the features such as treatment effect is stablized, but energy consumption is high, is easy to cause secondary pollution, processing cost higher, and it is stifled that equipment is easy fouling
Plug, equipment need often shut-down, disassembly and cleaning.Chemical precipitation method and break point chlorination method can effectively remove the ammonia nitrogen in waste water,
But new compound can be introduced, it is possible to cause secondary pollution, affect the recyclability of waste water.
Gas film (or being referred to as support air film, liquid-liquid film absorbs) method is to separate water containing ammonia using dewatering microporous film
(feed liquid or waste water) and sour absorbing liquid, volatile amino molecule diffuses to feed liquid-membrane interface from bulk water phase in feed liquid or waste water,
Gasification diffuses through micropore to film-acid solution interface dissolution and enters absorbing liquid, and quick irreversible reaction occurs with hydrogen ion and generates
Fixedness ammonium ion and removed, which directly does motive force with the chemical potential that Acid-Base neutralizes, and due to film
The concentration of absorption side free ammonia be zero, this provides the maximum impetus of deamination process, so that the deamination process is not necessarily to
Heat loss, without the electric power of air circulation, only need to consume a small amount of electric power makes feed liquid or waste water flow through membrane module, thus greatly reduces
Process operating cost.Since the membrane process provides maximum deamination motive force, this is but also the process can be easier waste water
In ammonia nitrogen concentration be down to national secondary discharge standard even first discharge standard hereinafter, so that deamination waste water even can be with
Reuse.
But during gas film deamination, not only amino molecule enters absorbing liquid through membranous wall, and hydrone also penetrates film
Micropore on wall enters absorbing liquid (osmotic distillation of association), leads to absorbing liquid rapid spatial expansion, as a result, absorbing liquid quilt
Dilution, and acid and salinity are higher in absorbing liquid, and the osmotic distillation phenomenon of water is more serious, therefore hardly results in the by-product of expectation
Product, that is, high concentration ammonium salt solution.Chinese patent CN106186492A is by keeping the temperature difference between waste water and absorbing liquid in 10-20
DEG C, the ammonia nitrogen concentration in waste water is improved to 1000-10000mg/L, and electrolyte is added to overcome the infiltration of association in waste water
Distillation problem thoroughly, but the temperature difference is difficult to control in this method, two sides quickly reach equalized temperature, and ammonia nitrogen in high density influences gaseous state
The stability of membrane module causes its easy to pollute, and reduced service life limits its popularization and application.Specifically for ammonia nitrogen waste water processing
Device it is more rare.
Utility model content
The purpose of this utility model is to provide a kind of processing unit of ammonia nitrogen waste water, the present apparatus exclusively for ammonia nitrogen waste water at
It manages and designs, ammonia nitrogen waste water is pre-processed, then remove ammonia nitrogen, ammonia nitrogen removal frank via stripping tower and gaseous state membrane module
Height, final waste liquid can be with direct emissions；By monitoring the condition of gas film deamination, so that the stability of gaseous state membrane module is good,
And the osmotic distillation that water can be greatly reduced maintains the concentration of absorbing liquid, promotes the generation of ammonium salt.
Specifically, in view of the deficiencies of the prior art, the utility model provides following technical solution:
A kind of processing unit of ammonia nitrogen waste water, the device include waste water original pond I 100, waste water original pond II 101, pretreatment pool
200, stripping tower 300, absorption tower 400, mixing pit 500, ultrafiltration apparatus 600, ultrafiltrate storage tank 601, gaseous state membrane module 700, suction
Receive liquid reserve pool 80 and ammonium salt storage tank 81, wherein
Waste water original pond I 100 is connected by pipeline with pretreatment pool 200, and treated that waste water leads to for pretreatment pool 200
Piping flows through pump 102, then the inlet tube 301 on 300 top of stripping tower is flow to by pipeline, and the lower end of the inlet tube 301 is set
There is spray nozzle 306；The top of the stripping tower 300 is equipped with gas outlet 303, and bottom is equipped with discharge port 304, and lower sides run through
It is connected with ventilation duct, one end of ventilation duct connects air blower 91, and the other end is the air outlet 305 in stripping tower 300；
The gas outlet 303 is connected by pipeline with the air inlet 401 on absorption tower 400, the absorption tower 400 it is upper
For portion's side wall through being connected with fluid-through tube, the fluid-through tube is located at one section inside absorption tower 400 equipped with atomizer 403, another
End connection pump 103 pumps 103 other end connection hydrochloric acid tank 9；
The discharge port 304 and waste water original pond II 101 are connected by pipeline with the entrance of mixing pit 500 respectively, mixing pit
500 outlet is connected by pipeline with the entrance of ultrafiltration apparatus 600, and the outlet of ultrafiltration apparatus 600 is stored up by pipeline and ultrafiltrate
Slot 601 is connected；
The ultrafiltrate storage tank 601 is connected by pipeline with the waste liquid entrance 702 on 700 shell of gaseous state membrane module, described
Several hollow fiber microporous membranes 701 are equipped with inside gaseous state membrane module 700, on the horizontal direction shell opposite with waste liquid entrance 702
Equipped with waste liquid outlet 703, waste liquid is flowed through in the hollow tube side of hollow fiber microporous membrane 701, the ipsilateral shell with waste liquid outlet 703
Be equipped with absorbing liquid entrance 704, with the ipsilateral shell of waste liquid entrance 702 be equipped with taphole, the taphole through pipeline with
Ammonium salt storage tank 81 is connected, and ammonium salt storage tank 81 is connected by pipeline with pump 102；
The absorbing liquid entrance 704 is connected by pipeline with absorbing liquid reserve pool 80.
Preferably, filled layer 302 is equipped with positioned at the lower part of spray nozzle 306 in the stripping tower 300；The absorption tower 400
The interior lower part positioned at atomizer 403 is equipped with buffer layer 402.
Preferably, described device further includes at least one of following technical characteristic:
Thermometer I 602 is equipped in the ultrafiltrate storage tank 601；
Thermometer II 801 is equipped in the absorbing liquid reserve pool 80.
Preferably, described device further includes at least one of following technical characteristic:
PH meter I 811 is equipped in the ammonium salt storage tank 81；
PH meter II 502 is equipped in the mixing pit 500.
Preferably, described device further includes at least one of following technical characteristic:
Pipeline between the ultrafiltrate storage tank 601 and waste liquid entrance 702 is equipped with valve I 603 and temperature indicator I
605, the valve I 603 is close to the outlet of ultrafiltrate storage tank 601, and temperature indicator I 605 is close to waste liquid entrance 702；
Pipeline between the absorbing liquid reserve pool 80 and absorbing liquid entrance 704 is equipped with valve II 802 and temperature display
Device II 804, the valve II 802 is close to the outlet of absorbing liquid reserve pool 80, and temperature indicator II 804 is close to absorbing liquid entrance
704。
Preferably, flow meter I 604 is additionally provided on the pipeline between the valve I 603 and temperature indicator I 605；It is described
Flow meter II 803 is additionally provided on pipeline between valve II 802 and temperature indicator II 804.
Compared with prior art, it the effect of the utility model and has an advantage that:
(1) present apparatus includes pretreatment pool, stripping tower, absorption tower, mixing pit, ultrafiltration apparatus and gaseous state membrane module, highly concentrated
Degree ammonia nitrogen waste water first carries out ammonia aeration through stripping tower, and after waste water is mixed with Low Concentration Ammonia Containing Wastewater after stripping, then gas is used in ultrafiltration
State membrane module removal of ammonia and nitrogen, the device are suitable for the ammonia nitrogen waste water of various concentration, have a wide range of application, and ammonia nitrogen removal is high-efficient, place
Waste liquid after reason meets discharge standard.
(2) pretreatment pool pretreatment of high strength ammonia nitrogen waste is taken off in addition composite decoloring agent and heavy metal chelating agent
Color and after removing removing heavy metals, then waste water is pumped to stripping tower, can greatly improve stripping efficiency by strainer flow ipe, drop
The blocked risk of filled layer in low stripping tower, extends stripping tower service life.
(3) ultrafiltrate and acid absorbing liquid are that a formula excessively is maintained by gaseous state membrane module, the concentration of acid absorbing liquid
Reduced levels avoid the osmotic distillation of water so that the vapour pressure of water is close in waste liquid and absorbing liquid, and gas film deamination can continue
It carries out, is convenient for industrializing implementation.
(4) regulation is super jointly for the thermometer I 602 in device, valve I 603, flow meter I 604 and temperature indicator I 605
Filtrate enters the temperature and flow velocity of gaseous state membrane module, thermometer II 801, valve II 802, flow meter II 803, temperature indicator II
804 collective effects regulation absorbing liquid enters the temperature and flow velocity of gaseous state membrane module, improves the mass tranfer coefficient of film, and it is de- to improve ammonia nitrogen
Except efficiency, while the stability of gas film can be improved, film surface is avoided to block, prevented the mutual pollution of absorbing liquid and waste liquid, mention
The service life of high film.
(5) solution collected in ammonium salt storage tank is that acid absorbing liquid is formed after the ammonia that gaseous state membrane module absorbs in waste liquid
Ammonium salt solution, add alkali adjust pH after, be pumped into stripping tower carry out ammonia aeration, then absorb to obtain the chlorination of high-purity through absorption tower
Ammonium avoids that high energy consumption caused by ammonium salt solution is concentrated using multi-effect evaporator.
To sum up, ammonia nitrogen wastewater treatment device provided by the utility model has a wide range of application, and ammonia nitrogen removal is high-efficient, stripping tower
Good, the long service life with the stability of gaseous state membrane module.Ammonia nitrogen waste water processing, the ammonia being able to achieve in waste water are carried out using the device
Nitrogen is completely converted into ammonium chloride, recycles, and economizes on resources, while not will lead to secondary pollution.
Detailed description of the invention
Fig. 1 is the schematic device of embodiment 1；
Fig. 2 is the schematic device of embodiment 2；
Fig. 3 is the schematic device of embodiment 3.
Wherein, 100- waste water original pond I, 101- waste water original pond II, 200- pretreatment pool, 201- feeding port, 102- pump,
300- stripping tower, 301- inlet tube, 306- spray nozzle, 302- filled layer, the gas outlet 303-, 304- discharge port, 305- outlet air
Mouthful, 91- air blower, the absorption tower 400-, 401- air inlet, 402- buffer layer, 403- atomizer, 404- discharge port, 103-
Pump, 9- hydrochloric acid tank, 500- mixing pit, 501- feed opening, 502-pH count II, 60- ultrafiltration apparatus, 600- ultrafiltration apparatus, 601-
Ultrafiltrate storage tank, 602- thermometer I, 603- valve I, 604- flow meter I, 605- temperature indicator I, 700- gaseous state membrane module,
701- hollow fiber microporous membrane, 702- waste liquid entrance, 703- waste liquid outlet, 704- absorbing liquid entrance, 80- absorbing liquid reserve pool,
801- thermometer II, 802- valve II, 803- flow meter II, 804- temperature indicator II, 81- ammonium salt storage tank, 811-pH meter
Ⅰ。
Specific embodiment
The utility model provides a kind of processing unit of ammonia nitrogen waste water, which includes waste water original pond I 100, waste water original
Pond II 101, pretreatment pool 200, stripping tower 300, absorption tower 400, mixing pit 500, ultrafiltration apparatus 600, ultrafiltrate storage tank 601,
Gaseous state membrane module 700, absorbing liquid reserve pool 80 and ammonium salt storage tank 81.Each equipment is used cooperatively, and improves ammonia nitrogen removal efficiency.
The utility model additionally provides a kind for the treatment of process of ammonia nitrogen waste water, which handled by above-mentioned ammonia nitrogen waste water
What device was realized, specific steps include:
S1. (ammonia-nitrogen content is flow in 1000mg/L or more) via pipeline the high-concentration ammonia nitrogenous wastewater in waste water original pond I 100
In pretreatment pool 200, pretreated wastewater pH enters the inlet tube of stripping tower 300 in 11-13 under the action of pumping 102
301, waste water is sprayed by spray nozzle 306, what the discharge pipe that waste water was arranged with stripping tower lower part be connected with air blower 91 was blown out
Hot air, stripping ammonia, ammonia flow to absorption tower 400 by gas outlet 303, generate ammonium chloride.
Wherein, in pretreatment pool 200 pretreatment of high strength ammonia nitrogen waste method are as follows: sequentially added by feeding port 201
Composite decoloring agent and heavy metal chelating agent stir 30-50 minutes, obtain pretreated waste water.Composite decoloring agent and high concentration
The solid-liquid ratio g/mL of ammonia nitrogen waste water is 10-20:10000, and the solid-liquid ratio g/mL of heavy metal chelating agent and high-concentration ammonia nitrogenous wastewater is
2-3:10000；And composite decoloring agent is by calcium hydroxide, sodium hydroxide, active carbon and flyash according to weight ratio 3-4:2:3:
1-2 is obtained by mixing.
S2. stripping treated waste water flows to mixing pit 500 through discharge port 304, the low concentration ammonia in waste water original pond II 101
Nitrogen waste water (ammonia-nitrogen content is in 20-30mg/L) is stirred to obtain mixed waste liquor that (ammonia nitrogen contains by pipeline flow-direction mixing pit 500
Amount is in 50-80mg/L), be added one or more of sodium hydroxide, calcium hydroxide and calcium oxide adjust the pH to 11 of waste liquid with
On, then through 600 ultrafiltration of ultrafiltration apparatus, ultrafiltrate is stored in ultrafiltrate storage tank 601.
S3. ultrafiltrate enters in the hollow fiber microporous membrane 701 in gaseous state membrane module 700 via waste liquid entrance 702
In blank pipe journey；Absorbing liquid in absorbing liquid reserve pool 80 enters in gaseous state membrane module 700 via absorbing liquid entrance 704, absorbing liquid
It is in opposite cross-flow passes with ultrafiltrate, the ammonia nitrogen vaporization in ultrafiltrate into absorbing liquid, reacts and produces ammonium salt solution.
Waste liquid after removal of ammonia and nitrogen is discharged via waste liquid outlet 703, and ammonium salt solution is flowed into ammonium salt storage tank 81 by taphole.It absorbs
Liquid is one of acid absorbing liquid, including sulfuric acid, hydrochloric acid, nitric acid and phosphoric acid, mass concentration 3-5%.
The flow velocity that control ultrafiltrate enters gaseous state membrane module is 2-5mL/s, and temperature is 35-45 DEG C, and absorbing liquid enters gaseous state
The flow velocity of membrane module is 1-6mL/s, and temperature is 50-60 DEG C.The mass tranfer coefficient of film is high, and ammonia nitrogen removal is high-efficient.
S4. the solution in ammonium salt storage tank 81 is pumped into the inlet tube of stripping tower 300 after adjusting pH to 11-13 by pump 102
In 301, ammonia aeration is carried out, is then absorbed by absorption tower 400 and obtains ammonium chloride.This method is avoided to be concentrated using multi-effect evaporator
High energy consumption caused by ammonium salt solution.So far, the ammonia nitrogen in waste water is completely converted into ammonium chloride, recycles, and realizes recycling.
The high-concentration ammonia nitrogenous wastewater of enterprise mainly includes condensation concentrated ammonia liquor, ammonia of the ammonia-nitrogen content in 10000-20000mg/L
Nitrogen content the weak aqua ammonia of 1000mg/L, ammonia-nitrogen content 10000mg/L mother liquor and ammonia-nitrogen content in the clear of 5000mg/L
APT waste water is washed, Low Concentration Ammonia Containing Wastewater is mainly ion exchange waste water of the ammonia-nitrogen content in 20-30mg/L, wherein ammonia nitrogen contains
Amount is all made of reagent colorimetric method measurement.
Below in conjunction with the attached drawing in the embodiments of the present invention, to the technical solution in the embodiments of the present invention
It is clearly and completely described, it is clear that the described embodiments are only a part of the embodiments of the utility model, rather than complete
The embodiment in portion.Based on the embodiments of the present invention, those of ordinary skill in the art are not before making creative work
Every other embodiment obtained is put, is fallen within the protection scope of the utility model.
It should be noted that the utility model relates to material, reagent and equipment be commercially available, wherein heavy metal chelating agent
Model HMC-M1 is purchased from the limpid Environmental Protection Technology Co., Ltd in Suzhou；The oil-filled shockproof dial thermometer of XY-014 is purchased from Changzhou
Xi Ya finite instrument company, city；The explosion-proof industrial ph of PHG-22 is purchased from Wuhan core light instrument Manufacturing Co., Ltd；Flyash purchase
From Lingshou County Heng Ju mineral products processing factory.
Embodiment 1
As shown in Fig. 1, a kind of processing unit of ammonia nitrogen waste water, the device include waste water original pond I 100, waste water original pond II
101, pretreatment pool 200, stripping tower 300, absorption tower 400, mixing pit 500, ultrafiltration apparatus 600, ultrafiltrate storage tank 601, gaseous state
Membrane module 700, absorbing liquid reserve pool 80 and ammonium salt storage tank 81.Wherein, waste water original pond I 100 passes through pipeline and 200 phase of pretreatment pool
Connection, the outlet of pretreatment pool 200 is connected with pipeline, and the exit is equipped with filter screen, treated the waste water stream of pretreatment pool 200
Through filter screen, pump 102 is flowed through by pipeline, then the inlet tube 301 on 300 top of stripping tower is flow to by pipeline, inlet tube 301
Lower end is equipped with spray nozzle 306.The top of stripping tower 300 is equipped with gas outlet 303, and bottom is equipped with discharge port 304, and lower sides run through
It is connected with ventilation duct, one end of ventilation duct connects air blower 91, and the other end is the air outlet 305 in stripping tower 300.Out
Port 303 is connected by pipeline with the air inlet 401 on absorption tower 400, and the upper portion side wall on absorption tower 400 is logical through being connected with
Liquid pipe, one end which is located inside absorption tower 400 are connected with atomizer 403, and other end connection pump 103 pumps 103
The other end connects hydrochloric acid tank 9.Discharge port 304 and waste water original pond II 101 pass through the entrance phase of pipeline and mixing pit 500 respectively
Even, the outlet of mixing pit 500 is connected by pipeline with the entrance of ultrafiltration apparatus 600, the outlet of ultrafiltration apparatus 600 pass through pipeline and
Ultrafiltrate storage tank 601 is connected.Ultrafiltration membrane in ultrafiltration apparatus 600 is polytetrafluoroethylene film.Ultrafiltrate storage tank 601 passes through pipeline
It is connected with the waste liquid entrance 702 on 700 shell of gaseous state membrane module, it is micro- that 1600 doughnuts is equipped with inside gaseous state membrane module 700
Pore membrane 701, the horizontal direction shell opposite with waste liquid entrance 702 are equipped with waste liquid outlet 703, and waste liquid flows through doughnut micropore
In the hollow tube side of film 701, it is equipped with absorbing liquid entrance 704 with the ipsilateral shell of waste liquid outlet 703, it is same with waste liquid entrance 702
The shell of side is equipped with taphole, which is connected through pipeline with ammonium salt storage tank 81, ammonium salt storage tank 81 pass through pipeline and
Pump 102 is connected；Absorbing liquid entrance 704 is connected by pipeline with absorbing liquid reserve pool 80.Doughnut micropore in the present apparatus
Film is hydrophobic film, specially polypropylene screen.
The process of ammonia nitrogen waste water processing is carried out using above-mentioned apparatus are as follows: the high-concentration ammonia nitrogenous wastewater quilt in waste water original pond I 100
It is transported in pretreatment pool 200 and is pre-processed, be then pumped into stripping tower 300 by pump 102 and carry out ammonia-nitrogen desorption, pretreatment
High-concentration ammonia nitrogenous wastewater improves stripping efficiency；The ammonia that stripping comes out enters gas pipeline by gas outlet 303, is transported to suction
Tower 400 is received, reacts to obtain ammonium chloride with ammonia by spraying hydrochloric acid.The bottom product of stripping tower is flowed into mixed by discharge port 304
Pond 500 is closed, is mixed with the Low Concentration Ammonia Containing Wastewater in the same waste water original pond II 101 for flowing into mixing pit 500, it is useless to obtain mixing
Liquid.Mixed waste liquor carries out ultrafiltration by ultrafiltration apparatus 600, and ultrafiltrate is stored in ultrafiltrate storage tank 601, then flows to gas film
Component 700, ultrafiltrate flow in the hollow tube side of hollow fiber microporous membrane 701, the acid absorption in absorbing liquid reserve pool 80
Liquid flows into gaseous state membrane module 700 by absorbing liquid entrance 704, and in shell fluid flow, absorbing liquid and ultrafiltrate are in opposite cross-flow passes,
Ammonia in ultrafiltrate is vaporizing with gas film interface and is diffusing through fenestra, in gas film and absorbing liquid interface and acid suction
The hydrogen ion reaction in liquid is received, ammonium salt solution is generated, ammonium salt solution flows into ammonium salt storage tank 81 by taphole, then passes through pump
102 are pumped into stripping tower 300, and the ammonia of stripping enters back into after absorption tower 400 is absorbed and generates ammonium chloride；And ultrafiltrate (waste liquid) passes through
Meet discharge standard (lower than 15mg/mL) after gas film deamination, it can be with direct emission.Whole device realizes ammonia nitrogen in waste water and arrives
Resource reutilization is realized in the conversion of ammonium chloride, environmentally friendly.In addition, the present apparatus can be applied to high concentration and low concentration simultaneously
Ammonia nitrogen waste water, have a wide range of application, the waste liquid after absorbing liquid and ultrafiltration is one to cross formula by gaseous state membrane module, it is ensured that is absorbed
The concentration of liquid is stablized, and ammonia-nitrogen removal rate is high.
Embodiment 2
As shown in Fig. 2, a kind of processing unit of ammonia nitrogen waste water, the device include waste water original pond I 100, waste water original pond II
101, pretreatment pool 200, stripping tower 300, absorption tower 400, mixing pit 500, ultrafiltration apparatus 600, ultrafiltrate storage tank 601, gaseous state
Membrane module 700, absorbing liquid reserve pool 80 and ammonium salt storage tank 81.Waste water original pond I 100 is connected by pipeline with pretreatment pool 200,
The outlet of pretreatment pool 200 is connected with pipeline, which is equipped with filter screen (pore size is 100 μm), at pretreatment pool 200
Waste water stream after reason flows through pump 102 by pipeline, is flow on stripping tower 300 by pipeline again under the action of pump through filter screen
The lower end of the inlet tube 301 in portion, inlet tube 301 is equipped with spray nozzle 306.The top of stripping tower 300 is equipped with gas outlet 303, bottom
Equipped with discharge port 304, for lower sides through being connected with ventilation duct, one end of ventilation duct connects air blower 91, the other end be positioned at
Air outlet 305 in stripping tower 300.Gas outlet 303 is connected by pipeline with the air inlet 401 on absorption tower 400, absorption tower
For 400 upper portion side wall through being connected with fluid-through tube, which is located at one section inside absorption tower 400 equipped with several atomizers
403, other end connection pump 103 pumps 103 other end connection hydrochloric acid tank 9.Discharge port 304 and waste water original pond II 101 are distinguished
It is connected by pipeline with the entrance of mixing pit 500, the outlet of mixing pit 500 passes through the entrance phase of pipeline and ultrafiltration apparatus 600
Even, the outlet of ultrafiltration apparatus 600 is connected by pipeline with ultrafiltrate storage tank 601.Ultrafiltration membrane in ultrafiltration apparatus 600 is to gather inclined fluorine
Vinyl film or polypropylene screen.Ultrafiltrate storage tank 601 passes through pipeline and 702 phase of waste liquid entrance on 700 shell of gaseous state membrane module
Even, be equipped with 2000 hollow fiber microporous membranes 701 inside gaseous state membrane module 700, horizontal direction it is opposite with waste liquid entrance 702 outside
Shell is equipped with waste liquid outlet 703, and waste liquid flows through in the hollow tube side of hollow fiber microporous membrane 701, ipsilateral with waste liquid outlet 703
Shell be equipped with absorbing liquid entrance 704, with the ipsilateral shell of waste liquid entrance 702 be equipped with taphole, the taphole warp
Pipeline is connected with ammonium salt storage tank 81, and ammonium salt storage tank 81 is connected by pipeline with pump 102；Absorbing liquid entrance 704 is by pipeline and inhales
Liquid reserve pool 80 is received to be connected.Hollow fiber microporous membrane in the present apparatus is hydrophobic film, specially polytetrafluoroethylene film.
Wherein, it is equipped with filled layer 302 (filler is ceramic packing) positioned at the lower part of spray nozzle 306 in stripping tower 300, absorbed
Positioned at the lower part of atomizer 403, equipped with buffer layer 402, (filler of buffer layer is that SM125Y polypropylene ripple is filled out in tower 400
Material).Filled layer can increase gas liquid interfacial area, improve stripping efficiency.Buffer layer equally can increase gas liquid interfacial area, improve ammonia
Aspiration efficiency.
It is equipped with pH meter II 502 in mixing pit 500, is equipped with pH meter I 811 in ammonium salt storage tank 81, monitors in mixing pit mix respectively
It closes the pH of liquid and the pH of ammonium salt solution, pH is adjusted to predetermined value and can effectively improve gaseous state membrane module and stripping tower removal ammonia nitrogen
Efficiency；Avoid the need for the trouble of period sampling measuring pH.PH meter II 502 and pH meter I 811 are the explosion-proof industrial ph of PHG-22.
Thermometer I 602, the temp probe of thermometer I 602 and going out for ultrafiltrate storage tank 601 are equipped in ultrafiltrate storage tank 601
Mouth is concordant, and the pipeline between ultrafiltrate storage tank 601 and waste liquid entrance 702 is equipped with valve I 603 and temperature indicator I 605, valve
Door I 603 is close to the outlet of ultrafiltrate storage tank 601, and temperature indicator I 605 is close to waste liquid entrance 702；Valve I 603 and temperature are aobvious
Show and is additionally provided with flow meter I 604 on the pipeline between device I 605.Thermometer II 801, thermometer II are equipped in absorbing liquid reserve pool 80
801 temp probe is concordant with the outlet of absorbing liquid reserve pool 80, the pipe between absorbing liquid reserve pool 80 and absorbing liquid entrance 704
Road is equipped with valve II 802 and temperature indicator II 804, and valve II 802 is close to the outlet of absorbing liquid reserve pool 80, temperature display
Device II 804 is additionally provided with flow meter II on the pipeline between absorbing liquid entrance 704, valve II 802 and temperature indicator II 804
803.Thermometer I 602 and thermometer II 801 are the oil-filled shockproof dial thermometer of XY-014.Ultrafiltrate storage tank 601 is to gaseous state
It is cased with thermal insulation material on the pipeline between waste liquid entrance 702 on membrane module, which is mineral wool, is purchased from Langfang good fortune nurse
This energy saving Science and Technology Ltd.；Pipe between the absorbing liquid entrance 704 of absorbing liquid reserve pool 80 being exported on gaseous state membrane module
Also the glass wool material of heat preservation is cased on road.Thermometer I 602, valve I 603, flow meter I 604 and temperature indicator I 605 are common
Regulation ultrafiltrate enters the temperature and flow velocity of gaseous state membrane module, and thermometer II 801, valve II 802, flow meter II 803, temperature are aobvious
Show that II 804 collective effect of device regulation absorbing liquid enters the temperature and flow velocity of gaseous state membrane module, improves the mass tranfer coefficient of film, improve
Ammonia nitrogen removal efficiency, while the stability of gas film can be improved, it avoids film surface from blocking, prevents the mutual dirt of absorbing liquid and waste liquid
Dye, improves the service life of film.
Embodiment 3
As shown in figure 3, ammonia nitrogen wastewater treatment device provided in this embodiment is improved on the basis of embodiment 2,
Ultrafiltration apparatus 60 is also provided with after pretreatment pool 200.High-concentration ammonia nitrogenous wastewater after pretreatment, is introduced into ultrafiltration apparatus
60 carry out ultrafiltration, then enter stripping tower by pump 102.Remaining is the same as embodiment 2.Ultrafiltration membrane in ultrafiltration apparatus 60 is to gather inclined fluorine
Vinyl film, aperture are 0.1 micron, can further filter out micron-sized impurity, improve the stripping efficiency of stripping tower.
Embodiment 4
A kind for the treatment of process of ammonia nitrogen waste water, comprising the following steps:
S1. the high-concentration ammonia nitrogenous wastewater in waste water original pond I 100 is the condensation concentrated ammonia liquor of ammonia-nitrogen content 15000mg/L, via
Pipeline is flow in pretreatment pool 200, and pretreated wastewater pH is 11, and the feed liquor of stripping tower 300 is entered under the action of pumping 102
Pipe 301 sprays waste water by spray nozzle 306, and the discharge pipe that waste water was arranged with stripping tower lower part be connected with air blower 91 is blown out
Hot air, stripping ammonia, ammonia flows to absorption tower 400 by gas outlet 303, generates ammonium chloride.
Wherein, in pretreatment pool 200 pretreatment of high strength ammonia nitrogen waste method are as follows: sequentially added by feeding port 201
Composite decoloring agent and heavy metal chelating agent HMC-M1 are stirred 50 minutes with the revolving speed of 250r/min, obtain pretreated waste water.
The solid-liquid ratio g/mL of composite decoloring agent and high-concentration ammonia nitrogenous wastewater is 10:10000, and heavy metal chelating agent and ammonia nitrogen in high density are useless
The solid-liquid ratio g/mL of water is 2:10000；And composite decoloring agent be by calcium hydroxide, sodium hydroxide, active carbon and flyash according to
Weight ratio 3:2:3:1 is obtained by mixing.
S2. ammonia-nitrogen content is 100mg/L in stripping treated waste water, flows to mixing pit 500, waste water through discharge port 304
Low Concentration Ammonia Containing Wastewater (ammonia-nitrogen content is in 20mg/L) in former pond II 101 is stirred by pipeline flow-direction mixing pit 500
To mixed waste liquor (ammonia-nitrogen content 50.2mg/L), the pH to 11 that sodium hydroxide adjusts waste liquid is added, then through ultrafiltration apparatus 600
Ultrafiltration, ultrafiltrate are stored in ultrafiltrate storage tank 601.
S3. ultrafiltrate enters in the hollow fiber microporous membrane 701 in gaseous state membrane module 700 via waste liquid entrance 702
In blank pipe journey；Absorbing liquid in absorbing liquid reserve pool 80 enters in gaseous state membrane module 700 via absorbing liquid entrance 704, absorbing liquid
It is in opposite cross-flow passes with ultrafiltrate, the ammonia nitrogen vaporization in ultrafiltrate into absorbing liquid, reacts and produces ammonium salt solution.
Waste liquid after removal of ammonia and nitrogen is discharged via waste liquid outlet 703, and ammonium salt solution is flowed into ammonium salt storage tank 81 by taphole.
Wherein, absorbing liquid is the sulfuric acid solution of mass concentration 3%, and hollow fiber microporous membrane is polytetrafluoroethylene film, film wire
Outer diameter is 1.2mm, and internal diameter 0.8mm, 0.1 μm of aperture loads density 50%, effective length 100mm.According to flowmeter and temperature
The numerical value of meter, control valve take heating or cooling measure, and the flow velocity that control ultrafiltrate enters gaseous state membrane module is 2mL/s, temperature
Degree is 35 DEG C, and the flow velocity that absorbing liquid enters gaseous state membrane module is 2mL/s, and temperature is 50 DEG C.After ammonia nitrogen removal processing, sulfuric acid is obtained
The waste liquid that ammonium salt solution and ammonia-nitrogen content are 5.1mg/L, can be with direct emission.
S4. the ammonium sulfate in ammonium salt storage tank 81 is pumped into stripping by pump 102 after adding sodium hydroxide adjusts pH to 12
In the inlet tube 301 of tower 300, ammonia aeration is carried out, is then absorbed by absorption tower 400 and obtains ammonium chloride.
Embodiment 5
A kind for the treatment of process of ammonia nitrogen waste water, comprising the following steps:
S1. the high-concentration ammonia nitrogenous wastewater in waste water original pond I 100 is the ammonium paratungstate production process of ammonia-nitrogen content 5000mg/L
In cleaning APT waste water, flow in pretreatment pool 200 via pipeline, pretreated wastewater pH be 12, pump 102 effect
The lower inlet tube 301 into stripping tower 300 sprays waste water, waste water and stripping tower lower part are arranged and air blast by spray nozzle 306
The hot air of the connected discharge pipe blowout of machine 91, stripping ammonia, ammonia flow to absorption tower 400 by gas outlet 303, generate
Ammonium chloride.
Wherein, in pretreatment pool 200 pretreatment of high strength ammonia nitrogen waste method are as follows: sequentially added by feeding port 201
Composite decoloring agent and heavy metal chelating agent HMC-M1 are stirred 40 minutes with the revolving speed of 300r/min, obtain pretreated waste water.
The solid-liquid ratio g/mL of composite decoloring agent and high-concentration ammonia nitrogenous wastewater is 16:10000, and heavy metal chelating agent and ammonia nitrogen in high density are useless
The solid-liquid ratio g/mL of water is 3:10000；And composite decoloring agent be by calcium hydroxide, sodium hydroxide, active carbon and flyash according to
Weight ratio 3:2:3:2 is obtained by mixing.
S2. ammonia-nitrogen content is 88.5mg/L in stripping treated waste water, flows to mixing pit 500 through discharge port 304, is given up
For Low Concentration Ammonia Containing Wastewater (ammonia-nitrogen content is in 28.6mg/L) in water original pond II 101 by pipeline flow-direction mixing pit 500, stirring is mixed
Conjunction obtains mixed waste liquor (ammonia-nitrogen content 53.6mg/L), and the pH to 12 that sodium hydroxide adjusts waste liquid is added, then sets through ultrafiltration
Standby 600 ultrafiltration, ultrafiltrate are stored in ultrafiltrate storage tank 601.
S3. ultrafiltrate enters in the hollow fiber microporous membrane 701 in gaseous state membrane module 700 via waste liquid entrance 702
In blank pipe journey；Absorbing liquid in absorbing liquid reserve pool 80 enters in gaseous state membrane module 700 via absorbing liquid entrance 704, absorbing liquid
It is in opposite cross-flow passes with ultrafiltrate, the ammonia nitrogen vaporization in ultrafiltrate into absorbing liquid, reacts and produces ammonium salt solution.
Waste liquid after removal of ammonia and nitrogen is discharged via waste liquid outlet 703, and ammonium salt solution is flowed into ammonium salt storage tank 81 by taphole.
Wherein, absorbing liquid is the sulfuric acid solution of mass concentration 5%, and hollow fiber microporous membrane is polytetrafluoroethylene film, film wire
Outer diameter is 1.2mm, and internal diameter 0.8mm, 0.1 μm of aperture loads density 50%, effective length 100mm.According to flowmeter and temperature
The numerical value of meter, control valve take heating or cooling measure, and the flow velocity that control ultrafiltrate enters gaseous state membrane module is 3mL/s, temperature
Degree is 40 DEG C, and the flow velocity that absorbing liquid enters gaseous state membrane module is 4mL/s, and temperature is 56 DEG C.After ammonia nitrogen removal processing, sulfuric acid is obtained
The waste liquid that ammonium salt solution and ammonia-nitrogen content are 4.6mg/L, can be with direct emission.
S4. the ammonium sulfate in ammonium salt storage tank 81 is pumped into stripping by pump 102 after adding sodium hydroxide adjusts pH to 12
In the inlet tube 301 of tower 300, ammonia aeration is carried out, is then absorbed by absorption tower 400 and obtains ammonium chloride.
Embodiment 6
A kind for the treatment of process of ammonia nitrogen waste water, comprising the following steps:
S1. the high-concentration ammonia nitrogenous wastewater in waste water original pond I 100 is the condensation concentrated ammonia liquor of ammonia-nitrogen content 20000mg/L, via
Pipeline is flow in pretreatment pool 200, and pretreated wastewater pH is 13, and the feed liquor of stripping tower 300 is entered under the action of pumping 102
Pipe 301 sprays waste water by spray nozzle 306, and the discharge pipe that waste water was arranged with stripping tower lower part be connected with air blower 91 is blown out
Hot air, stripping ammonia, ammonia flows to absorption tower 400 by gas outlet 303, generates ammonium chloride.
Wherein, in pretreatment pool 200 pretreatment of high strength ammonia nitrogen waste method are as follows: sequentially added by feeding port 201
Composite decoloring agent and heavy metal chelating agent HMC-M1 are stirred 40 minutes with the revolving speed of 450r/min, obtain pretreated waste water.
The solid-liquid ratio g/mL of composite decoloring agent and high-concentration ammonia nitrogenous wastewater is 20:10000, and heavy metal chelating agent and ammonia nitrogen in high density are useless
The solid-liquid ratio g/mL of water is 3:10000；And composite decoloring agent be by calcium hydroxide, sodium hydroxide, active carbon and flyash according to
Weight ratio 4:2:3:2 is obtained by mixing.
S2. ammonia-nitrogen content is 125.5mg/L in stripping treated waste water, flows to mixing pit 500 through discharge port 304, is given up
For Low Concentration Ammonia Containing Wastewater (ammonia-nitrogen content is in 28.7mg/L) in water original pond II 101 by pipeline flow-direction mixing pit 500, stirring is mixed
Conjunction obtains mixed waste liquor (ammonia-nitrogen content 61.3mg/L), and the pH to 13 that sodium hydroxide adjusts waste liquid is added, then sets through ultrafiltration
Standby 600 ultrafiltration, ultrafiltrate are stored in ultrafiltrate storage tank 601.
S3. ultrafiltrate enters in the hollow fiber microporous membrane 701 in gaseous state membrane module 700 via waste liquid entrance 702
In blank pipe journey；Absorbing liquid in absorbing liquid reserve pool 80 enters in gaseous state membrane module 700 via absorbing liquid entrance 704, absorbing liquid
It is in opposite cross-flow passes with ultrafiltrate, the ammonia nitrogen vaporization in ultrafiltrate into absorbing liquid, reacts and produces ammonium salt solution.
Waste liquid after removal of ammonia and nitrogen is discharged via waste liquid outlet 703, and ammonium salt solution is flowed into ammonium salt storage tank 81 by taphole.
Wherein, absorbing liquid is the sulfuric acid solution of mass concentration 4%, and hollow fiber microporous membrane is polypropylene screen, film wire outer diameter
For 1.2mm, internal diameter 0.8mm, 0.1 μm of aperture loads density 50%, effective length 100mm.According to flowmeter and thermometer
Numerical value, control valve takes heating or cooling measure, and the flow velocity that control ultrafiltrate enters gaseous state membrane module is 5mL/s, temperature
It is 45 DEG C, the flow velocity that absorbing liquid enters gaseous state membrane module is 5mL/s, and temperature is 60 DEG C.After ammonia nitrogen removal processing, ammonium sulfate is obtained
The waste liquid that solution and ammonia-nitrogen content are 6.3mg/L, can be with direct emission.
S4. the ammonium sulfate in ammonium salt storage tank 81 is pumped into stripping by pump 102 after adding sodium hydroxide adjusts pH to 13
In the inlet tube 301 of tower 300, ammonia aeration is carried out, is then absorbed by absorption tower 400 and obtains ammonium chloride.
Embodiment 7
A kind for the treatment of process of ammonia nitrogen waste water, comprising the following steps:
S1. the high-concentration ammonia nitrogenous wastewater in waste water original pond I 100 is the waste water of ammonia-nitrogen content 1000mg/L, via pipeline stream
To pretreatment pool 200, pretreated wastewater pH is 11, and the inlet tube 301 of stripping tower 300 is entered under the action of pumping 102,
Waste water is sprayed by spray nozzle 306, the hot sky that the discharge pipe that waste water be arranged with stripping tower lower part be connected with air blower 91 is blown out
Gas contact, stripping ammonia, ammonia flow to absorption tower 400 by gas outlet 303, generate ammonium chloride.
Wherein, in pretreatment pool 200 pretreatment of high strength ammonia nitrogen waste method are as follows: sequentially added by feeding port 201
Composite decoloring agent and heavy metal chelating agent HMC-M1 are stirred 30 minutes with the revolving speed of 500r/min, obtain pretreated waste water.
The solid-liquid ratio g/mL of composite decoloring agent and high-concentration ammonia nitrogenous wastewater is 11:10000, and heavy metal chelating agent and ammonia nitrogen in high density are useless
The solid-liquid ratio g/mL of water is 2.6:10000；And composite decoloring agent be by calcium hydroxide, sodium hydroxide, active carbon and flyash by
It is obtained by mixing according to weight ratio 4:2:3:1.5.
S2. ammonia-nitrogen content is 66.8mg/L in stripping treated waste water, flows to mixing pit 500 through discharge port 304, is given up
For Low Concentration Ammonia Containing Wastewater (ammonia-nitrogen content is in 23.4mg/L) in water original pond II 101 by pipeline flow-direction mixing pit 500, stirring is mixed
Conjunction obtains mixed waste liquor (ammonia-nitrogen content 50mg/L), and the pH to 11.5 that calcium hydroxide adjusts waste liquid is added, then sets through ultrafiltration
Standby 600 ultrafiltration, ultrafiltrate are stored in ultrafiltrate storage tank 601.
S3. ultrafiltrate enters in the hollow fiber microporous membrane 701 in gaseous state membrane module 700 via waste liquid entrance 702
In blank pipe journey；Absorbing liquid in absorbing liquid reserve pool 80 enters in gaseous state membrane module 700 via absorbing liquid entrance 704, absorbing liquid
It is in opposite cross-flow passes with ultrafiltrate, the ammonia nitrogen vaporization in ultrafiltrate into absorbing liquid, reacts and produces ammonium salt solution.
Waste liquid after removal of ammonia and nitrogen is discharged via waste liquid outlet 703, and ammonium salt solution is flowed into ammonium salt storage tank 81 by taphole.
Wherein, absorbing liquid is the phosphoric acid solution of mass concentration 5%, and hollow fiber microporous membrane is polypropylene screen, film wire outer diameter
For 1.2mm, internal diameter 0.8mm, 0.1 μm of aperture loads density 50%, effective length 100mm.According to flowmeter and thermometer
Numerical value, control valve takes heating or cooling measure, and the flow velocity that control ultrafiltrate enters gaseous state membrane module is 5mL/s, temperature
It is 40 DEG C, the flow velocity that absorbing liquid enters gaseous state membrane module is 6mL/s, and temperature is 55 DEG C.After ammonia nitrogen removal processing, ammonium phosphate is obtained
The waste liquid that solution and ammonia-nitrogen content are 5.2mg/L, can be with direct emission.
S4. the ammonium phosphate solution in ammonium salt storage tank 81 is pumped into stripping by pump 102 after adding sodium hydroxide adjusts pH to 11
In the inlet tube 301 of tower 300, ammonia aeration is carried out, is then absorbed by absorption tower 400 and obtains ammonium chloride.
Comparative example 1
The difference of this comparative example and embodiment 4 is that high-concentration ammonia nitrogenous wastewater does not pass through pre-treatment step, is directly entered
Stripping tower carries out ammonia aeration, remaining is the same as embodiment 4.As a result, ammonia-nitrogen content is 1168.7mg/L, gas in stripping treated waste water
Ammonia-nitrogen content is 486.5mg/L in waste liquid after state film process, does not meet discharge standard.Moreover, not pretreated high concentration
Contain heavy metal and other suspended impurities in ammonia nitrogen waste water, be easy to cause the packing layer in stripping tower to block, influence stripping tower
Service life.
Comparative example 2
The difference of this comparative example and embodiment 5 is, replaces composite decoloring agent using active carbon in preprocessing process, remaining
With embodiment 5.As a result, ammonia-nitrogen content is 368.2mg/L in stripping treated waste water, ammonia nitrogen in gas film treated waste liquid
Content is 189.7mg/L, does not meet discharge standard.
Comparative example 3
The difference of this comparative example and embodiment 5 is, replaces composite decoloring agent using flyash in preprocessing process, remaining
With embodiment 5.As a result, ammonia-nitrogen content is 413.8mg/L in stripping treated waste water, ammonia nitrogen in gas film treated waste liquid
Content is 205.6mg/L, does not meet discharge standard.
Comparative example 4
The difference of this comparative example and embodiment 5 is that, without addition heavy metal chelating agent in preprocessing process, remaining is the same as real
Apply example 5.As a result, ammonia-nitrogen content is 166.5mg/L in stripping treated waste water, ammonia-nitrogen content in gas film treated waste liquid
For 58.7mg/L, discharge standard is not met.Heavy metal chelating agent not only influences the content of beary metal in waste liquid, also will affect stripping
The stripping efficiency of tower, causes the ammonia-nitrogen content in final waste liquid exceeded.
Comparative example 5
The difference of this comparative example and embodiment 5 is that high-concentration ammonia nitrogenous wastewater is pre-processed using the identical method of embodiment 5
Afterwards, it without stripping, is directly entered mixing pit and is mixed with Low Concentration Ammonia Containing Wastewater, obtain waste liquid, remaining is the same as embodiment 5.As a result,
Ammonia-nitrogen content is 62.3mg/L in the waste liquid of discharge, does not meet discharge standard.In addition, high-concentration ammonia nitrogenous wastewater directlys adopt gaseous state
Embrane method deamination, very big to the loss of gas film, the required acid liquid measure that absorbs is very big, at high cost.
Comparative example 6
The difference of this comparative example and embodiment 5 is that the flow velocity that the waste liquid after ultrafiltration enters gaseous state membrane module is 6mL/s,
Temperature is 50 DEG C, and the flow velocity that sulfuric acid absorption liquid carries out gaseous state membrane module is 4mL/s, and temperature 50 C, remaining is the same as embodiment 5.As a result,
Ammonia-nitrogen content is 30.9mg/L in treated waste liquid, does not meet discharge standard.
After the process processing waste water that embodiment 1 and embodiment 2 are addressed in Chinese patent CN106186492A, in waste water
Ammonia-nitrogen content be down to 28.10mg/L and 52.80mg/L respectively, do not meet discharge standard.
To sum up, ammonia nitrogen wastewater treatment device provided by the utility model can apply to high concentration and the ammonia nitrogen of low concentration is useless
Water, each equipment cooperate, and simplify operating procedure, so that ammonia-nitrogen content meets discharge standard in treated waste water, and by ammonia
Nitrogen is converted into recycling ammonium chloride, is conducive to industrial applications.
The preferable specific embodiment of the above, only the utility model, but the protection scope of the utility model is not
It is confined to this, anyone skilled in the art within the technical scope disclosed by the utility model, can readily occur in
Change or replacement, should be covered within the scope of the utility model.
Claims (6)
1. a kind of processing unit of ammonia nitrogen waste water, which is characterized in that including waste water original pond I (100), waste water original pond II (101), pre-
Processing pond (200), stripping tower (300), absorption tower (400), mixing pit (500), ultrafiltration apparatus (600), ultrafiltrate storage tank
(601), gaseous state membrane module (700), absorbing liquid reserve pool (80) and ammonium salt storage tank (81), wherein
Waste water original pond I (100) is connected by pipeline with pretreatment pool (200), pretreatment pool (200) treated waste water
It is flowed through pump (102) by pipeline, then flow to the inlet tube (301) on stripping tower (300) top, the inlet tube by pipeline
(301) lower end is equipped with spray nozzle (306)；The top of the stripping tower (300) is equipped with gas outlet (303), and bottom is equipped with discharging
Mouth (304), lower sides connect air blower (91) through ventilation duct, one end of ventilation duct is connected with, and the other end is positioned at stripping
Air outlet (305) in tower (300)；
The gas outlet (303) is connected by pipeline with the air inlet (401) on absorption tower (400), the absorption tower (400)
Upper portion side wall is located at one section of absorption tower (400) inside equipped with atomizer through fluid-through tube, the fluid-through tube is connected with
(403), the other end of other end connection pump (103), pump (103) connects hydrochloric acid tank (9)；
The discharge port (304) and waste water original pond II (101) are connected by pipeline with the entrance of mixing pit (500) respectively, are mixed
The outlet in pond (500) is connected by pipeline with the entrance of ultrafiltration apparatus (600), the outlet of ultrafiltration apparatus (600) pass through pipeline and
Ultrafiltrate storage tank (601) is connected；
The ultrafiltrate storage tank (601) is connected by pipeline with the waste liquid entrance (702) on gaseous state membrane module (700) shell, institute
It states and is equipped with several hollow fiber microporous membranes (701) inside gaseous state membrane module (700), horizontal direction and waste liquid entrance (702) are opposite
Shell be equipped with waste liquid outlet (703), waste liquid flows through in the hollow tube side of hollow fiber microporous membrane (701), with waste liquid outlet
(703) ipsilateral shell is equipped with absorbing liquid entrance (704), is equipped with taphole with the ipsilateral shell of waste liquid entrance (702),
The taphole is connected through pipeline with ammonium salt storage tank (81), and ammonium salt storage tank (81) is connected by pipeline with pump (102)；
The absorbing liquid entrance (704) is connected by pipeline with absorbing liquid reserve pool (80).
2. the processing unit of ammonia nitrogen waste water according to claim 1, which is characterized in that be located at spray in the stripping tower (300)
The lower part for drenching mouth (306) is equipped with filled layer (302)；Lower part in the absorption tower (400) positioned at atomizer (403) is equipped with slow
Rush layer (402).
3. the processing unit of ammonia nitrogen waste water according to claim 1, which is characterized in that further include in following technical characteristic extremely
Few one kind:
Thermometer I (602) is equipped in the ultrafiltrate storage tank (601)；
Thermometer II (801) is equipped in the absorbing liquid reserve pool (80).
4. the processing unit of ammonia nitrogen waste water according to claim 1, which is characterized in that further include in following technical characteristic extremely
Few one kind:
PH meter I (811) is equipped in the ammonium salt storage tank (81)；
PH meter II (502) is equipped in the mixing pit (500).
5. the processing unit of ammonia nitrogen waste water according to claim 4, which is characterized in that further include following technical characteristic:
Pipeline between the ultrafiltrate storage tank (601) and waste liquid entrance (702) is equipped with valve I (603) and temperature indicator I
(605), the valve I (603) is close to the outlet of ultrafiltrate storage tank (601), and temperature indicator I (605) is close to waste liquid entrance
(702)；
Pipeline between the absorbing liquid reserve pool (80) and absorbing liquid entrance (704) is equipped with valve II (802) and temperature is aobvious
Show device II (804), the valve II (802) is close to the outlet of absorbing liquid reserve pool (80), and temperature indicator II (804) is close to suction
It receives liquid entrance (704).
6. the processing unit of ammonia nitrogen waste water according to claim 5, which is characterized in that the valve I (603) and temperature display
Flow meter I (604) are additionally provided on pipeline between device I (605)；Between the valve II (802) and temperature indicator II (804)
Pipeline on be additionally provided with flow meter II (803).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109231572A (en) * | 2018-10-29 | 2019-01-18 | 江西铜鼓有色冶金化工有限责任公司 | A kind of processing system and technique of ammonia nitrogen waste water |
| CN113880314A (en) * | 2021-11-10 | 2022-01-04 | 广东工业大学 | Treatment method and treatment system for obtaining ammonia water from ammonia nitrogen wastewater |
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2018
- 2018-10-29 CN CN201821759030.0U patent/CN209242811U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109231572A (en) * | 2018-10-29 | 2019-01-18 | 江西铜鼓有色冶金化工有限责任公司 | A kind of processing system and technique of ammonia nitrogen waste water |
| CN109231572B (en) * | 2018-10-29 | 2024-04-19 | 江西铜鼓有色冶金化工有限责任公司 | Ammonia nitrogen wastewater treatment system and process |
| CN113880314A (en) * | 2021-11-10 | 2022-01-04 | 广东工业大学 | Treatment method and treatment system for obtaining ammonia water from ammonia nitrogen wastewater |
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