CN205313302U - Ammonia nitrogen wastewater resourceful treatment system - Google Patents
Ammonia nitrogen wastewater resourceful treatment system Download PDFInfo
- Publication number
- CN205313302U CN205313302U CN201521116078.6U CN201521116078U CN205313302U CN 205313302 U CN205313302 U CN 205313302U CN 201521116078 U CN201521116078 U CN 201521116078U CN 205313302 U CN205313302 U CN 205313302U
- Authority
- CN
- China
- Prior art keywords
- tank
- waste water
- ammonia nitrogen
- outlet
- import
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn - After Issue
Links
Landscapes
- Water Treatment By Sorption (AREA)
Abstract
The utility model discloses an ammonia nitrogen wastewater resourceful treatment system, ammonia nitrogen wastewater resourceful treatment system includes the consecutive catch basin that connects, buffer pool, regulation cauldron, first buffer tank, MVR vaporization system, regulation jar, adsorption system, second buffer tank, deamination nitrogen system, catch basin, buffer pool, regulation cauldron, first buffer tank, MVR vaporization system, regulation jar, adsorption system, second buffer tank, deamination nitrogen system all are provided with import and export, the utility model discloses preprocessing device is succinct, and area is little, convenient operation, and the operational environment health, purifying effect is good, and no secondary pollution admittedly useless output is little, can retrieve the ammonia nitrogen resource in the waste water with the form of ammonium salt is high -efficient, but the system goes out water reuse of reclaimed water.
Description
Technical field
This utility model relates to brine waste process field, is specifically related to a kind of ammonia nitrogen waste water recycling treatment system.
Background technology
China is as new industry big country, the industrial wastewater produced is of a great variety, and the scale of construction is huge, and the discharge watershed environment of waste water and residents ' health cause and have a strong impact on, the wherein directly discharge of high ammonia-nitrogen wastewater, the ecological environment of locality can be destroyed, cause the eutrophication in residing waters, cause the death of a large amount of fish and shrimp, and waste valuable ammonia nitrogen, so during to this kind of waste water treatment, not only making discharged wastewater met the national standard, also needing to carry out the recovery of ammonia nitrogen resource.
Current ammonia nitrogen waste water treatment method mainly has blow-off method, vaporizing extract process, membrane separation process, biochemical process, and evaporation technique. Blow-off method needs to add substantial amounts of alkali liquor and regulates pH value of waste water, and can produce secondary pollution in process; Vaporizing extract process energy consumption is high, and the ammonia difficult quality of recovery reaches requirement; Biochemical process is difficult to directly process high-concentration ammonia nitrogenous wastewater, and floor space is big, once puts into height; Membrane separation process has obtained a degree of popularization as the ammonia nitrogen removal technology that several years rise, but membrane module price is still high, inflow requirement is extremely strict, and required pretreatment process is loaded down with trivial details, thus limiting it to process the large-scale use in engineering at ammonia nitrogen waste water; The problems such as the salinity in waste water can effectively be isolated by traditional evaporation technique, but it is big to there is energy consumption, and efficiency is low and cost for wastewater treatment is high,
MVR evaporation technique is low because of its energy consumption, processes high-salt wastewater technical advantage obvious, is more and more applied in brine waste process, and this method can avoid the drawback of tradition evaporation technique. Due to industrial wastewater complicated component, the content of Organic substance and salt is high, it is directly entered MVR vapo(u)rization system if not preprocessed, vaporizer long-play, Organic substance is easily enriched with, it is easy to causes the coking of evaporator heat exchange tubulation to stick with paste pipe, causes that vaporizer stops, affect the properly functioning of enterprise's production, so waste water needs waste water is carried out materialized pretreatment before entering vaporizer.
Before vaporizer traditional at present, preconditioning technique is to carry out iron-carbon micro-electrolysis and Fenton oxidation after waste water regulates pH value, remove the COD in waste water, again through flocculation sediment effect, the iron ion in waste water is made to remove with the form of iron cement, reducing organic content in waste water further, water outlet enters vaporizer after regulating pH value and processes simultaneously.This flow process can effectively reduce vaporizer longtime running and cause sticking with paste the probability of pipe, but has the disadvantage that: (1) pretreatment process is long, must regulate pH value frequently, increase manipulation strength; (2) iron-carbon micro-electrolysis process pH value constantly becomes big, simultaneously need to certain aeration, so causing the loss of ammonia nitrogen in ammonium salt-containing waste water, making the ammonium salt total nitrogen content of recovery decline, and the effusion of ammonia can cause the secondary pollution of surrounding; (3) waste water is through being all sequentially carried out iron-carbon micro-electrolysis and Fenton oxidation with after water quality adjustment pH value, and owing to the COD of waste water is relatively big, the load of pretreatment is big, so the yield of iron cement is big, ferrum carbon and hydrogen peroxide consumption big, operating cost is high.
Utility model content
For solving the problems referred to above, the purpose of this utility model is to provide a kind of white ammonium salt that can obtain high total nitrogen content from ammonia nitrogen waste water, and solid waste yield is few and water outlet can the ammonia nitrogen waste water recycling treatment system of reuse.
For realizing above-mentioned technical purpose, the technical solution adopted in the utility model is as follows: a kind of ammonia nitrogen waste water recycling treatment system of the present utility model, and described ammonia nitrogen waste water recycling treatment system includes collecting-tank, Buffer Pool, adjustment still, the first surge tank, MVR vapo(u)rization system, regulates tank, adsorption system, the second surge tank, ammonia nitrogen removal system; Described collecting-tank, Buffer Pool, adjustment still, the first surge tank, MVR vapo(u)rization system, adjustment tank, adsorption system, the second surge tank, ammonia nitrogen removal system are provided with inlet and outlet;
The outlet of described collecting-tank is connected with the import of Buffer Pool, the outlet of described Buffer Pool is connected with the import regulating still, the outlet of described adjustment still is connected with the import of the first surge tank, the outlet of described first surge tank is connected with the import of MVR vapo(u)rization system, the outlet of described MVR vapo(u)rization system is connected with the import regulating tank, the described outlet of adjustment tank is connected with the import of adsorption system, the outlet of described adsorption system is connected with the import of the second surge tank, and the outlet of described second surge tank is connected with the import of ammonia nitrogen removal system.
Further, the front portion of described collecting-tank is provided with grid device; Described grid device includes coarse rack and fine fack,
The grid gap of coarse rack is 20-30mm, and the outlet of coarse rack is connected with the import of fine fack by pipeline, and the grid gap of fine fack is 5-10mm, and the outlet of fine fack is connected with pipeline collecting-tank;
Being provided with aerating system, the first stirring system and effusion meter in described collecting-tank, described aerating system includes aeration head and aeration air compressor, and described aeration head is arranged at the bottom of the pond of collecting-tank; Described first stirring system includes stirring paddle and motor,
The top of described collecting-tank is provided with porous plate, described first stirring system is arranged on the porous plate on top of collecting-tank, described aerating system is connected with effusion meter, and described effusion meter is connected with aeration air compressor, and described aeration air compressor is arranged on the outside of collecting-tank.
Further, the pond Bottom Shape of described Buffer Pool is taper, is removed less float and impurity by precipitation; PH value of waste water in described adjustment still is adjusted to 5-6.5, and waste water is 30-120min in the time of staying regulated in still; Being provided with anti-coking agent in described adjustment still, described anti-coking agent quality is the 0.1-0.5% of wastewater quality.
Further; described anti-coking agent is sodium dithionite, thiourea dioxide, Methyl disulfide, sodium sulfide or sodium borohydride; the adsorbent added in described adjustment still is powdered activated carbon or granular active carbon, and described quality of activated carbon is the 0.02-1.5% of wastewater quality.
Further, described adjustment tank being provided with acid solution automatic medicament feeding system and the second stirring system, the pH value of waste water in described adjustment tank is adjusted to 3-5.
Further, described acid solution automatic medicament feeding system includes liquor box, the agitator tank of belt stirrer, liquidometer, dosing pump, electric cabinet and effusion meter; Described liquor box, the agitator tank of belt stirrer, liquidometer, dosing pump, electric cabinet and effusion meter are provided with import and outlet;
The outlet of described agitator tank is connected with the import of liquor box by pipeline, and the outlet of described liquor box is connected with the import regulating tank by dosing pump, and described metering delivery side of pump is connected with the import of effusion meter; The stir speed (S.S.) of the second stirring system is at 300-550r/min.
Further, being provided with macroporous adsorbent resin in described adsorption system, the saturated adsorption volume of resin is 65-100 times of resin volume.
Further, in described ammonia nitrogen removal system, it is provided with acid cation exchange resin, 55-260 times that saturated adsorption volume is resin volume of resin.
Beneficial effect: this utility model pretreatment unit is succinct, floor space is little, easy to operate, working environment health, good purification, non-secondary pollution, solid waste yield is little, can by the form high efficiente callback with ammonium salt of the ammonia nitrogen resource in waste water, and system water outlet meets process water reuse standard, save the water resource of preciousness, adequately achieved recycling of waste water, there is good environment and economic benefit.
Accompanying drawing explanation
Fig. 1 is flow chart of the present utility model;
Wherein: 1 collecting-tank, 2 Buffer Pools, 3 adjustment stills, 4 first surge tanks, 5MVR vapo(u)rization system, 6 adjustment tank, 7 adsorption systems, 8 second surge tanks, 9 ammonia nitrogen removal systems.
Detailed description of the invention
Following by specific embodiment, this utility model done further specific descriptions, but be not to be construed as the restriction to this utility model protection domain.
Embodiment 1
A kind of ammonia nitrogen waste water recycling treatment system of the present utility model, described ammonia nitrogen waste water recycling treatment system includes collecting-tank 1, Buffer Pool 2, adjustment still the 3, first surge tank 4, MVR vapo(u)rization system 5, regulates tank 6, adsorption system the 7, second surge tank 8, ammonia nitrogen removal system 9; Described collecting-tank 1, Buffer Pool 2, adjustment still the 3, first surge tank 4, MVR vapo(u)rization system 5, adjustment tank 6, adsorption system the 7, second surge tank 8, ammonia nitrogen removal system 9 are provided with inlet and outlet;
The outlet of described collecting-tank 1 is connected with the import of Buffer Pool 2, the outlet of described Buffer Pool 2 is connected with the import regulating still 3, the outlet of described adjustment still 3 is connected with the import of the first surge tank 4, the outlet of described first surge tank 4 is connected with the import of MVR vapo(u)rization system 5, the outlet of described MVR vapo(u)rization system 5 is connected with the import regulating tank 6, the outlet of described adjustment tank 6 is connected with the import of adsorption system 7, the outlet of described adsorption system 7 is connected with the import of the second surge tank 8, the described outlet of the second surge tank 8 is connected with the import of ammonia nitrogen removal system 9.
The front portion of described collecting-tank 1 is provided with grid device; Described grid device includes coarse rack and fine fack, and the grid gap of coarse rack is 20mm, retains bigger float, and the outlet of coarse rack is connected with the import of fine fack by pipeline, and the grid gap of fine fack is 5mm, and the outlet of fine fack is connected with pipeline collecting-tank;
Being provided with aerating system, the first stirring system and effusion meter in described collecting-tank 1, described aerating system includes aeration head and aeration air compressor, and described aeration head is arranged at the bottom of the pond of collecting-tank 1;Described first stirring system includes stirring paddle and motor,
The top of described collecting-tank 1 is provided with porous plate, described first stirring system is arranged on the porous plate on top of collecting-tank 1, described aerating system is connected with effusion meter, and described effusion meter is connected with aeration air compressor, and described aeration air compressor is arranged on the outside of collecting-tank. Formed aeration agitation by motor and stirring paddle to work simultaneously.
The pond Bottom Shape of described Buffer Pool 2 is taper, is beneficial to collection particulate matter.
Described adjustment still 3 to be equipped with soda acid automatic medicament feeding system and the first stirring system, pH value of waste water is 6.5, waste water is 30min in the time of staying regulated in still 3, it is provided with sodium dithionite in described adjustment still 3, the quality of affiliated sodium dithionite is the 0.1% of wastewater quality, adsorbent is powdered activated carbon, and described quality of activated carbon is the 0.02% of wastewater quality;
Being provided with acid solution automatic medicament feeding system and the second stirring system on described adjustment tank 6, the pH value of waste water in described adjustment tank 6 is adjusted to 3. The stir speed (S.S.) of the second stirring system is at 300r/min.
Described acid solution automatic medicament feeding system includes liquor box, the agitator tank of belt stirrer, liquidometer, dosing pump, electric cabinet and effusion meter; Described liquor box, the agitator tank of belt stirrer, liquidometer, dosing pump, electric cabinet and effusion meter are provided with import and outlet;
The outlet of described agitator tank is connected with the import of liquor box by pipeline, according to required acid strength, configure in agitator tank, acid solution is flowed into the entrance of liquor box by the outlet at the end of agitator tank by pipeline, the outlet of described liquor box is connected with the import regulating tank 6 by dosing pump, and described metering delivery side of pump is connected with the import of effusion meter; Described adjustment tank 6 upper end is provided with the second stirring system, and described second stirring system includes stirring paddle and motor, regulates mixing speed by motor speed.
Being provided with macroporous adsorbent resin in described adsorption system 7, the saturated adsorption volume of resin is 65 times of resin volume. It is provided with acid cation exchange resin, saturated adsorption volume is resin volume 55 times of resin in described adsorption system 7.
The water quality of the front and back that the waste water of embodiment 1 is entered each system is analyzed, and draws the situation of change of COD and ammonia nitrogen concentration in wastewater treatment process, and waste water COD result is as shown in table 1, and ammonia nitrogen in waste water result is as shown in table 2.
Table 1
Table 2
As shown in Table 1 and Table 2, one waste water in dye production flows into collecting-tank 1, waste water and balanced water quality and quantity is stored in pond, waste water is in harmonious proportion water quality by the 1 entrance Buffer Pool 2 that catchments, waste water after Buffer Pool 2, its COD is dropped to 3850mg/L by 4200mg/L, and the ammonia-nitrogen content of waste water is dropped to 528mg/L by 540mg/L; Waste water after overregulating still 3, its COD is dropped to 3640mg/L by 3850mg/L, and ammonia-nitrogen content is dropped to 492mg/L by 528mg/L; Waste water is after MVR vapo(u)rization system processes, and waste water COD is dropped to 430mg/L by the 3640mg/L before evaporating, and ammonia-nitrogen content is dropped to 97mg/L, water outlet COD and the ammonia nitrogen concentration discharge standard higher than waste water by 492mg/L, in addition it is also necessary to further process; After adsorption system 7, the COD of waste water is dropped to 100mg/L by 430mg/L, and ammonia-nitrogen content is dropped to 92mg/L by 97mg/L; After ammonia nitrogen removal system 9, the COD of waste water is dropped to 92mg/L by 100mg/L, and ammonia-nitrogen content is dropped to 20mg/L by 92mg/L.By the ammonium salt obtained is detected, it is determined that the total nitrogen content of ammonium salt is 13.9%, colours white, it is contemplated that the ammonium salt of acquisition has certain economic worth, ammonia nitrogen waste water reclaims with the form of ammonium salt has considerable economic benefit.
Embodiment 2
Embodiment 2 and embodiment 1 are distinctive in that: the front portion of described collecting-tank 1 is provided with grid device; Described grid device includes coarse rack and fine fack, and the grid gap of coarse rack is 25mm, retains bigger float, and the outlet of coarse rack is connected with the import of fine fack by pipeline, and the grid gap of fine fack is 8mm, and the outlet of fine fack is connected 1 with pipeline collecting-tank;
Described adjustment still 3 regulates pH value of waste water to 6 in whipping process; Waste water time of staying in regulating still 3 is 80min, still is initially charged thiourea dioxide, addition quality is wastewater quality the 0.3% of thiourea dioxide, it is subsequently adding adsorbent powder shaped activated carbon, it is the 0.8% of wastewater quality that activated carbon adds quality, anti-coking agent suppresses the aromatic series Organic substance in waste water to occur oxidative polymerization to produce tarry matters under the high temperature conditions, the Organic substance in waste water is removed in activated carbon adsorption, thus avoiding MVR vapo(u)rization system 5 longtime running to cause the appearance of heat exchanger components coking situation, it is ensured that the stable operation of vaporizer;
Being provided with acid solution automatic medicament feeding system and the second stirring system on described adjustment tank 6, the pH value of waste water in described adjustment tank is adjusted to 4. The stir speed (S.S.) of the second stirring system is at 450r/min.
Described acid solution automatic medicament feeding system includes liquor box, the agitator tank of belt stirrer, liquidometer, dosing pump, electric cabinet and effusion meter; Described liquor box, the agitator tank of belt stirrer, liquidometer, dosing pump, electric cabinet and effusion meter are provided with import and outlet;
The outlet of described agitator tank is connected with the import of liquor box by pipeline, and the outlet of described liquor box is connected with the import regulating tank 6 by dosing pump, and described metering delivery side of pump is connected with the import of effusion meter; Described adjustment tank upper end is provided with the second stirring system, and described second stirring system includes stirring paddle and motor, regulates mixing speed by motor speed.
Being provided with macroporous adsorbent resin in described adsorption system 7, the saturated adsorption volume of resin is 90 times of resin volume.
It is provided with acid cation exchange resin, saturated adsorption volume is resin volume 110 times of resin in described adsorption system 7.
The water quality of the front and back that the waste water of embodiment 2 is entered each system is analyzed, and draws the situation of change of COD and ammonia nitrogen concentration in wastewater treatment process, and waste water COD result is as shown in table 3, and ammonia nitrogen in waste water result is as shown in table 4,
Table 3
Table 4
As shown in Table 3 and Table 4, one chemical production wastewater flows into collecting-tank 1, waste water and balanced water quality and quantity is stored in pond, waste water is entered Buffer Pool 2 by collecting-tank 1 and is in harmonious proportion water quality, waste water after Buffer Pool 2, its COD is dropped to 10200mg/L by 11500mg/L, and the ammonia-nitrogen content of waste water is dropped to 9100mg/L by 9900mg/L; Waste water after overregulating still 3, its COD is dropped to 9030mg/L by 10200mg/L, and ammonia-nitrogen content is dropped to 8220mg/L by 9100mg/L; Waste water is after MVR vapo(u)rization system 5 processes, and waste water COD is dropped to 1275mg/L by the 9030mg/L before evaporating, and ammonia-nitrogen content is dropped to 420mg/L, water outlet COD and the ammonia nitrogen concentration discharge standard higher than waste water by 8220mg/L, in addition it is also necessary to further process;After adsorption system 7, the COD of waste water is dropped to 100mg/L by 1275mg/L, and ammonia-nitrogen content is dropped to 395mg/L by 420mg/L; After ammonia nitrogen removal system 9, the COD of waste water is dropped to 91mg/L by 100mg/L, and ammonia-nitrogen content is dropped to 20mg/L by 395mg/L. By the ammonium salt obtained is detected, it is determined that the total nitrogen content of ammonium salt is 17.1%, colours white, it is contemplated that the ammonium salt of acquisition has certain economic worth, ammonia nitrogen waste water reclaims with the form of ammonium salt has considerable economic benefit.
Embodiment 3
Embodiment 3 and embodiment 1 are distinctive in that: the front portion of described collecting-tank 1 is provided with grid device; Described grid device includes coarse rack and fine fack, the grid gap of coarse rack is 30mm, retains bigger float, and the outlet of coarse rack is connected with the import of fine fack by pipeline, the grid gap of fine fack is 10mm, and the outlet of fine fack is connected 1 with pipeline collecting-tank;
Described adjustment still 3 is at stirring and adjusting pH value of waste water to 5, retention time of sewage is 30min, still is initially charged Methyl disulfide, addition quality is wastewater quality the 0.5% of Methyl disulfide, it is subsequently adding adsorbent powder shaped activated carbon, it is wastewater quality 1.5% that activated carbon adds quality, the aromatic series Organic substance in waste water is suppressed to occur oxidative polymerization to produce tarry matters under the high temperature conditions in anti-coking agent, the Organic substance in waste water is removed in activated carbon adsorption, thus avoiding MVR vapo(u)rization system 5 longtime running to cause the appearance of heat exchanger components coking situation, ensure the stable operation of vaporizer.
Being provided with acid solution automatic medicament feeding system and the second stirring system on described adjustment tank 6, the pH value of waste water in described adjustment tank 6 is adjusted to 5.
Described acid solution automatic medicament feeding system includes liquor box, the agitator tank of belt stirrer, liquidometer, dosing pump, electric cabinet and effusion meter; Described liquor box, the agitator tank of belt stirrer, liquidometer, dosing pump, electric cabinet and effusion meter are provided with import and outlet;
The outlet of described agitator tank is connected with the import of liquor box by pipeline, and the outlet of described liquor box is connected with the import regulating tank 6 by dosing pump, and described metering delivery side of pump is connected with the import of effusion meter; Described adjustment tank 6 upper end is provided with the second stirring system, and described second stirring system includes stirring paddle and motor, regulates mixing speed by motor speed, and the stir speed (S.S.) of the second stirring system is at 550r/min.
Being provided with macroporous adsorbent resin in described adsorption system 7, the saturated adsorption volume of resin is 100 times of resin volume.
It is provided with acid cation exchange resin, saturated adsorption volume is resin volume 260 times of resin in described adsorption system 7.
The water quality of the front and back that the waste water of embodiment 3 is entered each system is analyzed, and draws the situation of change of COD and ammonia nitrogen concentration in wastewater treatment process, and waste water COD result is as shown in table 5, and ammonia nitrogen in waste water result is as shown in table 6.
Table 5
Table 6
As shown in table 5 and table 6, one chemical production wastewater flows into collecting-tank 1, waste water and balanced water quality and quantity is stored in pond, waste water is entered Buffer Pool 2 by collecting-tank and is in harmonious proportion water quality, waste water after Buffer Pool 2, its COD is dropped to 22100mg/L by 23500mg/L, and the ammonia-nitrogen content of waste water is dropped to 14820mg/L by 15750mg/L; Waste water after overregulating still, its COD is dropped to 18450mg/L by 22100mg/L, and ammonia-nitrogen content is dropped to 13310mg/L by 14820mg/L;Waste water is after MVR vapo(u)rization system 5 processes, and waste water COD is dropped to 2100mg/L by the 18450mg/L before evaporating, and ammonia-nitrogen content is dropped to 790mg/L, water outlet COD and the ammonia nitrogen concentration discharge standard higher than waste water by 13310mg/L, in addition it is also necessary to further process; After adsorption system 7, the COD of waste water is dropped to 100mg/L by 2100mg/L, and ammonia-nitrogen content is dropped to 766mg/L by 790mg/L; After ammonia nitrogen removal system 9, the COD of waste water is dropped to 93mg/L by 100mg/L, and ammonia-nitrogen content is dropped to 20mg/L by 766mg/L. By the ammonium salt obtained is detected, it is determined that the total nitrogen content of ammonium salt is 18.5%, colours white, it is contemplated that the ammonium salt of acquisition has certain economic worth, ammonia nitrogen waste water reclaims with the form of ammonium salt has considerable economic benefit.
Embodiment 4
Embodiment 4 and embodiment 1 are distinctive in that:
Described anti-coking agent is sodium sulfide.
Embodiment 5
Embodiment 5 and embodiment 1 are distinctive in that: described anti-coking agent is sodium borohydride.
Although more employing collecting-tank 1, Buffer Pool 2, adjustment still the 3, first surge tank 4, MVR vapo(u)rization system 5 herein, regulating the terms such as tank 6, adsorption system the 7, second surge tank 8, ammonia nitrogen removal system 9, but it is not precluded from using the probability of other term. These terms are used to be only used to describe and explain essence of the present utility model more easily; It is all contrary with this utility model spirit for being construed as any additional restriction.
Of the present utility model ultimate principle, principal character and of the present utility model advantage have more than been shown and described. Skilled person will appreciate that of the industry; this utility model is not restricted to the described embodiments; described in above-described embodiment and description is that principle of the present utility model is described; under the premise without departing from this utility model spirit and scope; this utility model also has various changes and modifications, and this utility model claims scope and defined by appending claims, description and equivalent thereof.
Claims (8)
1. an ammonia nitrogen waste water recycling treatment system, it is characterised in that: described ammonia nitrogen waste water recycling treatment system includes collecting-tank, Buffer Pool, adjustment still, the first surge tank, MVR vapo(u)rization system, regulates tank, adsorption system, the second surge tank, ammonia nitrogen removal system; Described collecting-tank, Buffer Pool, adjustment still, the first surge tank, MVR vapo(u)rization system, adjustment tank, adsorption system, the second surge tank, ammonia nitrogen removal system are provided with inlet and outlet;
The outlet of described collecting-tank is connected with the import of Buffer Pool, the outlet of described Buffer Pool is connected with the import regulating still, the outlet of described adjustment still is connected with the import of the first surge tank, the outlet of described first surge tank is connected with the import of MVR vapo(u)rization system, the outlet of described MVR vapo(u)rization system is connected with the import regulating tank, the described outlet of adjustment tank is connected with the import of adsorption system, the outlet of described adsorption system is connected with the import of the second surge tank, and the outlet of described second surge tank is connected with the import of ammonia nitrogen removal system.
2. ammonia nitrogen waste water recycling treatment system according to claim 1, it is characterised in that: the front portion of described collecting-tank is provided with grid device; Described grid device includes coarse rack and fine fack, and the grid gap of coarse rack is 20-30mm, and the outlet of coarse rack is connected with the import of fine fack by pipeline, and the grid gap of fine fack is 5-10mm, and the outlet of fine fack is connected with pipeline collecting-tank;
Being provided with aerating system, the first stirring system and effusion meter in described collecting-tank, described aerating system includes aeration head and aeration air compressor, and described aeration head is arranged at the bottom of the pond of collecting-tank; Described first stirring system includes stirring paddle and motor,
The top of described collecting-tank is provided with porous plate, described first stirring system is arranged on the porous plate on top of collecting-tank, described aerating system is connected with effusion meter, and described effusion meter is connected with aeration air compressor, and described aeration air compressor is arranged on the outside of collecting-tank.
3. ammonia nitrogen waste water recycling treatment system according to claim 1, it is characterised in that: the pond Bottom Shape of described Buffer Pool is taper, is removed less float and impurity by precipitation; PH value of waste water in described adjustment still is adjusted to 5-6.5, and waste water is 30-120min in the time of staying regulated in still; Being provided with anti-coking agent in described adjustment still, described anti-coking agent quality is the 0.1-0.5% of wastewater quality.
4. ammonia nitrogen waste water recycling treatment system according to claim 1; it is characterized in that: described anti-coking agent is sodium dithionite, thiourea dioxide, Methyl disulfide, sodium sulfide or sodium borohydride; the adsorbent added in described adjustment still is powdered activated carbon or granular active carbon, and described quality of activated carbon is the 0.02-1.5% of wastewater quality.
5. ammonia nitrogen waste water recycling treatment system according to claim 1, it is characterised in that: being provided with acid solution automatic medicament feeding system and the second stirring system on described adjustment tank, the pH value of waste water in described adjustment tank is adjusted to 3-5.
6. ammonia nitrogen waste water recycling treatment system according to claim 4, it is characterised in that: described acid solution automatic medicament feeding system includes liquor box, the agitator tank of belt stirrer, liquidometer, dosing pump, electric cabinet and effusion meter; Described liquor box, the agitator tank of belt stirrer, liquidometer, dosing pump, electric cabinet and effusion meter are provided with import and outlet;
The outlet of described agitator tank is connected with the import of liquor box by pipeline, and the outlet of described liquor box is connected with the import regulating tank by dosing pump, and described metering delivery side of pump is connected with the import of effusion meter; The stir speed (S.S.) of the second stirring system is at 300-550r/min.
7. ammonia nitrogen waste water recycling treatment system according to claim 1, it is characterised in that: being provided with macroporous adsorbent resin in described adsorption system, the saturated adsorption volume of resin is 65-100 times of resin volume.
8. ammonia nitrogen waste water recycling treatment system according to claim 1, it is characterised in that: it is provided with acid cation exchange resin in described ammonia nitrogen removal system, 55-260 times that saturated adsorption volume is resin volume of resin.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521116078.6U CN205313302U (en) | 2015-12-28 | 2015-12-28 | Ammonia nitrogen wastewater resourceful treatment system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521116078.6U CN205313302U (en) | 2015-12-28 | 2015-12-28 | Ammonia nitrogen wastewater resourceful treatment system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205313302U true CN205313302U (en) | 2016-06-15 |
Family
ID=56199781
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201521116078.6U Withdrawn - After Issue CN205313302U (en) | 2015-12-28 | 2015-12-28 | Ammonia nitrogen wastewater resourceful treatment system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205313302U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105601014A (en) * | 2015-12-28 | 2016-05-25 | 江苏瑞达环保科技有限公司 | Ammonia-nitrogen wastewater resourceful treatment system and treatment method of ammonia-nitrogen wastewater resourceful treatment system |
-
2015
- 2015-12-28 CN CN201521116078.6U patent/CN205313302U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105601014A (en) * | 2015-12-28 | 2016-05-25 | 江苏瑞达环保科技有限公司 | Ammonia-nitrogen wastewater resourceful treatment system and treatment method of ammonia-nitrogen wastewater resourceful treatment system |
| CN105601014B (en) * | 2015-12-28 | 2018-01-12 | 江苏瑞达环保科技有限公司 | A kind of ammonia nitrogen waste water recycling treatment system and its processing method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104649524B (en) | A kind of livestock and poultry cultivation sewage water treatment method | |
| CN108191162A (en) | A kind for the treatment of process of the organic wastewater with difficult degradation thereby of high content of salt containing aniline | |
| CN103435224A (en) | Waste water treatment technology for livestock breeding | |
| CN104291532B (en) | A kind of 2-Naphthol production wastewater treatment method and apparatus | |
| CN209957618U (en) | Medicine comprehensive wastewater treatment system | |
| CN107759036A (en) | Treatment method and device for preparing compound fertilizer from sludge | |
| CN102198997B (en) | Treatment process method for wastewater from abscisic acid production | |
| CN104402167A (en) | Printing and dyeing wastewater biochemical treatment method | |
| CN106242191A (en) | A kind of process technique of Pb-Zn deposits beneficiation wastewater | |
| CN108793405A (en) | Build sewage water denitrification dephosphorization apparatus method, denitrification dephosphorization apparatus and denitrification and dephosphorization method | |
| CN107500476A (en) | A kind of high protein waste water treatment process | |
| CN110304759A (en) | A kind of system and method using denitrification processing acid-basic regenerated waste liquids in water | |
| CN205347118U (en) | Processing system who contains inorganic ammonium salt waste water | |
| CN205313302U (en) | Ammonia nitrogen wastewater resourceful treatment system | |
| CN101602546B (en) | Anaerobic reactor and wastewater treatment method with same | |
| CN107055947B (en) | Electrolytic enhanced membrane bioreactor and method for treating wastewater by using same | |
| CN205151914U (en) | Compound microorganisms fluidized bed aerobic reaction ware | |
| CN204111543U (en) | A kind of 2-Naphthol production wastewater treatment equipment | |
| CN205368049U (en) | Sizing agent effluent treatment plant | |
| CN105601014B (en) | A kind of ammonia nitrogen waste water recycling treatment system and its processing method | |
| CN102015553B (en) | Method for treating and/or pretreating liquid manure or biogas plant waste for removing harmful substances, in particular nitrogen, phosphorus and odorous molecules | |
| CN208532380U (en) | A kind of modified IC anaerobic reactor | |
| CN218810841U (en) | Be used for waste water activated sludge to strengthen phosphorus removal device | |
| CN107827322B (en) | Sewage treatment process for realizing sludge growth of soybean protein wastewater anaerobic reactor | |
| CN108862849A (en) | The treatment process and processing system of Almond debitterizing wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20160615 Effective date of abandoning: 20180112 |
|
| AV01 | Patent right actively abandoned |