CN203976573U - Synchronously realize the system that industrial cycle water softening and sewage phosphorus reclaim - Google Patents
Synchronously realize the system that industrial cycle water softening and sewage phosphorus reclaim Download PDFInfo
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- CN203976573U CN203976573U CN201320844859.1U CN201320844859U CN203976573U CN 203976573 U CN203976573 U CN 203976573U CN 201320844859 U CN201320844859 U CN 201320844859U CN 203976573 U CN203976573 U CN 203976573U
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Abstract
The utility model relates to a kind of system that synchronously realizes industrial cycle water softening and sewage phosphorus recovery.Heat-exchange equipment is connected with internal recycle under meter, side water flow meter respectively, and internal recycle under meter, cooling tower, water cooling pond, water circulating pump, heat-exchange equipment are connected successively; Septic tank and sewage equalizing tank are connected, the built-in submersible sewage pump of sewage equalizing tank, and submersible sewage pump, sewage flowmeter, reaction tank are connected successively; Side water flow meter, reaction tank, settling tank are connected successively; Reaction tank built-in temperature sensor, pH sensor; PH regulator flow container, dosing pump, reaction tank are connected successively; Settling tank, back-water valve, circling water flow rate meter, aeration tank, second pond, back water pump, cooling tower are connected successively; Aerator is set in aeration tank, and aerator, gas meter, air pump are connected successively; Second pond, sludge reflux under meter, sludge reflux pump, aeration tank are connected successively; PLC controller is connected with each under meter, each sensor, dosing pump respectively.
Description
Technical field
The utility model relates to a kind of New Type of Sewage Treatment System, is specifically related to a kind of system that synchronously realizes industrial cycle water softening and sewage phosphorus recovery.
Background technology
Than municipal wastewater, plant produced and sanitary sewage, because of its potential hazardness, are carried out more strict processing and emission standard conventionally.Existing industrial park, because of its comparatively ripe supporting pipe network of municipal administration, plant area's sewage just can enter municipal drainage pipe network after mostly only needing processing to reach " integrated wastewater discharge standard " grade III Standard.And for many newly-built industrial parks, sometimes often need to strictly process at on-site due to municipal administration supporting asynchronous, dirty, waste water, reach after " integrated wastewater discharge standard " primary standard, can be discharged into surface water body nearby.
With regard to sanitary sewage, the strict degree varies of effluent index of C, N, this three large pollutent of P in existing " integrated wastewater discharge standard " primary standard of carrying out, COD<100mg/L, NH
4 +-N<15mg/L, PO
4 3--P<0.5mg/L.Obviously, plant area to sewage without denitrogenation requirement, but dephosphorization require very strict, reach " urban wastewater treatment firm pollutant emission standard " highest standard (one-level A mark) (GB18918-2002).In daily life, after the phosphoric in human body food intake, except for the synthesis of self cell enlargement, the overwhelming majority all excretes by movement (ight soil and urine).Except indivedual exclusive phosphorus industrial plants, the universal main carriers that makes sanitary sewage become phosphoric in most plant effuents of flush toilet.Therefore, the key of plant effuent dephosphorization is to find economic, effective treatment process, realizes the qualified discharge of sanitary sewage water outlet phosphorus concentration.
The same with the much fossil class energy, be widely used in Rock Phosphate (72Min BPL) in the industrial and agricultural productions such as agricultural, medicine, chemical industry, food, national defence (with PO
4 3--P form exists for master) resource belongs to nonrenewable resources, day by day reduces, and become the national strategy resource of the restricted outlet of China.At sewage treatment area, through the technical development of last 100 years, by discharge, chemical precipitation or the biochemical processing mode combining of biological rich phosphorous sludge, the non-difficult problem of the removal of phosphoric.But it is front line science problem that the phosphoric in sewage is reclaimed, and makes rational use of resources, utility model novel treatment system and processing method will have prospect at following production field, produce potential economic benefit.
On the other hand, in industrial production system, recirculating cooling water system is dominate usually.Particularly, for open type system, owing to being subject to the restriction of cycles of concentration, in the working cycle of water, must discharging a certain amount of dense water and supplement a certain amount of new water.In the dense water of wherein discharging, saltiness higher is a subject matter, and for example, in Northern Part of China, life-time service is containing Ca
2+, Mg
2+the recirculated water that plasma concentration is higher or make up water, very likely cause the fouling of circulating pipe and water cooling equipment, has a strong impact on the working efficiency of heat-exchange equipment.Therefore, above-mentioned brine waste is carried out to even reuse of side processing, there is important Significance for Environment and economic worth.
In sum, realizing that efficient, economic desalination and phosphorus reclaims is respectively the potential problems that industrial circulating water and sanitary sewage disposal face.At present, for the recovery of phosphoric, the precipitator method effect that adds metal ion is better, but needs outer adding medicine, has certain Financial cost, and Process operating parameters still needs optimization, to improve the rate of recovery.And the higher Ca of content in industrial circulating water
2+it is unheeded potential medicament in chemical dephosphorization process.Therefore, for the industrial working that has sanitary sewage disposal and industrial cycle water treatment two large systems concurrently, by rational technical renovation, said system is rationally coupled, and set up effective control method, will make synchronously to realize industrial cycle water softening reuse and sanitary sewage phosphorus and reclaim and become possibility.
The Chinese patent that application number is 200910115969.2, name is called a kind of removal method of phosphor in sewage, application number is the removal method that Chinese patent that 200710108304.X, name are called the method for a kind of municipal sewage plant dephosphorization discloses phosphor in sewage, but the same with other prior aries, have that dephosphorization technique is unstable, chemical dephosphorization dosage is large, in industrial circulating water use procedure containing Ca
2+the problems such as the higher blowdown water demineralizing of concentration.
Utility model content
The purpose of this utility model is to overcome above shortcomings in prior art, and a kind of system that synchronously realizes industrial cycle water softening and sewage phosphorus recovery of establishing is provided, will be containing Ca
2+the sewage from industrial cycle water that concentration is higher is originated as the metal ion of chemical dephosphorization, introduces domestic sewage processing system, forms the coupling of industrial cycle water softening and domestic sewage processing system; And optimize operating parameter, and form efficient, economic control method, synchronously realize the recovery of softening reuse and Phosphorus in Domestic Wastewater with Pulverized element in industrial cycle.
The technical scheme in the invention for solving the above technical problem is:
Synchronously realize the system that industrial cycle water softening and sewage phosphorus reclaim, comprise septic tank, sewage equalizing tank, submersible sewage pump, sewage flowmeter, heat-exchange equipment, internal recycle under meter, side water flow meter, cooling tower, water cooling pond, water circulating pump, reaction tank, temperature sensor, pH sensor, PLC controller, dosing pump, pH regulator flow container, settling tank, back-water valve, circling water flow rate meter, aeration tank, aerator, gas meter, air pump, second pond, back water pump, sludge reflux pump, mud valve, sludge reflux under meter;
Heat-exchange equipment is connected with internal recycle under meter, side water flow meter respectively, and internal recycle under meter, cooling tower, water cooling pond, water circulating pump, heat-exchange equipment are connected successively;
Septic tank and sewage equalizing tank are connected, the built-in submersible sewage pump of sewage equalizing tank, and submersible sewage pump, sewage flowmeter, reaction tank are connected successively; Side water flow meter, reaction tank, settling tank are connected successively;
Reaction tank built-in temperature sensor, pH sensor; PH regulator flow container, dosing pump, reaction tank are connected successively;
Settling tank, back-water valve, circling water flow rate meter, aeration tank, second pond, back water pump, cooling tower are connected successively;
Aerator is set in aeration tank, and aerator, gas meter, air pump are connected successively; Bottom, aeration tank is provided with mud valve;
Second pond, sludge reflux under meter, sludge reflux pump, aeration tank are connected successively;
PLC controller is connected with internal recycle under meter, side water flow meter, sewage flowmeter, temperature sensor, pH sensor, dosing pump, circling water flow rate meter respectively.
Settling tank described in the utility model bottom is provided with exhaust-valve.
In reaction tank described in the utility model, be provided with agitator.
The problems such as the utility model is unstable for existing biological phosphate-eliminating technology, chemical dephosphorization technology dosage large, industrial cycle water desalination, the softening treatment system of coupling domestic sewage processing system and sewage from industrial cycle water side, alkalescence and the middle hot environment of utilizing circulating hot water sewer to provide, and the Ca being wherein rich in
2+as metal-salt, and PO in sanitary sewage
4 3-reaction.By the optimization function of regulation system, for realizing efficiently, economically Ca
2+with PO
4 3-precipitin reaction create conditions, and then synchronous softening industrial circulating water reclaim the phosphoric in sewage.The utility model compared with prior art, has the following advantages and effect:
1 compares with existing biological removal of phosphorus in wastewater system, and effluent quality is more secure, efficient, reliability is better, and without spoil disposal, reduces sludge disposal difficulty.
2, the thick salt media that in industrial circulating water system, sewer is rich in can be used as the required metal-salt of chemical phosphorus removal system, has saved adding of outer adding medicine.
3, by coupling Open recirling cooling water system, realize CO in water and air by the aeration in cooling tower
2balance, water pH is 8.5 left and right, can the required alkaline environment of self-assembling formation metal ion chemical precipitation method.
4, the calcium phosphate precipitation forming after reaction can be collected the recovery that realizes phosphoric, and system water outlet can realize reuse by secondary treatment where necessary, for the make up water of circulating water system, creates economic worth.
5, can ensure system water outlet PO
4 3--P mass concentration <0.5mg/L, reduces the Ca in circulating water system simultaneously to the full extent
2+mass concentration.
Brief description of the drawings
Fig. 1 is a kind of system architecture schematic diagram of synchronously realizing industrial cycle water softening and sewage phosphorus recovery of the utility model embodiment.
Fig. 2 is the control method schematic diagram of a kind of utility model that synchronously realizes industrial cycle water softening and sewage phosphorus recovery of the utility model embodiment.
In figure: 1-septic tank, 2-sewage equalizing tank, 3-submersible sewage pump, 4-sewage flowmeter, 5-heat-exchange equipment, 6-internal recycle under meter, 7-side water flow meter, 8-cooling tower, 9-water cooling pond, 10-water circulating pump, 11-reaction tank, 12-agitator, 13-temperature sensor, 14-pH sensor, 15-PLC controller, 16-dosing pump, 17-pH regulates flow container, 18-settling tank, 19-exhaust-valve, 20-back-water valve, 21-circling water flow rate meter, 22-aeration tank, 23-aerator, 24-gas meter, 25-air pump, 26-second pond, 27-back water pump, 28-sludge reflux pump, 29-mud valve, 30-sludge reflux under meter.
Embodiment
Below in conjunction with accompanying drawing and by embodiment, the utility model is described in further detail, and following examples are to explanation of the present utility model and the utility model is not limited to following examples.
Referring to Fig. 1 and Fig. 2, in a kind of system that synchronously realizes industrial cycle water softening and sewage phosphorus recovery of the utility model embodiment, heat-exchange equipment 5 is connected with internal recycle under meter 6, side water flow meter 7 respectively by two-way pipeline, and internal recycle under meter 6, cooling tower 8, water cooling pond 9, water circulating pump 10, heat-exchange equipment 5 are connected successively by pipeline; Above structure forms recirculated water main flow system.Internal recycle under meter 6 is all connected with PLC controller 15 by electric wire with side water flow meter 7.
Septic tank 1 is connected with sewage equalizing tank 2 by pipeline, the built-in submersible sewage pump 3 of sewage equalizing tank 2, and submersible sewage pump 3, sewage flowmeter 4, reaction tank 11 are connected successively by pipeline; Side water flow meter 7, reaction tank 11, settling tank 18 are connected successively by pipeline, and above structure forms recirculated water by-pass flow and softens and sewage phosphorus recovery system.Sewage flowmeter 4 is connected with PLC controller 15 by electric wire.
The built-in agitator 12 of reaction tank 11, temperature sensor 13, pH sensor 14.PH regulator flow container 17, dosing pump 16, reaction tank 11 are connected successively by pipeline.Temperature sensor 13, pH sensor 14, dosing pump 16 are all connected with PLC controller 15 by electric wire.Settling tank 18 bottoms are provided with exhaust-valve 19.The NaOH solution that the built-in amount of substance concentration of pH regulator flow container 17 is 0.1-0.5mol/L.In the present embodiment, the NaOH solution that the built-in amount of substance concentration of pH regulator flow container 17 is 0.1mol/L.
Settling tank 18, back-water valve 20, circling water flow rate meter 21, aeration tank 22, second pond 26, back water pump 27, cooling tower 8 are connected successively by pipeline, and above structure forms cooling circulating water reuse water charging system.Circling water flow rate meter 21 is connected with PLC controller 15 by electric wire.The interior aerator 23 that arranges in aeration tank 22, aerator 23, gas meter 24, air pump 25 are connected successively by pipeline.22 bottoms, aeration tank are connected by pipeline and mud valve 29.Second pond 26 bottoms, sludge reflux under meter 30, sludge reflux pump 28, aeration tank 22 are connected successively by pipeline.
A kind of method that synchronously realizes industrial cycle water softening and sewage phosphorus recovery of the utility model embodiment, can ensure system water outlet PO
4 3--P mass concentration <0.5mg/L, reduces the Ca in circulating water system simultaneously to the full extent
2+mass concentration.Its principle is: domestic sewage processing system and the softening treatment system of sewage from industrial cycle water side are coupled, the alkalescence (pH is in 8.5 left and right) and middle high temperature (35 DEG C of the T >) environment that utilize circulating hot water sewer to provide, and the Ca being wherein rich in
2+as metal-salt, and through the PO in the pretreated sanitary sewage of septic tank
4 3-reaction.By regulation system (being formed by sewage flowmeter 4, internal recycle under meter 6, side water flow meter 7, temperature sensor 13, pH sensor 14, dosing pump 16 and PLC controller 15), temperature and pH value in water inlet ratio, the reaction tank of optimization Wastewater Form Circulating Cooling Water and sanitary sewage, realize Ca efficiently, economically
2+with PO
4 3-precipitin reaction, and then synchronous softening industrial circulating water reclaim the phosphoric in sewage.
The method specifically comprises following process:
(1), sanitary sewage enters sewage equalizing tank 2 after septic tank 1 pre-treatment, PLC controller 15 regulates the revolution of sewage flowmeter 4, making through the discharge of sewage in it is Q
1, flow is Q
1sewage enter reaction tank 11 through the lifting of submersible sewage pump 3.
(2), PLC controller 15 regulates internal recycle under meter 6 and side water flow meter 7 revolutions, it is Q that heat-exchange equipment 5 produces flow
2and Q
3hot water enter respectively the softening and sewage phosphorus recovery system of recirculated water main flow system, recirculated water by-pass flow.Q
2with Q
3ratio be 40-100.In the present embodiment, Q
2with Q
3ratio be 50.
Recirculating cooling water system is followed the increase of working time, can cause Ca
2+, Mg
2+the increase of plasma concentration, need regularly drain a part of dense water, contains high density Ca in this dense water
2+, Mg
2+, in the application, this part dense water is the sewage through side under meter, and Q
2for the internal recycle discharge of sewage, control Q
2with Q
3ratio be that 40-100 can maintain the Ca in circulating water system well
2+concentration maintains stationary value.Simultaneously according to Q
3, can extrapolate the Ca that enters chemical precipitation reaction
2+concentration, and then control dosage.
(3), flow is Q
2hot water enter after cooling tower 8 and to enter water cooling pond 9 after cooling cooling tower 8 is interior, and be recycled water pump 10 and be promoted to heat-exchange equipment 5 and again utilize.
(4), flow is Q
3hot water enter after reaction tank 11, under the effect of agitator 12, be Q with flow
1sewage mix, mixed stream, after the interior stop of reaction tank 11 30-45min, enters settling tank 18, the flocculate precipitate generating in reaction tank is at the interior stop of settling tank 18 1-1.5h.In the present embodiment, mixed stream, after the interior stop of reaction tank 11 30min, enters settling tank 18, and the flocculate precipitate generating in reaction tank is at the interior stop of settling tank 18 1h.
Mixed stream stops 30-45min in reaction tank, is the Ca of normal concentration in industrial circulating water
2+with PO
4 3-reaction is to generating the required time interval of precipitation completely.
The flocculate precipitate generating in reaction tank stops 1-1.5h in settling tank, and it is completely quiet heavy generally can to realize, and ensures effluent quality on the one hand, can at utmost realize on the other hand the sedimentary recovery of phosphorus.
(5), open back-water valve 20, PLC controller 15 regulates the revolution of circling water flow rate meter 21, making through the discharge in it is that flow is Q
4, flow is Q
4settling tank 18 water outlets enter aeration tank 22, flow is Q
1+ Q
3-Q
418 water outlets of residue settling tank be exhausted from system by exhaust-valve 19.
(6), open air pump 25, the revolution of PLC controller 15 adjusting gas flow meters 21, makes air demand Q
5with Q
4ratio be 5-8.Flow is Q
418 water outlets of partly precipitated pond after the interior stop in aeration tank 22 2-3h, the mud mixture of active sludge (being in the nature microorganism) and water enters second pond 26 from aeration tank 22, sink through the quiet of 1-1.5h, realize mud-water separation, supernatant liquor again enters cooling tower 8 after back water pump 27 promotes, and enters circulating water system carry out reuse with this; In the present embodiment, Q
5with Q
4ratio be 7, flow is Q
418 water outlets of partly precipitated pond after the interior stop in aeration tank 22 2.5h, the mud mixture of active sludge and water enters second pond 26 from aeration tank 22, sink through the quiet of 1.5h, realize mud-water separation, supernatant liquor again enters cooling tower 8 after back water pump 27 promotes, and enters circulating water system carry out reuse with this.
Q
5with Q
4ratio is called as gas-water ratio in biological sewage treatment, by the ratio control of gas flow and the discharge of sewage, can utilize aerobic slight biology in aeration tank 22 by a part of organic matter removal in sewage, make reuse circulation organic pollutants concentration lower, reduce growing of the biologies such as bacterium in circulating water system pipeline.The ratio of 5-8 is comparatively economic, efficient gas-water ratio scope.
In this process, above-mentioned 2-3h is that organism obtains the preliminary required time of degraded in aeration tank 22.
(7), the revolution of conditioning of mud return flow meter 30, making through the mud discharge in it is Q
6, Q
6value is 0.5Q
4-Q
4, the active sludge in second pond 26 is refluxed and is entered aeration tank 22 by return sludge pump 28; In the present embodiment, Q
6=Q
4.
Active sludge in second pond 26, can be along with the increase of working time from aeration tank 22, and concentration constantly rises, and therefore needs to carry out sludge reflux with return sludge pump 28, and the flow of backflow (is Q in the application according to the processing flow of sewage
4) determine, the flow refluxing in the application is 50-100%, i.e. Q
6value is 0.5Q
4-Q
4.
In aeration tank 22, add active sludge, active sludge mass concentration is 2000-3000mg/L; Regularly open mud valve 29, control sludge retention time is 15-20d.In the present embodiment, the interior active sludge mass concentration in aeration tank 22 is 2500mg/L; Regularly open mud valve 29, control sludge retention time is 20d.
Active sludge mass concentration 2000-3000mg/L ensures in aeration tank 22 that organic pollutant is under the conditions such as above-mentioned flow, gas-water ratio, obtains the reasonable concentration of effectively degraded: active sludge mass concentration is too low, and the required treatment time can increase, and efficiency is low; Active sludge mass concentration is too high, and microorganism lacks enough organism for metabolism, can enter the endogenous respiration stage (consuming self to provide energy for Metabolic activity), continuous aging death.
Along with microorganism constantly absorbs the organism in sewage, it is growth constantly, active sludge mass concentration in reaction tank 11 can improve constantly, therefore need by mud valve regularly discharge mud (being called excess sludge) 29 every days, maintain the activity of active sludge, sludge retention time equals active sludge mass concentration in aeration tank 22 divided by the excess sludge quality that need to discharge every day.By controlling sludge retention time, can calculate the excess sludge quality of required discharge every day.Control sludge retention time is 15-20d, comparatively favourable to maintaining the activity of active sludge.
Said process (one), to (seven), carries out, without sequencing simultaneously.
The method also comprises following control process:
Following condition is set:
Condition A: settling tank 18 water outlet PO
4 3--P mass concentration <0.5mg/L; This condition is PO in " integrated wastewater discharge standard " primary standard
4 3-the emission standard of-P, i.e. <0.5mg/L;
Condition B: settling tank 18 water outlet Ca
2+mass concentration <5.0mg/L; This condition is Ca
2+with PO
4 3-the concentration limit of-P reaction, is less than 5mg/L, and speed of reaction is very low, and 5mg/L is also the parameter value of inspection chemical precipitation effect simultaneously;
Condition C: interior pH>=8.0 of reaction tank 11; This condition detects by pH sensor 14, and, Ca
2+and PO
4 3--P reaction needed alkaline environment, pH is 8 to be conventional threshold values;
Condition D: interior temperature >=20 DEG C of reaction tank 11; This condition detects by temperature sensor 13, and chemical reaction needs rational temperature, and 20 DEG C is a conventional threshold value of speed of reaction height, and temperature is less than 20 DEG C, and speed of reaction declines obviously.
Following strategy is set:
Strategy I: regularly detect PO in settling tank 18 water outlets
4 3--P and Ca
2+mass concentration;
Strategy II: improve side water flow meter 7 revolutions; This strategy improves side water flow meter 7 revolutions by PLC controller 15;
Strategy III: improve sewage flowmeter 4 revolutions; This strategy improves sewage flowmeter 4 revolutions by PLC controller 15;
Strategy IV: open dosing pump 16; This strategy can join the pH regulator liquid in pH regulator flow container in reaction tank 11.
Strategy V: reduce sewage flowmeter 4 revolutions.This strategy reduces sewage flowmeter 4 revolutions by PLC controller 15.
Condition A is to condition D execution sequentially in a control cycle.
Strategy I and tactful II are carried out in a control cycle sequentially to tactful V, i.e. first implementation strategy I, then implementation strategy II is to tactful V; Between strategy II, tactful III, tactful IV, tactful V without sequencing.
This control process comprises the steps:
A, implementation strategy I, Rule of judgment A, in the time that condition A sets up, Rule of judgment B, in the time that condition B sets up, returns to implementation strategy I; In the time that condition B is false, implementation strategy III, and return to the judgement of condition A; In the time that condition A is false, Rule of judgment B, in the time that condition B sets up, implementation strategy II, and return to the judgement of condition B, when condition, B still sets up, repeatedly implementation strategy IV; In the time that condition B is false, Rule of judgment C;
B, in the time that condition C is false, implementation strategy IV, and return to the judgement of condition C, in the time that condition C is still false, implementation strategy IV repeatedly; In the time that condition C is set up, Rule of judgment D;
C, in the time that condition D is false, implementation strategy II, and return to the judgement of condition D, when condition, D is still false, repeatedly implementation strategy II; In the time that condition D sets up, implementation strategy V, and return to implementation strategy I;
D, repetitive sequence are implemented above-mentioned steps a to c.
Case: adopt the embodiment of the present invention to process the sanitary sewage of flushing the toilet (COD=200-400mg/L, the NH of certain factory's discharge
4 +-N=50-90mg/L, PO
4 3--P=, 5-15mg/L).After steady running, water outlet NH
4 +-N is less than 15mg/L, and COD is less than 100mg/L, PO
4 3--P is less than 0.5mg/L, meets " integrated wastewater discharge standard " primary standard.
In addition, it should be noted that, the specific embodiment described in this specification sheets, shape, institute's title of being named etc. of its parts and components can be different, and the above content described in this specification sheets is only to structure example of the present invention explanation.
Claims (3)
1. synchronously realize the system that industrial cycle water softening and sewage phosphorus reclaim, it is characterized in that: comprise septic tank, sewage equalizing tank, submersible sewage pump, sewage flowmeter, heat-exchange equipment, internal recycle under meter, side water flow meter, cooling tower, water cooling pond, water circulating pump, reaction tank, temperature sensor, pH sensor, PLC controller, dosing pump, pH regulator flow container, settling tank, back-water valve, circling water flow rate meter, aeration tank, aerator, gas meter, air pump, second pond, back water pump, sludge reflux pump, mud valve, sludge reflux under meter;
Heat-exchange equipment is connected with internal recycle under meter, side water flow meter respectively, and internal recycle under meter, cooling tower, water cooling pond, water circulating pump, heat-exchange equipment are connected successively;
Septic tank and sewage equalizing tank are connected, the built-in submersible sewage pump of sewage equalizing tank, and submersible sewage pump, sewage flowmeter, reaction tank are connected successively; Side water flow meter, reaction tank, settling tank are connected successively;
Reaction tank built-in temperature sensor, pH sensor; PH regulator flow container, dosing pump, reaction tank are connected successively;
Settling tank, back-water valve, circling water flow rate meter, aeration tank, second pond, back water pump, cooling tower are connected successively;
Aerator is set in aeration tank, and aerator, gas meter, air pump are connected successively; Bottom, aeration tank is provided with mud valve;
Second pond, sludge reflux under meter, sludge reflux pump, aeration tank are connected successively;
PLC controller is connected with internal recycle under meter, side water flow meter, sewage flowmeter, temperature sensor, pH sensor, dosing pump, circling water flow rate meter respectively.
2. the system that synchronously realizes industrial cycle water softening and sewage phosphorus recovery according to claim 1, is characterized in that: described settling tank bottom is provided with exhaust-valve.
3. the system that synchronously realizes industrial cycle water softening and sewage phosphorus recovery according to claim 1, is characterized in that: in described reaction tank, be provided with agitator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320844859.1U CN203976573U (en) | 2013-12-20 | 2013-12-20 | Synchronously realize the system that industrial cycle water softening and sewage phosphorus reclaim |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320844859.1U CN203976573U (en) | 2013-12-20 | 2013-12-20 | Synchronously realize the system that industrial cycle water softening and sewage phosphorus reclaim |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203976573U true CN203976573U (en) | 2014-12-03 |
Family
ID=51974037
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320844859.1U Withdrawn - After Issue CN203976573U (en) | 2013-12-20 | 2013-12-20 | Synchronously realize the system that industrial cycle water softening and sewage phosphorus reclaim |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103723889A (en) * | 2013-12-20 | 2014-04-16 | 中国联合工程公司 | System and method for synchronously implementing softening of industrial circulating water and recovery of phosphorus in sewage |
| CN115367972A (en) * | 2022-09-22 | 2022-11-22 | 浙江开创环保科技股份有限公司 | Small-sized integrated MBR sewage treatment equipment and process suitable for inflow fluctuation |
| CN116789248A (en) * | 2023-08-25 | 2023-09-22 | 华侨大学 | Device and method for carbonization recycling of concrete wastewater and waste slurry |
-
2013
- 2013-12-20 CN CN201320844859.1U patent/CN203976573U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103723889A (en) * | 2013-12-20 | 2014-04-16 | 中国联合工程公司 | System and method for synchronously implementing softening of industrial circulating water and recovery of phosphorus in sewage |
| CN115367972A (en) * | 2022-09-22 | 2022-11-22 | 浙江开创环保科技股份有限公司 | Small-sized integrated MBR sewage treatment equipment and process suitable for inflow fluctuation |
| CN116789248A (en) * | 2023-08-25 | 2023-09-22 | 华侨大学 | Device and method for carbonization recycling of concrete wastewater and waste slurry |
| CN116789248B (en) * | 2023-08-25 | 2023-11-24 | 华侨大学 | Device and method for carbonization recycling of concrete wastewater and waste slurry |
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