CN209797625U - Desulfurization and denitrification wastewater treatment device - Google Patents
Desulfurization and denitrification wastewater treatment device Download PDFInfo
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- CN209797625U CN209797625U CN201822077643.2U CN201822077643U CN209797625U CN 209797625 U CN209797625 U CN 209797625U CN 201822077643 U CN201822077643 U CN 201822077643U CN 209797625 U CN209797625 U CN 209797625U
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- softening
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- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The utility model relates to a SOx/NOx control effluent treatment plant, including the equalizing basin, the elevator pump, first reaction tank, the second reaction tank, soften the circulating pump, the automatically cleaning filter, soften the tubular milipore filter, produce the water pump and soften the water tank, the equalizing basin water inlet is connected with the waste water collecting pit, the equalizing basin passes through the elevator pump at the bottom of the pool and is connected with first reaction tank mouth, first reaction tank passes through the raceway at the bottom of the pool and is connected with second reaction tank mouth, the second reaction tank passes through softening the circulating pump at the bottom of the pool and is connected with the automatically cleaning filter, get into afterwards and soften tubular milipore filter and filter the concentration, get into through softening tubular milipore filter partly through mixing water pump entering softening water tank, partly milipore filter concentrate flows back and advances the equalizing basin. The system effectively and quickly shortens the wastewater treatment time, improves the treatment effect and meets the national discharge requirement.
Description
Technical Field
The utility model relates to a waste water treatment technical field specifically relates to a SOx/NOx control effluent treatment plant.
Background
The waste water produced in the wet desulfurization (limestone/gypsum method) process of the boiler flue gas comes from the discharge water of the absorption tower. In order to maintain the balance of the mass of the slurry circulation system of the desulfurization unit, prevent the soluble fraction of the flue gas, i.e., the chlorine concentration, from exceeding the specified value and ensure the quality of gypsum, a certain amount of waste water must be discharged from the system, which is mainly from the gypsum dewatering and cleaning system. The impurities contained in the wastewater mainly comprise suspended matters, supersaturated sulfite, sulfate and heavy metals, and many of the impurities are the first pollutants which are strictly controlled in the national environmental protection standard.
The standard exceeding items of the desulfurization and denitrification wastewater mainly comprise suspended matters, pH values, heavy metal ions, fluorides and the like, and in order to reach the sewage discharge standard or realize recycling, the most widely applied method is a physical and chemical method, such as a flocculation precipitation method. The physical and chemical method mainly comprises the steps of adding a pH regulator to regulate pH, adding a flocculating agent to perform reaction flocculation clarification, creating a proper reaction gradient through mechanical stirring to enable most heavy metals in the wastewater to form precipitates and settle, and finally performing neutralization to achieve the removal effect.
The defects of the prior art are that the reaction area is too large, the flow is too long, however, the purpose of removing trace heavy metals cannot be achieved by using the traditional flocculation precipitation method due to the fact that the water quality of the desulfurization and denitrification wastewater changes quickly, high treatment cost is required to be paid out by using a large amount of reagents, non-existent pollutants can be introduced into a water body, secondary pollution is caused, and the emission of heavy metals cannot reach the standard completely by adopting the process along with the strict control of environmental regulations.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a SOx/NOx control effluent treatment plant, the effective quick waste water treatment time that has shortened of this system has improved the treatment effect, reaches the national emission requirement.
The technical scheme of the utility model as follows: the utility model provides a SOx/NOx control effluent treatment plant, the device is including equalizing basin, elevator pump, first reaction tank, second reaction tank, softening circulating pump, automatically cleaning filter, softening tubular milipore filter, product water pump and soften the water tank, the equalizing basin water inlet is connected with the waste water collecting pit, and the equalizing basin passes through the elevator pump at the bottom of the pool and is connected with first reaction tank mouth, and first reaction tank passes through raceway and second reaction tank mouth at the bottom of the pool and is connected, and the second reaction tank passes through softening circulating pump and is connected with the self-cleaning filter at the bottom of the pool, gets into softening tubular milipore filter subsequently and filters the concentration, gets into the softening water tank through mixing the water pump through softening tubular milipore filter partly, and partly milipore filter concentrate flows back into the equalizing basin, be equipped with PH adjusting agent device in the first reaction tank, add lime device and add softening medicine device, be equipped with PH adjusting agent device in the second reaction tank, A coagulant adding device and a magnesium oxide adding device.
As a modification, the PH regulating medicament device in the first reaction tank comprises an acid adding device and an alkali adding device.
As an improvement scheme, the PH regulating medicine device in the first reaction tank is a NaOH adding device.
As a modification, the first reaction tank and the second reaction tank are provided with mechanical stirring devices.
As a modification, the produced water of the softened water tank further enters a DTRO device for treatment.
As an improvement scheme, the produced water of the softened water tank enters a sand filter through a DTRO (draw texturing yarn) water inlet pump and then enters a core filter, a primary high-pressure plunger pump is connected to a liquid outlet pipe of the core filter, a DTRO membrane module is connected behind the primary high-pressure plunger pump, primary permeate of a primary disc tubular membrane column enters a secondary disc tubular membrane column, primary concentrate enters a concentrate storage pool, secondary concentrate of the secondary disc tubular membrane column flows back to a water inlet pipe of the DTRO water inlet pump, secondary permeate enters a degassing tower, and the degassing tower is connected with and enters a clean water tank.
As an improvement scheme, a scale inhibitor adding device and a NaOH adding device are arranged between the sand filter and the core filter.
As an improvement scheme, a primary servo motor control valve and a secondary servo motor control valve are respectively arranged on concentrated solution conveying pipes of the primary concentrated solution and the secondary concentrated solution.
As an improvement scheme, a second-stage high-pressure plunger pump and a second-stage high-pressure energy accumulator are arranged on a connecting pipe of the first-stage disc tubular membrane column and the second-stage disc tubular membrane column.
as an improved scheme, a circulating pump is arranged on a water inlet pipe of the DTRO membrane module, and a shock absorber is arranged behind each plunger pump in the DTRO membrane module.
Compared with the prior art, the beneficial effects of the utility model are that:
1. The system has stable water quality and meets the national emission requirement: because the factors influencing the retention rate of the membrane system are few, the effluent quality of the system is stable and is not influenced by pretreatment, slight change of water quality and other factors, the filtering precision of the tubular ultrafiltration membrane is 0.03 mu m, post-precipitation flocculation is avoided, a subsequent DTRO system is protected, and salt, heavy metal and the like are removed by DTRO.
2. The system is flexible to operate: the tubular ultrafiltration membrane and DTRO membrane system is used as a set of physical separation equipment, is flexible to operate, can be operated continuously or intermittently, and can adjust the series-parallel connection mode of the system to adapt to the requirements of water quality and water quantity.
3. The construction cycle is short, and debugging, start-up are quick: the construction of the tubular ultrafiltration membrane and DTRO membrane system is mainly mechanical processing, and is accompanied by the construction of matched plants and water pools, so that the scale is small and the construction speed is high. The installation and debugging work can be completed only in about two weeks after the equipment is transported to the site.
4. Can be operated automatically, and the operation is simple and convenient: the tubular ultrafiltration membrane and DTRO membrane system can be fully automatic, the whole system is provided with a perfect monitoring and control system, the PLC can automatically adjust according to sensor parameters and timely send out an alarm signal to protect the system, an operator only needs to search for an error code according to an operation manual to remove faults, and the experience of the operator is not high.
5. The occupied area is small: the tubular ultrafiltration membrane and DTRO membrane system is installed in an integrated mode, and accessory structures and facilities are also small structures, so that the floor area is small.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without inventive exercise.
FIG. 1 is a schematic structural diagram of the present invention;
Wherein, 1, adjusting a pool; 2. a lift pump; 3. a first reaction tank; 4. a second reaction tank; 5. softening the circulating pump; 6. a self-cleaning filter; 7. softening the tubular ultrafiltration membrane; 8. a water production pump; 9. softening the water tank; 10. An acid adding device; 11. an alkali adding device; 12. a lime adding device; 13. a softening medicine adding device; 14-1/14-2, adding NaOH device; 15. a coagulant adding device; 16. a magnesium oxide adding device; 17. a mechanical stirring device; 18. a DTRO water inlet pump; 19. a sand filter; 20. a cartridge filter; 21. a first-stage high-pressure plunger pump; 22. a first-stage disc-tube membrane column; 23. a second-stage disc-tube membrane column; 24. a concentrated solution storage pool; 25. a degassing tower; 26. a clean water tank; 27. a scale inhibitor adding device; 28. a primary servo motor control valve; 29. a secondary servo motor control valve; 30. a secondary high pressure plunger pump; 31. a secondary high-voltage energy storage; 32. and a circulating pump.
Detailed Description
The following description of the embodiments of the present invention is provided for illustrative purposes, and other advantages and effects of the present invention will be readily apparent to those skilled in the art from the disclosure herein.
As shown in figure 1, a desulfurization and denitrification wastewater treatment device comprises an adjusting tank 1, a lift pump 2, a first reaction tank 3, a second reaction tank 4, a softening circulating pump 5, a self-cleaning filter 6, a softening tubular ultrafiltration membrane 7, a water production pump 8 and a softening water tank 9, wherein a water inlet of the adjusting tank 1 is connected with a wastewater collection tank, the adjusting tank 1 is connected with a first reaction tank 3 port through the lift pump 2 at the bottom of the tank, the first reaction tank 3 is connected with a second reaction tank 4 port through a water pipe at the bottom of the tank, the second reaction tank 4 is connected with the self-cleaning filter 6 through the softening circulating pump 5 at the bottom of the tank, then the wastewater enters the softening tubular ultrafiltration membrane 7 for filtration and concentration, a part of the wastewater enters the softening water tank 9 through the water production pump 8 after passing through the softening tubular ultrafiltration membrane 7, a part of the ultrafiltration membrane concentrate flows back into the adjusting tank 1, an acid adding device 10 is, An alkali adding device 11, a lime adding device 12 and a softening agent adding device 13, wherein a NaOH adding device 14-1, a coagulant adding device 15 and a magnesium oxide adding device 16 are arranged in the second reaction tank 4. The first reaction tank 3 and the second reaction tank 4 are provided with a mechanical stirring device 17.
The produced water of the softened water tank 9 further enters a DTRO device for treatment, the produced water of the softened water tank enters a sand filter 19 through a DTRO water inlet pump 18 and then enters a core filter 20, a primary high-pressure plunger pump 21 is connected to the liquid outlet pipe of the core filter 20, a DTRO membrane assembly is connected behind the primary high-pressure plunger pump 21, primary permeate of a primary disc tubular membrane column 22 enters a secondary disc tubular membrane column 23, primary concentrate enters a concentrate storage pool 24, secondary concentrate of the secondary disc tubular membrane column 23 flows back to a water inlet pipe of the DTRO water inlet pump 18, secondary permeate enters a degassing tower 25, and the degassing tower 25 is connected with a clear water tank 26. A scale inhibitor adding device 27 and a NaOH adding device 14-2 are arranged between the sand filter 19 and the core filter 20, a first-stage servo motor control valve 28 and a second-stage servo motor control valve 29 are respectively arranged on concentrated solution conveying pipes of the first-stage concentrated solution and the second-stage concentrated solution, a second-stage high-pressure plunger pump 30 and a second-stage high-pressure energy accumulator 31 are arranged on a connecting pipe of the first-stage disc tubular membrane column 22 and the second-stage disc tubular membrane column 23, a circulating pump 32 is arranged on a water inlet pipe of the DTRO membrane module, and a shock absorber (not marked) is arranged behind each plunger pump in the DTRO membrane module.
The operation process of the desulfurization and denitrification wastewater treatment device is as follows:
And the wastewater directly enters the regulating tank and is pumped into a chemical softening pretreatment system of the tubular ultrafiltration membrane softening system through a wastewater lifting pump. The chemical softening pretreatment system consists of a chemical dosing system and two-stage reaction tanks, corresponding chemical agents are added according to process requirements in the two reaction tanks, the pH value of the reaction is accurately controlled, the agents and inlet water are completely mixed through sufficient mechanical stirring to react, and the water containing sediments after the two-stage reaction overflows into a concentration tank of the tubular membrane. Meanwhile, the two-stage reaction tank is matched with a mechanical stirring device, so that precipitates are prevented from sinking into the bottom of the tank.
In the first reaction tank, pH regulating agent (acid/alkali adding device) or lime and softening agent are usually added to regulate pH to 9.5-10 for softening calcium ion, and part of magnesium ion may form magnesium hydroxide. The wastewater automatically flows into a second reaction tank, and the pH value is adjusted to 11.5-12 by NaOH, so that magnesium ions can be subjected to sufficient chemical reaction, and the efficiency of removing magnesium is improved. Meanwhile, PAC can be considered to be added as a coagulant according to the characteristics of the wastewater, so that the coagulation effect of fine particles can be improved, and the efficiency of removing organic matters can be improved. When residual active silicon particles exist in the wastewater, magnesium oxide is considered to be added, and is hydrolyzed to generate magnesium hydroxide to effectively adsorb and coprecipitate the active silicon, so that the removal efficiency of silicon is improved, the incoming water enters a dosing pool, calcium magnesium ions, heavy metal ions and silicon dioxide are changed into precipitates by adding lime milk or sodium carbonate, then the incoming water enters a self-cleaning filter through a softening circulating pump to remove a large amount of particles, impurities and suspended matters, then the incoming water enters a softening tubular ultrafiltration membrane for filtration and concentration, the tubular membrane water is produced through a water production pump, the produced water enters a softening water production tank, and the concentrated solution of the softening tubular ultrafiltration membrane enters an adjusting pool for neutralization.
Softened product water of producing the water tank gets into sand filtration filter through the DTRO intake pump, and sand filtration filter play water supplies water for one-level DTRO equipment, gets into the core at first and strains, and the suspended solid in the filtration liquid is further got rid of to the core formula filter, and equipment is furnished with 1 cover of core formula filter, and it advances, the water outlet end all has pressure sensor, automated inspection pressure differential, and the system suggestion is changed the filter core when pressure differential surpasses 2.0 bar. The filtering precision of the core filter is 10 mu m, a last protective barrier is provided for the membrane column, in order to prevent various insoluble sulfates and silicates from scaling in the membrane component due to high-power concentration and effectively prolong the service life of the membrane, a certain amount of scale inhibitor is added before the first-stage DTRO membrane, and the adding amount is determined according to the concentration of the insoluble salts in raw water.
The percolate passing through the core type filter directly enters a first-stage reverse osmosis high-pressure plunger pump. A shock absorber is arranged behind each plunger pump of the DTRO membrane system and is used for absorbing pressure pulses generated by the high-pressure pump and providing stable pressure for the membrane column. The effluent after passing through the high-pressure pump enters a membrane module, the membrane module adopts a disc-tube type reverse osmosis membrane column, the membrane module has the advantage of strong pollution resistance, the adaptability to leachate is strong, the service life of the membrane is prolonged to more than 3 years, and a first-stage DTRO system is arranged at one stage.
In order to ensure enough flow and cross flow velocity on the membrane surface and avoid membrane pollution, a circulating pump is arranged in front of the membrane component. The high pressure and high flow water from the circulating pump directly enters the membrane column.
The water output of the DTRO membrane column group is divided into two parts: first-stage concentrated solution and first-stage permeate. The concentrated solution end is provided with a servo control valve for controlling the pressure in the membrane group to generate necessary produced water recovery rate, the primary permeate enters a secondary high-pressure pump to wait for the further treatment of secondary DTRO, and the primary concentrated solution is discharged into a concentrated solution storage pool to wait for recharging or outward transportation for disposal.
The second-stage DTRO is used for further processing the first-stage DTRO permeate liquid, the permeate liquid processed by the first-stage DT membrane system is directly sent to a second-stage DT membrane system high-pressure pump without adding any medicament, a buffer tank is not needed to be arranged between the first stage and the second stage, and the flow is automatically matched when the system operates. The second-stage high-pressure pump is provided with variable frequency control, the operation frequency and the output flow of the second-stage high-pressure pump are automatically matched according to the feedback value of the first-stage permeation liquid flow sensor, and meanwhile, the inlet pipeline of the second-stage high-pressure pump is provided with concentrated liquid self-compensation, so that the operation of the second-stage system is not influenced by the water yield of the first-stage system. Because the concentration of the pollutants in the inlet water of the second-stage DTRO is greatly reduced, the requirement on the filtration flow rate of the membrane surface is low, and the recovery rate is high, the second-stage reverse osmosis does not need an online booster pump, and can meet the requirement only by using a high-pressure pump.
And the second-stage DTRO concentrated solution end is also provided with a servo motor control valve for controlling the pressure and the recovery rate in the membrane group. The second-stage DTRO concentrated solution is discharged to the water inlet end of the first-stage system because the water quality is far better than that of raw leachate, and is combined with the water inlet of the first-stage DTRO for treatment, the recovery rate of the system is improved, and the second-stage DTRO permeating solution is discharged into a degassing tower.
The basic principles, main features and advantages of the present invention have been shown and described above. It will be understood by those skilled in the art that the present invention is not limited to the above embodiments, and that the foregoing embodiments and descriptions are provided only to illustrate the principles of the present invention without departing from the spirit and scope of the present invention. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (10)
1. The utility model provides a SOx/NOx control effluent treatment plant which characterized in that: the device comprises an adjusting tank, a lift pump, a first reaction tank, a second reaction tank, a softening circulating pump, a self-cleaning filter, a softening tubular ultrafiltration membrane, a water production pump and a softening water tank, the water inlet of the regulating tank is connected with the wastewater collecting tank, the regulating tank is connected with a first reaction tank port at the bottom of the tank through a lift pump, the first reaction tank is connected with a second reaction tank port at the bottom of the tank through a water pipe, the second reaction tank is connected with a self-cleaning filter at the bottom of the tank through a softening circulating pump, then the first reaction tank enters a softening tubular ultrafiltration membrane for filtering and concentration, a part of the second reaction tank enters a softening water tank through a water mixing pump after passing through the softening tubular ultrafiltration membrane, and a part of ultrafiltration membrane concentrated solution flows back into the regulating tank, a PH regulating agent device, a lime adding device and a softening agent adding device are arranged in the first reaction tank, and a PH regulating medicament device, a coagulant adding device and a magnesium oxide adding device are arranged in the second reaction tank.
2. the desulfurization and denitrification wastewater treatment device according to claim 1, wherein: the PH adjusting medicament device in the first reaction tank comprises an acid adding device and an alkali adding device.
3. The desulfurization and denitrification wastewater treatment device according to claim 1, wherein: and the PH regulating agent device in the first reaction tank is a NaOH adding device.
4. The desulfurization and denitrification wastewater treatment apparatus according to any one of claims 1 to 3, wherein: and mechanical stirring devices are arranged in the first reaction tank and the second reaction tank.
5. The desulfurization and denitrification wastewater treatment device according to claim 1, wherein: the produced water of the softened water tank further enters a DTRO device for treatment.
6. The desulfurization and denitrification wastewater treatment device according to claim 5, wherein: softened water tank's product water passes through the DTRO intake pump and gets into sand filtration filter, gets into core filter afterwards, connects one-level high-pressure plunger pump on the core filter drain pipe, connect the DTRO membrane module behind the one-level high-pressure plunger pump, its one-level dish tubular membrane post one-level permeate liquid gets into second grade dish tubular membrane post, one-level concentrate gets into the concentrate reservoir, the second grade concentrate backward flow of second grade dish tubular membrane post gets into the DTRO intake pump inlet tube, second grade permeate liquid gets into the degasser, the degasser is connected and is got into the clean water jar.
7. The desulfurization and denitrification wastewater treatment device according to claim 6, wherein: and a scale inhibitor adding device and a NaOH adding device are arranged between the sand filter and the core filter.
8. The desulfurization and denitrification wastewater treatment device according to claim 7, wherein: and a primary servo motor control valve and a secondary servo motor control valve are respectively arranged on the concentrated solution conveying pipes of the primary concentrated solution and the secondary concentrated solution.
9. The desulfurization and denitrification wastewater treatment device according to claim 7, wherein: and a second-stage high-pressure plunger pump and a second-stage high-pressure energy accumulator are arranged on the connecting pipe of the first-stage disc tubular membrane column and the second-stage disc tubular membrane column.
10. the desulfurization and denitrification wastewater treatment apparatus according to any one of claims 6 to 9, wherein: and a circulating pump is arranged on a water inlet pipe of the DTRO membrane module, and a shock absorber is arranged behind each plunger pump in the DTRO membrane module.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201822077643.2U CN209797625U (en) | 2018-12-11 | 2018-12-11 | Desulfurization and denitrification wastewater treatment device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201822077643.2U CN209797625U (en) | 2018-12-11 | 2018-12-11 | Desulfurization and denitrification wastewater treatment device |
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| Publication Number | Publication Date |
|---|---|
| CN209797625U true CN209797625U (en) | 2019-12-17 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201822077643.2U Expired - Fee Related CN209797625U (en) | 2018-12-11 | 2018-12-11 | Desulfurization and denitrification wastewater treatment device |
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| CN (1) | CN209797625U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114409142A (en) * | 2022-02-16 | 2022-04-29 | 莱特莱德(上海)技术有限公司 | High-hardness wastewater softening treatment device and method |
-
2018
- 2018-12-11 CN CN201822077643.2U patent/CN209797625U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114409142A (en) * | 2022-02-16 | 2022-04-29 | 莱特莱德(上海)技术有限公司 | High-hardness wastewater softening treatment device and method |
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
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Granted publication date: 20191217 Termination date: 20211211 |