CN112093973A - Method and equipment for treating coal-fired sludge coupling wastewater of thermal power plant - Google Patents
Method and equipment for treating coal-fired sludge coupling wastewater of thermal power plant Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
- C02F11/04—Anaerobic treatment; Production of methane by such processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
Abstract
The invention provides a method and equipment for treating coal-fired sludge coupling wastewater of a thermal power plant, which comprises the following steps: s1, feeding the coal-fired sludge coupling wastewater with high ammonia nitrogen and COD into a regulating tank; s2, anaerobic degradation; s3, aerobic degradation; s5, treating the wastewater in a secondary sedimentation tank and then entering an intermediate water tank; s6, further processing by a modified regenerated membrane device; s7, starting a cleaning program; s8, backwashing the regenerated membrane by the modified regenerated membrane device; and S9, chemically cleaning the modified regenerated membrane device. And S10, introducing the effluent of the modified regenerated membrane device into a clean water tank, and discharging and recycling the clean water which reaches the standard through the clean water. The invention has the characteristics of high treatment efficiency and low cost.
Description
Technical Field
The invention relates to the field of thermal power plant coal-fired sludge coupling wastewater treatment, and relates to a thermal power plant coal-fired sludge coupling wastewater treatment method and equipment.
Background
China has a large population and a huge industrial scale. In recent years, the domestic and industrial sludge yield is increased sharply, and the coal-fired coupled sludge power generation technology is popularized in the national thermal power generation industry in order to treat sludge on a large scale. In order to reduce the co-combustion energy consumption, the sludge and the fire coal are dried before coupled combustion, so that the moisture content in the sludge is reduced to be below about 30 percent. Generally, sludge drying employs a steam dehydration process. In the process, water in the sludge is heated and evaporated, and condensed water is formed after cooling, has the characteristics of high COD, BOD and ammonia nitrogen, and belongs to high-concentration organic wastewater. If the traditional biochemical process is adopted for treatment, most of COD, BOD, ammonia nitrogen and suspended matters in the coal-fired sludge coupling wastewater can be degraded, but the wastewater still can hardly stably reach the national comprehensive sewage discharge standard.
The traditional membrane treatment processes such as ultrafiltration and reverse osmosis and the like are combined with a biochemical method to have good treatment effect on coal-fired sludge coupling wastewater of a thermal power plant, but the membrane has short service cycle and high treatment cost per ton of water. The efficient and low-cost membrane treatment process and equipment are urgently developed. On the other hand, a large number of reverse osmosis membranes are replaced due to reduction of the desalination rate of the make-up water produced by the boiler of the thermal power plant every year, and the residual value of the reverse osmosis membranes is not developed.
Based on the situation, the invention provides a method and equipment for treating coal-fired sludge coupling wastewater of a thermal power plant by combining a biochemical method with a modified regenerated membrane filtration process, wherein a waste reverse osmosis membrane is modified and then used for treating the coal-fired sludge coupling wastewater of the thermal power plant, so that the treatment cost can be greatly reduced.
In order to overcome the defects of the conventional thermal power plant coal-fired sludge coupling wastewater treatment, the invention designs the thermal power plant coal-fired sludge coupling wastewater treatment method and the thermal power plant coal-fired sludge coupling wastewater treatment equipment with high efficiency and low cost.
Disclosure of Invention
The invention provides a method and equipment for treating high-efficiency and low-cost coal-fired sludge coupling wastewater of a thermal power plant, aiming at solving the problems in the prior art.
The purpose of the invention can be realized by the following technical scheme:
a method for treating coal-fired sludge coupling wastewater of a thermal power plant comprises the following steps:
s1, feeding the coal-fired sludge coupling wastewater with high ammonia nitrogen and COD into a regulating tank, regulating the water temperature to 12-38 ℃ through natural cooling, and regulating the pH value to 7-9 by using industrial hydrochloric acid;
s2, anaerobic degradation: the wastewater lift pump conveys the high-concentration coal-fired sludge coupling wastewater to the anaerobic tank, so that the organic matters in the high-concentration coal-fired sludge coupling wastewater are subjected to anaerobic degradation reaction under the action of denitrifying bacteria, and a stirrer in the anaerobic tank runs uninterruptedly;
s3, aerobic degradation: the coal-fired sludge coupling wastewater after the anaerobic reaction treatment flows from the bottom of the anaerobic tank to the aerobic tank, overflows to the secondary sedimentation tank, flows through the honeycomb inclined tube in the secondary sedimentation tank from bottom to top, the activated sludge in the secondary sedimentation tank is pumped back to the anaerobic tank by a sludge pump, and the sludge is discharged through a sludge discharge pipeline according to the determined sludge age;
s5, the coal-fired sludge coupling wastewater treated by the secondary sedimentation tank automatically flows into an intermediate water tank;
s6, conveying the coal-fired sludge coupling wastewater in the intermediate water tank to a modified regenerated membrane device for further treatment at a pressure of 0.3MPa through an intermediate water pump;
s7, when the differential pressure on the differential pressure gauge is larger than or equal to 100kPa, starting a cleaning program, and discharging cleaning water to an anaerobic tank through a self-cleaning filter blow-down valve;
s8, backwashing the regenerated membrane for 1min by the modified regenerated membrane device, controlling the flow rate to be 50t/h, and discharging backwash water to an adjusting tank by a backwash water discharge valve;
and S9, chemically cleaning the modified regenerated membrane device.
S10, introducing the effluent of the modified regenerated membrane device into a clean water tank: a COD instrument and an ammonia nitrogen instrument are arranged in the clean water tank, when the COD is more than 60mg/L or the ammonia nitrogen is more than 15mg/L, sodium hypochlorite solution is added into the clean water tank for further degradation, and the clean water reaching the standard is discharged through the clean water and recycled.
As a further improvement of the scheme, the dissolved oxygen of the wastewater in the aerobic tank in S3 is 2.5-4.0 mg/L.
As a further improvement of the scheme, the modified regeneration membrane device comprises a membrane shell and a modified regeneration membrane, the modified regeneration membrane is arranged in the membrane shell, and the preparation method of the modified regeneration membrane comprises the following steps:
1. screening an 8040 reverse osmosis membrane which is judged to be invalid due to low desalination rate;
2. soaking in hydrochloric acid solution with the pH value of 2, taking out after carbon dioxide bubbles are not generated in the hydrochloric acid solution any more, and removing a scale layer in the reverse osmosis membrane;
3. and (3) respectively soaking the acid-washed reverse osmosis membrane in 2% sodium hypochlorite solution for about 24 hours, washing the reverse osmosis membrane with desalted water at low pressure until the residual chlorine in the water is less than or equal to 0.05mg/L, and oxidizing the reverse osmosis membrane to expand and shape the membrane pores.
As a further improvement of this solution, in step 9, when the inter-stage differential pressure of the modified and regenerated membrane device rises to 0.10MPa, a chemical cleaning solution is configured in a chemical cleaning water tank, and the modified and regenerated membrane device is chemically cleaned by a chemical cleaning pump, and the cleaning step is as follows:
1. preparing 2% FC820 solution, closing an inlet adjusting valve, an outlet valve and a concentrated water reflux valve of the modified regeneration membrane device, opening an inlet valve and an outlet valve of a chemical cleaning pump, starting the chemical cleaning pump to circularly clean the modified regeneration membrane device for 1h, soaking for 1h, and repeating twice;
2. injecting industrial water into the chemical cleaning box, discharging and flushing the modified regenerated membrane device, and discharging the effluent to a clean water tank until the pH of the effluent is close to neutral.
As a further improvement of the scheme, in the step 1, the temperature of the coal-fired sludge coupling wastewater in the regulating tank is 16-34 ℃; and when the pH value of the coal-fired sludge coupling wastewater in the regulating tank is more than 9, adding 31% of industrial hydrochloric acid, and controlling the pH value to be 7-8.5.
According to a further improvement of the scheme, in the step S1, the pH value is 8.1, and the temperature of the coal-fired sludge coupling wastewater in the regulating tank is 26-29 ℃.
A coal-fired sludge coupling waste water's of thermal power plant treatment facility includes:
one side of the adjusting tank is provided with a sludge coupling wastewater inlet pipe and an acid inlet pipe, and the other side of the adjusting tank is provided with a wastewater conveying pipeline;
one end of the waste water conveying pipeline is communicated with the anaerobic tank;
the bottom of the aerobic tank is communicated with the anaerobic tank, and an aeration pipeline is arranged at the bottom of the aerobic tank and is connected with a Roots blower;
the secondary sedimentation tank is communicated, a guide plate and a honeycomb inclined pipe are arranged in the secondary sedimentation tank, the guide plate is arranged on one side of the honeycomb inclined pipe, a sludge return pipeline is arranged at the bottom of the secondary sedimentation tank, one end of the sludge return pipeline is communicated with the anaerobic tank, and a sludge return pump and a sludge discharge pipeline are arranged on the sludge return pipeline;
the middle water tank is communicated with the secondary sedimentation tank;
the modified regeneration membrane device comprises a plurality of membrane tubes connected in parallel, the modified regeneration membrane device is communicated with a water outlet pool through a water outlet pipeline of an intermediate pool, a self-cleaning filter is arranged at the upper part of the modified regeneration membrane device and the inlet of the anaerobic pool, and a sewage discharge pipeline of the self-cleaning filter is communicated to the anaerobic pool;
the clean water tank is communicated with the modified regenerated membrane device, an online liquid level meter, an online nitrogen tester and an online COD tester are arranged on the clean water tank, and a hypochlorous acid conveying pipeline and a clean water tank output pipeline are also arranged on the clean water tank;
modified regeneration membrane device cleaning system including chemical cleaning tank and backwash drain line, is equipped with the backwash drain valve on the backwash drain line, and modified regeneration membrane device cleaning system passes through backwash drain line and equalizing basin intercommunication, and chemical cleaning tank outlet pipeline one and modified regeneration membrane device entry intercommunication, chemical cleaning tank outlet pipeline two and modified regeneration membrane device export intercommunication, chemical cleaning tank inlet pipeline and clean water basin output pipeline intercommunication.
As a further improvement of the scheme, the adjusting tank is a sunken concrete closed water tank, an online submerged pH meter is arranged in the adjusting tank, and a wastewater lifting pump is arranged on the wastewater conveying pipeline.
As a further improvement of the scheme, the anaerobic tank is a concrete water tank, and a mechanical submerged stirrer is arranged in the anaerobic tank.
As a further improvement of the scheme, the aerobic tank is a concrete open water tank, and the opening density of the branch pipe of the aeration pipeline is 2.5cm2And m, arranging an elastic filler in the aerobic tank.
As a further improvement of the scheme, the precision of the filter screen of the self-cleaning filter is 100 microns, a pressure difference meter is arranged at an inlet and an outlet of the self-cleaning filter, and a blowdown valve of the self-cleaning filter is arranged on the filtered water side.
Compared with the prior art, the invention has the following beneficial effects:
1) aiming at the water quality characteristic of the coal-fired sludge coupling wastewater, a biochemical method and a membrane filtration process are combined, and the coal-fired sludge coupling wastewater is deeply treated, so that the coal-fired sludge coupling wastewater of a thermal power plant is qualified and recycled, and the method specifically comprises the following steps: firstly, performing primary treatment on coal-fired sludge coupling wastewater through an anaerobic/aerobic tank and a secondary sedimentation tank; the coupling wastewater of the coal-fired sludge after biochemical treatment enters a modified regeneration membrane device for secondary treatment, and finally a small amount of sodium hypochlorite solution is added for qualified treatment to realize recycling;
2) according to the method for modifying and regenerating the waste reverse osmosis membrane, the modified and regenerated membrane is used for replacing a new membrane, so that the treatment cost is greatly reduced;
3) the aim of deeply degrading COD, ammonia nitrogen and suspended matters in the coal-fired sludge coupling wastewater is achieved at lower cost, and the comprehensive wastewater discharge standard of China (GB8978-1996) is stably achieved;
4) the upper limits of COD and ammonia nitrogen concentration in the coal-fired sludge coupling wastewater of the thermal power plant which can be treated by the invention are 1450mg/L and 350mg/L respectively (BOD is 25-40% of COD), and the final COD and ammonia nitrogen concentration of the effluent are stably less than 60mg/L and 15mg/L respectively.
Drawings
FIG. 1 is a schematic structural diagram of a thermal power plant coal-fired sludge coupled wastewater treatment facility according to the present invention.
Detailed Description
The technical solution of the present invention is further described below with reference to the following embodiments and the accompanying drawings.
A coal-fired sludge coupling waste water's of thermal power plant treatment facility includes:
a regulating tank 10, wherein one side of the regulating tank 10 is provided with a sludge coupling wastewater inlet pipe 11 and an acid inlet pipe 12, and the other side of the regulating tank 10 is provided with a wastewater conveying pipeline 13;
one end of the waste water conveying pipeline 13 is communicated with the anaerobic tank 20;
the bottom of the aerobic tank 30 is communicated with the anaerobic tank 20, the bottom of the aerobic tank 20 is provided with an aeration pipeline 31, and the aeration pipeline 31 is connected with a Roots blower 32;
the upper part of the secondary sedimentation tank 40 is communicated with the aerobic tank 30, a guide plate 41 and a honeycomb inclined tube 42 are arranged in the secondary sedimentation tank, the guide plate 41 is arranged on one side of the honeycomb inclined tube 42, a sludge return pipeline 43 is arranged at the bottom of the secondary sedimentation tank 40, one end of the sludge return pipeline 43 is communicated with the anaerobic tank 20, and a sludge return pump 44 and a sludge discharge pipeline 45 are arranged on the sludge return pipeline 43;
the intermediate water tank 50, the intermediate water tank 50 communicates with the secondary sedimentation tank 40;
the modified regeneration membrane device 60 comprises a plurality of membrane pipes which are connected in parallel, the modified regeneration membrane device 60 is communicated with the water outlet pool 50 through a water outlet pipeline of the middle water pool, the upper part of the modified regeneration membrane device 60 is communicated with the anaerobic pool 20, a self-cleaning filter 61 is arranged at the inlet of the modified regeneration membrane device 60, a self-cleaning filter sewage discharge pipeline 62 is arranged on the self-cleaning filter 61, and the self-cleaning filter sewage discharge pipeline 62 is communicated to the anaerobic pool 20;
the clean water tank 70 is communicated with the modified regenerated membrane device 60, the clean water tank 70 is provided with an online liquid level meter 71, an online nitrogen tester 72 and an online COD tester 73, and the clean water tank 70 is also provided with a hypochlorous acid conveying pipeline 74 and a clean water tank output pipeline 75;
modified regeneration membrane device cleaning system 80, including chemical cleaning tank 81 and backwash drain line 82, be equipped with backwash drain valve 821 on the backwash drain line 82, modified regeneration membrane device cleaning system 80 passes through backwash drain line 82 and equalizing basin 10 intercommunication, and chemical cleaning tank outlet pipeline one 83 and modified regeneration membrane device entry intercommunication, chemical cleaning tank outlet pipeline two 84 and modified regeneration membrane device export intercommunication, chemical cleaning tank inlet pipeline 85 and clean water basin output pipeline 75 intercommunication.
As a further preferred embodiment, the adjusting tank 10 is a sunken concrete closed water tank, an online submerged pH meter 14 is arranged in the adjusting tank, and a wastewater lifting pump 131 is arranged on the wastewater conveying pipeline 13.
In the embodiment, the specification of the regulating tank 10 is 8000X 4000mm, 1 DN25 acid inlet valve is arranged on the acid inlet pipe 12, the model is Q41F-10, and an online submerged pH meter 14 is arranged in the regulating tank 10 and used for monitoring the pH value of sludge coupling wastewater in the tank. The wastewater lifting pump 131 is a self-control self-priming pump, the model is 80DWXB-AD, and the rated flow is 25m3And h, is arranged at the upper part of the regulating reservoir 10. The outlet pipe of the wastewater lift pump 131 is provided with 1 DN80 isolation valve each, and the model is J41F-10. The specification of the waste water conveying pipeline 13 is DN80 and the material is 316L.
In a further preferred embodiment, the anaerobic tank 20 is a concrete pool, and a mechanical underwater agitator 21 is provided in the anaerobic tank 20.
In this embodiment, the anaerobic tank 20 has a specification of 8000 × 4000 × 4000 mm; the submerged mixer was 316L in total. By arranging the stirrer 21 in the anaerobic tank 20, the stirrer 21 runs uninterruptedly, so that the sludge is fully contacted with the coal-fired sludge coupling wastewater, and the denitrification reaction is favorably and smoothly carried out.
As a further preferred embodiment, the aerobic tank 30 is a concrete open pond, and the opening density of the branch pipe of the aeration pipeline 31 is 2.5cm2And/m, elastic fillers are arranged in the aerobic tank 30.
As a further preferred embodiment, an on-line dissolved oxygen meter 33 is provided in the aerobic tank 30, and the dissolved oxygen meter 33 is used for monitoring the dissolved oxygen level in the water in the aerobic tank.
In this embodiment, the aerobic tank 30 is a concrete open water tank with a specification of 8000 × 4000 × 4000mm, the bottom of the aerobic tank 30 is provided with an aeration pipeline 31, and the specification of the main pipe isDN80, material 316L, branch specification DN32, material 316L, and the density of the openings on the branch pipes is 2.5cm2And m, round hole and upward direction.
Moreover, the model KB6008 of the Roots blower 32 provides power for aeration of the aerobic tank 30, 1 DN100 check valve and 1 isolating valve are respectively arranged at the outlet of the blower, and the models are H41H and J41H-16 respectively; the aerobic tank 30 is internally provided with elastic filler made of PVDF and arranged at a density of 2 groups/m2The elastic filler is used for providing an attachment carrier for strains in the activated sludge. The dissolved oxygen level in the water in the aerobic tank is monitored by an on-line dissolved oxygen meter 33 provided in the aerobic tank 30.
As a further preferred embodiment, both the inlet and outlet pipes of the sludge-return pump 44 are provided with isolation valves.
In this embodiment, the guide plate 41 arranged in the secondary sedimentation tank 40 flows through the honeycomb inclined tube 42 in the secondary sedimentation tank 40 from bottom to top under the action of the guide plate 41, and about 70% of suspended matters are precipitated in the secondary sedimentation tank in the process. The guide plate 41 in the secondary sedimentation tank 40 is made of 316L material, the honeycomb inclined tube 42 is made of PP material, and the drift diameter is 35 mm.
Furthermore, part of the activated sludge in the secondary sedimentation tank 40 is pumped back to the anaerobic tank 20 by a sludge reflux pump 44, so that the activated sludge alternately circulates under anaerobic and aerobic environments, the reflux ratio is adjusted by an outlet adjusting valve of the sludge pump, and then a certain amount of sludge is periodically discharged into the sludge concentration tank according to the measured sludge age.
More specifically, the anaerobic tank 20 is communicated with the aerobic tank 30 at the position 100mm away from the tank bottom on the side surface of the tank wall, and the aerobic tank 30 is communicated with the secondary sedimentation tank 40 at the position 2800mm away from the tank bottom on the side surface of the tank wall; the model of the sludge reflux pump 44 is 65AWFB-B, 1 DN125 isolation valve is arranged on the inlet pipe, the model is D41F-10, 1 DN125 isolation valve is arranged on the outlet pipe, and the model is Z41F-10. The starting point of the sludge backflow is the bottom of the secondary sedimentation tank 40, and the end point is the anaerobic tank 20. The specification of the sludge return pipeline is DN80, the material is 316L, the sludge discharge pipeline is connected with the sludge return pipeline gauge through a DN80 manual isolation valve, a DN125 sludge discharge valve 451 is arranged behind the sludge pump, the model is Z41F-10, and the sludge discharge valve 451 can discharge the sludge without activity to the system regularly.
As a further preferred embodiment, the intermediate water tank 50 is a concrete open water tank, and an intermediate water pump 51 is arranged on a water outlet pipeline of the intermediate water tank 50.
In this embodiment, the specification of the intermediate water tank 50 is 4000 × 3000 × 4000mm, the intermediate water pump 51 is a corrosion-resistant centrifugal pump, model number GH80-100, and rated flow rate is 25m3The head is 35m, the inlet pipe of the middle water pump 51 is provided with a DN80 isolating valve 1 with the model D41F-10; the outlet pipe of the intermediate water pump 51 is provided with DN100 isolation valves 1 with model J41F-10.
As a further preferred embodiment, the screen accuracy of the self-cleaning filter 61 is 100 μm, a pressure difference gauge 63 is provided at the inlet/outlet of the self-cleaning filter, and a drain valve 64 for the self-cleaning filter is provided at the filtered water side.
In the embodiment, one self-cleaning filter 61 is arranged at the inlet of the modified regeneration membrane device, the model is YNF-XF-X01-80, the material is 316L, and the precision of the filter screen is 100 mu m. A pressure difference meter is arranged at an inlet and an outlet of the self-cleaning filter, a sewage valve of the self-cleaning filter is arranged on a water filtering side, and when the differential pressure is larger than or equal to 100kPa, a cleaning program is automatically started. The cleaning water is discharged to the anaerobic tank through the self-cleaning filter blowdown valve;
specifically, the modified regenerated membrane device 60 is vertically placed in parallel by taking six cylindrical glass fiber reinforced plastic cylinders as a membrane shell, the inner diameter of the membrane shell is 203mm, the length of the membrane shell is 8040mm, and the modified regenerated membrane device is suitable for 8040 type reverse osmosis membranes which are mainstream in industrial water production at present. The modified regenerated membranes are respectively arranged in the membrane shells, and the modified regenerated membrane device 60 is provided with an inlet valve and an outlet valve, wherein the types of the inlet valve and the outlet valve are respectively T941F-10 and D941F-10.
As a further preferred embodiment, a clean water pump 76 is arranged on the clean water tank output pipeline 75, and the clean water pump 76 is an automatic control self-priming pump.
In this embodiment, the clean water tank 70 is a concrete open water tank with a specification of 4000 × 3000 × 4000mm, and the produced water of the modified regenerated membrane device enters the clean water tank through a DN80 pipeline. The clean water tank is internally provided with an online liquid level meter 71, an online nitrogen tester 72 and an online COD tester 73 which are used for detecting the COD and the ammonia nitrogen concentration of the effluent, namely monitoring the water quality in the clean water tank. The online liquid level meter 71 is used for detecting the liquid level of the clean water tank.
In particular, QingThe water pump 76 is a self-control self-priming pump with the model number of 80DWXB-AD and the rated flow of 25m3And h, installing the water tank part.
In a further preferred embodiment, a backwash pump 851 is provided on the chemical cleaning tank inlet line 85, and a chemical cleaning pump 831 is provided on the chemical cleaning tank outlet line one 83.
In this embodiment, the chemical cleaning tank 81 is made of PP material and has a volume of 3m3. The back washing pump 851 is a corrosion-resistant centrifugal pump with model GH100-125 and rated flow 50m3The head is 50m, the inlet pipe is provided with one DN100 isolating valve with the model D41F-10, and the outlet pipe is provided with one DN125 isolating valve with the model J41F-10; during backwashing, backwash water flows in from the water production side of the modified regeneration membrane device and flows out from the water inlet side of the modified regeneration membrane device under the action of a backwashing pump 851 and is discharged into the regulating tank 10 through a backwashing drainage valve.
Specifically, the chemical cleaning pump 831 is a vertical corrosion-resistant centrifugal pump, the model is 80ZLF, and the rated flow is 30m3And the head is 25m, the inlet pipe is provided with 1 DN80 isolating valve with the model D41F-10, and the outlet pipe is provided with 1 DN100 isolating valve with the model J41F-10.
The traditional membrane treatment processes such as ultrafiltration and reverse osmosis and the like are combined with a biochemical method to have good treatment effect on coal-fired sludge coupling wastewater of a thermal power plant, but the membrane has short service cycle and high treatment cost per ton of water. The efficient and low-cost membrane treatment process and equipment are urgently developed.
A treatment device for coal-fired sludge coupling wastewater of a thermal power plant comprises the following steps:
s1, feeding the coal-fired sludge coupling wastewater with high ammonia nitrogen and COD into an adjusting tank 10, adjusting the water temperature to 12-38 ℃ through natural cooling, and adjusting the pH value to 7-9 by using industrial hydrochloric acid;
s2, anaerobic degradation: the wastewater lift pump 13 conveys the high-concentration coal-fired sludge coupling wastewater to the anaerobic tank 20, so that the organic matters in the high-concentration coal-fired sludge coupling wastewater are subjected to anaerobic degradation reaction under the action of denitrifying bacteria, and the stirrer 21 in the anaerobic tank 20 runs uninterruptedly;
s3, aerobic degradation: the coal-fired sludge coupling waste water after the anaerobic reaction treatment flows to the aerobic tank 30 from the bottom of the anaerobic tank 20, organic matters in the waste water are subjected to aerobic degradation reaction under the action of nitrobacteria, and aeration is carried out in the aerobic tank through an aeration Roots blower 32;
as a further preferred embodiment, the dissolved oxygen of the wastewater in the aerobic tank 30 in S3 is 2.5-4.0 mg/L.
In step 3, under the action of nitrifying bacteria, organic matters in the wastewater are subjected to aerobic degradation reaction, and aeration is performed in the aerobic tank through the aeration Roots blower 32 so as to improve the dissolved oxygen in the coal-fired sludge coupled wastewater. Dissolved oxygen is controlled by the Roots blower 32, and the specific range is 2.5-4.0 mg/L.
S4, removing suspended matters: the coal-fired sludge coupling wastewater after the aerobic reaction treatment overflows from the aerobic tank 30 to a secondary sedimentation tank 40, flows through a honeycomb inclined pipe 41 in the secondary sedimentation tank 40 from bottom to top through a guide plate 41, an activated sludge in the secondary sedimentation tank 40 is pumped back to the anaerobic tank by a sludge pump 44, and the sludge is discharged through a sludge discharge pipeline 45 according to the determined sludge age;
the treatment in step 4 causes about 70% of the suspended matter to settle in the secondary sedimentation tank 40. The guide plate in the secondary sedimentation tank is made of 316L material, and the drift diameter of the honeycomb inclined tube is 35 mm. Part of the activated sludge in the secondary sedimentation tank 40 is pumped back to the anaerobic tank 20 by a sludge pump 44, so that the activated sludge alternately circulates under anaerobic and aerobic environments, and the reflux ratio is adjusted by an outlet adjusting valve of the sludge pump. And (4) regularly discharging quantitative sludge into the sludge concentration tank according to the measured sludge age.
S5, the coal-fired sludge coupling wastewater treated by the secondary sedimentation tank 40 automatically flows into the intermediate water tank 42;
s6, conveying the coal sludge coupling wastewater in the intermediate water tank 42 to the modified regenerated membrane device 60 for further treatment at a pressure of 0.3MPa through the intermediate water pump 51.
As a further preferred embodiment, the modified regenerated membrane device 60 comprises a membrane shell and a modified regenerated membrane, wherein the modified regenerated membrane is arranged in the membrane shell, and the preparation method of the modified regenerated membrane is as follows:
1. screening an 8040 reverse osmosis membrane which is judged to be invalid due to low desalination rate;
2. soaking in hydrochloric acid solution with the pH value of 2, taking out after carbon dioxide bubbles are not generated in the hydrochloric acid solution any more, and removing a scale layer in the reverse osmosis membrane;
3. soaking the acid-washed reverse osmosis membrane in 2% sodium hypochlorite solution for about 24h respectively, washing with desalted water at low pressure until the residual chlorine in the water is less than or equal to 0.05mg/L, oxidizing the reverse osmosis membrane to expand and shape the membrane pores;
in this embodiment, the modified regenerated membrane device 60 is formed by vertically placing six cylindrical glass fiber reinforced plastic cylinders as membrane shells in parallel, wherein the inner diameter of the membrane shells is 203mm, the length of the membrane shells is 8040mm, and the modified regenerated membrane device is suitable for 8040 type reverse osmosis membranes which are mainstream in industrial water production at present.
Specifically, the method comprises the following steps: the modified regenerated membrane is prepared by screening 8040 type reverse osmosis membranes which are judged to be invalid due to low desalination rate, selecting reverse osmosis membranes with light mechanical damage degree for modification regeneration, soaking the reverse osmosis membranes in hydrochloric acid solution with pH of 2, and taking out the reverse osmosis membranes when carbon dioxide bubbles are not generated in the hydrochloric acid solution. This step is intended to remove the scale layer from the membrane surface. Then, the reverse osmosis membranes after acid cleaning are respectively soaked in 2 percent sodium hypochlorite solution for about 24 hours, and the reverse osmosis membranes are washed by desalted water under low pressure until the residual chlorine in the water is less than or equal to 0.05 mg/L. The step aims to perform forced oxidation on the polyurethane structure of the reverse osmosis membrane, induce the membrane pores to expand and shape.
Too long a sodium hypochlorite solution soaking time or a sodium hypochlorite solution concentration exceeding 2% may result in damage to the membrane surface or too large a modified pore size. Repeated tests show that the filtration precision of the regenerated membrane prepared by the method is about 0.001-0.01 μm. Under the action of osmotic pressure, water molecules in the coal-fired sludge coupling wastewater pass through the regeneration membrane, and particles with the particle size of more than or equal to 0.01 mu m and part of macromolecular organic matters are intercepted by the regeneration membrane and are recycled to the anaerobic tank 20 along with the concentrated water.
During specific operation, the water inlet flow of the modified regeneration membrane device is regulated by an inlet regulating valve of the modified regeneration device. When the water inlet flow of the modified regeneration membrane device is 20t/h, the pressure is 0.3Mpa and the water temperature is 25 ℃, the recovery rate is about 84 percent.
S7, when the differential pressure on the differential pressure gauge 63 is larger than or equal to 100kPa, starting a cleaning program, and discharging cleaning water to the anaerobic tank 20 through the self-cleaning filter blow-down valve 64;
in step 7, in order to reduce the damage of the large-particle-size particles to the modified regeneration membrane, a self-cleaning filter 61 is arranged in front of the modified regeneration membrane device. The filtering precision of the self-cleaning filter 61 is 100 μm, a pressure difference meter 63 is arranged at the inlet and the outlet, and when the pressure difference is larger than or equal to 100kPa, the cleaning program is started automatically. The cleaning water is discharged to the anaerobic tank through a self-cleaning filter blow-down valve.
S8, starting a backwashing pump 851 to backwash the regenerated membrane for 1min when the modified regenerated membrane device 60 runs for 2h every time, controlling the flow rate to be 50t/h, and discharging backwash water from a backwash water discharge valve 821 to an adjusting tank 10;
and S9, chemically cleaning the modified regenerated membrane device.
In a further preferred embodiment, when the pressure difference between the sections of the modified regeneration membrane device rises to 0.10MPa, a chemical cleaning solution is configured in the chemical cleaning water tank 81, and the modified regeneration membrane device 60 is chemically cleaned by the chemical cleaning pump 831, wherein the cleaning step is as follows:
1. preparing 2% FC820 solution, closing an inlet adjusting valve, an outlet valve and a concentrated water reflux valve of the modified regeneration membrane device 60, opening an inlet valve and an outlet valve of a chemical cleaning pump, starting the chemical cleaning pump to circularly clean the modified regeneration membrane device for 1h, soaking for 1h, and repeating for 2 times;
2. injecting industrial water into the chemical cleaning tank 81, discharging and flushing the modified regenerated membrane device 60, and discharging the effluent to the clean water tank 70 until the pH of the effluent is close to neutral;
s10, introducing the effluent of the modified regenerated membrane device 60 into a clean water tank 70: a COD instrument and an ammonia nitrogen instrument are arranged in the clean water tank 70, when the COD is more than 60mg/L or the ammonia nitrogen is more than 15mg/L, sodium hypochlorite solution is added into the clean water tank 70 for further degradation, and the clean water reaching the standard is discharged through the clean water 76 and recycled.
In the step 10, through repeated tests, the final effluent COD and ammonia nitrogen concentration of the system are respectively and stably less than 60mg/L and 15 mg/L.
As a further preferred embodiment, in step S1, the temperature of the coal sludge coupling wastewater in the regulating reservoir 10 is 16-34 ℃; and when the pH value of the coal-fired sludge coupling wastewater in the regulating tank is more than 9, adding 31% of industrial hydrochloric acid, and controlling the pH value to be 7-8.5.
By adjusting the temperature and the pH value, the coal-fired sludge coupling wastewater is in an active area of nitrifying bacteria and denitrifying bacteria, and COD and ammonia nitrogen are reduced as much as possible in anaerobic and aerobic treatment links.
As a further preferable example, in step S1, the pH is 8.1, and the temperature of the coal-fired sludge coupling wastewater in the adjusting tank 10 is 26 to 29 ℃.
In this embodiment, when the pH is 8.1 and the temperature of the coal sludge coupled wastewater in the adjusting tank 10 is within the range of 26 to 29 ℃, the ammonia nitrogen removal efficiency in steps S1 to S5 is the best, about 65.2%, and the COD degradation rate is about 69 to 75%.
In step S2, the frequency of the wastewater lift pump is automatically changed along with the liquid level in the regulating reservoir, the liquid level in the regulating reservoir is controlled to be 1.5-3.2 m, and the flow is less than or equal to 21.5m3/h。
As a further preferred embodiment, in step S6, the reflux ratio of the sludge is controlled to be 2: 1.
In this embodiment, in step 6, the reflux ratio of the sludge is controlled to be 2:1, and about 5t of sludge with a water content of about 98.5% is discharged outwards every 14 days according to the measured age of the sludge, so as to ensure that the amount of activated sludge in the aerobic tank 30 is in a proper proportion of 18%.
As a further preferred embodiment, the flow rate of the inflow water of the reforming regeneration membrane apparatus 60 is 20t/h, the pressure is 0.3MPa, and the water temperature is 25 ℃.
In this example, a large number of experiments have shown that the recovery rate of the regenerated membrane device 60 is about 84% at a water inlet flow rate of 20t/h, a pressure of 0.3MPa and a water temperature of 25 ℃. In the process, as the organic macromolecules are further removed, the COD and ammonia nitrogen in the sludge coupling wastewater can be continuously reduced by about 25 percent and 18 percent respectively, and the suspended matters in the effluent are stably less than 5 mg/L.
Compared with the prior art, the invention has the following beneficial effects:
1) aiming at the water quality characteristic of the coal-fired sludge coupling wastewater, a biochemical method and a membrane filtration process are combined, and the coal-fired sludge coupling wastewater is deeply treated, so that the coal-fired sludge coupling wastewater of a thermal power plant is qualified and recycled, and the method specifically comprises the following steps: firstly, performing primary treatment on coal-fired sludge coupling wastewater through an anaerobic/aerobic tank and a secondary sedimentation tank; the coupling wastewater of the coal-fired sludge after biochemical treatment enters a modified regeneration membrane device for secondary treatment, and finally a small amount of sodium hypochlorite solution is added for qualified treatment to realize recycling;
2) according to the method for modifying and regenerating the waste reverse osmosis membrane, the modified and regenerated membrane is used for replacing a new membrane, so that the treatment cost is greatly reduced;
3) the aim of deeply degrading COD, ammonia nitrogen and suspended matters in the coal-fired sludge coupling wastewater is achieved at lower cost, and the comprehensive wastewater discharge standard of China (GB8978-1996) is stably achieved;
4) the upper limits of COD and ammonia nitrogen concentration in the coal-fired sludge coupling wastewater of the thermal power plant which can be treated by the invention are 1450mg/L and 350mg/L respectively (BOD is 25-40% of COD), and the final COD and ammonia nitrogen concentration of the effluent are stably less than 60mg/L and 15mg/L respectively.
Example 1
Coupling coal-fired sludge with wastewater COD1400mg/L and ammonia nitrogen 350mg/L, adjusting pH to 9.5, and adding acid to adjust pH to 8;
controlling the dissolved oxygen in the coal-fired sludge coupling wastewater in the aerobic tank to be 2.5mg/L, and controlling the primary treatment effluent COD420mg/L and the ammonia nitrogen 120 mg/L;
controlling the water inlet flow of the modified regenerated membrane device to be 20t/h, the pressure to be 0.3Mpa, the recovery rate to be 84 percent, the effluent COD of the secondary treatment to be 120mg/L and the ammonia nitrogen to be 25mg/L, adding a 10 percent sodium hypochlorite solution into the clear water tank for treatment and then recycling the treated effluent to the original water tank.
Example 2
Coupling coal-fired sludge with wastewater COD1200mg/L and ammonia nitrogen 250mg/L, wherein the pH value is 8.9, and adding acid to adjust the pH value to 8.2;
controlling the dissolved oxygen in the coal-fired sludge coupling wastewater in the aerobic tank to be 3mg/L, and controlling the primary treatment effluent COD to be 300mg/L and the ammonia nitrogen to be 80 mg/L;
controlling the water inlet flow of the modified regenerated membrane device to be 22t/h, the pressure to be 0.3Mpa, the recovery rate to be 82 percent, the effluent COD of the secondary treatment to be 55mg/L and the ammonia nitrogen to be 11.8mg/L, and directly recycling the treated clean water to a plant flushing water system.
The membrane modification regeneration treatment method comprises the following steps:
1) screening 8040 type reverse osmosis membranes which are judged to be invalid due to low desalination rate, and selecting reverse osmosis membranes with lighter mechanical damage degree for modification and regeneration;
2) soaking the reverse osmosis membrane in a hydrochloric acid solution with the pH value of 2, wherein a large amount of carbon dioxide bubbles are generated, 500mL of 31% hydrochloric acid is added every 4 hours, after soaking for about 12 hours, the bubbles disappear, and taking out the treated reverse osmosis membrane;
3) and (3) respectively soaking the acid-washed reverse osmosis membranes in 2% sodium hypochlorite solution for about 24 hours, and washing with desalted water at low pressure until the residual chlorine in the water is 0.01 mg/L. And immediately filling the wet modified regenerated membrane into a membrane shell of the modified regenerated membrane device for standby.
According to the method for modifying and regenerating the waste reverse osmosis membrane, the modified and regenerated membrane is used for replacing a new membrane, so that the treatment cost is greatly reduced; the upper limits of COD and ammonia nitrogen concentration in the coal-fired sludge coupling wastewater of the thermal power plant which can be treated by the invention are 1450mg/L and 350mg/L respectively (BOD is 25-40% of COD), and the final COD and ammonia nitrogen concentration of the effluent are stably less than 60mg/L and 15mg/L respectively.
What has been described herein is merely a preferred embodiment of the invention, and the scope of the invention is not limited thereto. Modifications, additions, or substitutions by those skilled in the art to the specific embodiments described herein are intended to be within the scope of the invention.
Claims (10)
1. A method for treating coal-fired sludge coupling wastewater of a thermal power plant is characterized by comprising the following steps:
s1, feeding the coal-fired sludge coupling wastewater with high ammonia nitrogen and COD into a regulating tank (10), regulating the water temperature to 12-38 ℃ through natural cooling, and regulating the pH value to 7-9 by using industrial hydrochloric acid;
s2, anaerobic degradation: the wastewater lift pump (13) conveys the high-concentration coal-fired sludge coupling wastewater to the anaerobic tank (20), so that organic matters in the high-concentration coal-fired sludge coupling wastewater are subjected to anaerobic degradation reaction under the action of denitrifying bacteria, and a stirrer (21) in the anaerobic tank (20) runs uninterruptedly;
s3, aerobic degradation: the coal-fired sludge coupling wastewater after the anaerobic reaction treatment flows to an aerobic tank (30) from the bottom of an anaerobic tank (20), organic matters in the wastewater undergo aerobic degradation reaction under the action of nitrobacteria, and the aerobic tank is aerated by an aeration Roots blower (32);
s4, removing suspended matters: the coal-fired sludge coupling wastewater after the aerobic reaction treatment overflows to a secondary sedimentation tank (40) from an aerobic tank (30), flows through a honeycomb inclined pipe (41) in the secondary sedimentation tank (40) from bottom to top through a guide plate (41), an activated sludge in the secondary sedimentation tank (40) is pumped back to an anaerobic tank by a sludge pump (44), and the sludge is discharged through a sludge discharge pipeline (45) according to the determined sludge age;
s5, the coal-fired sludge coupling wastewater treated by the secondary sedimentation tank (40) automatically flows into an intermediate water tank (42);
s6, conveying the coal sludge coupling wastewater in the intermediate water tank (42) to a modified regenerated membrane device (60) for further treatment at a pressure of 0.3MPa through an intermediate water pump (51);
s7, when the differential pressure on the differential pressure gauge (63) is larger than or equal to 100kPa, starting a cleaning program, and discharging cleaning water to the anaerobic tank (20) through a self-cleaning filter blow-down valve (64);
s8, starting a backwashing pump (851) to backwash the regenerated membrane for 1min when the modified regenerated membrane device (60) is set to operate for 2h every time, controlling the flow rate to be 50t/h, and discharging backwash water outlet water to an adjusting tank (10) through a backwashing drainage valve (821);
and S9, chemically cleaning the modified regenerated membrane device.
S10, introducing the effluent of the modified regeneration membrane device (60) into a clean water tank (70): a COD instrument and an ammonia nitrogen instrument are arranged in the clean water tank (70), when the COD is more than 60mg/L or the ammonia nitrogen is more than 15mg/L, sodium hypochlorite solution is added into the clean water tank (70) for further degradation, and the clean water reaching the standard is discharged through the clean water (76) and recycled.
2. The method for treating the coal-fired sludge coupling wastewater of the thermal power plant as claimed in claim 1, wherein the dissolved oxygen in the wastewater in the aerobic tank (30) in the S3 is 2.5-4.0 mg/L.
3. The method for treating the coal-fired sludge coupling wastewater of the thermal power plant as claimed in claim 1, wherein the modified regeneration membrane device (60) comprises a membrane shell and a modified regeneration membrane, the modified regeneration membrane is arranged in the membrane shell, and the preparation method of the modified regeneration membrane comprises the following steps:
1. screening an 8040 reverse osmosis membrane which is judged to be invalid due to low desalination rate;
2. soaking in hydrochloric acid solution with the pH value of 2, taking out after carbon dioxide bubbles are not generated in the hydrochloric acid solution any more, and removing a scale layer in the reverse osmosis membrane;
3. and (3) respectively soaking the acid-washed reverse osmosis membrane in 2% sodium hypochlorite solution for about 24 hours, washing the reverse osmosis membrane with desalted water at low pressure until the residual chlorine in the water is less than or equal to 0.05mg/L, and oxidizing the reverse osmosis membrane to expand and shape the membrane pores.
4. The method for treating the coal-fired sludge coupling wastewater of the thermal power plant as claimed in claim 1, wherein in step 9, when the differential pressure between the sections of the modified regeneration membrane device rises to 0.10MPa, a chemical cleaning solution is configured in the chemical cleaning water tank (81), the modified regeneration membrane device (60) is chemically cleaned by a chemical cleaning pump (831), and the cleaning step is as follows:
1. preparing 2% FC820 solution, closing an inlet adjusting valve, an outlet valve and a concentrated water reflux valve of the modified regeneration membrane device (60), opening an inlet valve and an outlet valve of a chemical cleaning pump, starting the chemical cleaning pump to circularly clean the modified regeneration membrane device for 1h, soaking for 1h, and repeating twice;
2. injecting industrial water into the chemical cleaning box (81), discharging and flushing the modified regenerated membrane device (60), and discharging the effluent to a clean water tank (70) until the pH of the effluent is close to neutral.
5. The method for treating the coal-fired sludge coupling wastewater of the thermal power plant according to claim 1, wherein in the step 1, the temperature of the coal-fired sludge coupling wastewater in the regulating tank (10) is 16-34 ℃; when the pH value of the coal sludge coupling wastewater in the adjusting tank (10) is more than 9, 31% of industrial hydrochloric acid is added, and the pH value is controlled to be 7-8.5.
6. The method for treating the coal-fired sludge coupling wastewater of the thermal power plant as claimed in claim 1, wherein the pH value in step S1 is 8.1, and the temperature of the coal-fired sludge coupling wastewater in the regulating tank (10) is 26-29 ℃.
7. The treatment equipment for the coal-fired sludge coupling wastewater of the thermal power plant based on the treatment method for the coal-fired sludge coupling wastewater of the thermal power plant according to any one of claims 1 to 6 is characterized by comprising the following steps:
the device comprises an adjusting tank (10), wherein one side of the adjusting tank (10) is provided with a sludge coupling wastewater inlet pipe (11) and an acid inlet pipe (12), and the other side of the adjusting tank (10) is provided with a wastewater conveying pipeline (13);
one end of the waste water conveying pipeline (13) is communicated with the anaerobic tank (20);
the bottom of the aerobic tank (30) is communicated with the anaerobic tank (20), the bottom of the aerobic tank (20) is provided with an aeration pipeline (31), and the aeration pipeline (31) is connected with a Roots blower (32);
the device comprises a secondary sedimentation tank (40), wherein the upper part of the secondary sedimentation tank (40) is communicated with an aerobic tank (30), a guide plate (41) and a honeycomb inclined tube (42) are arranged in the secondary sedimentation tank, the guide plate (41) is arranged on one side of the honeycomb inclined tube (42), a sludge return pipeline (43) is arranged at the bottom of the secondary sedimentation tank (40), one end of the sludge return pipeline (43) is communicated with an anaerobic tank (20), and a sludge return pump (44) and a sludge discharge pipeline (45) are arranged on the sludge return pipeline (43);
the intermediate water tank (50), the intermediate water tank (50) is communicated with the secondary sedimentation tank (40);
the modified regeneration membrane device (60) comprises a plurality of membrane tubes connected in parallel, the modified regeneration membrane device (60) is communicated with a water outlet pool (50) through a water outlet pipeline of an intermediate pool, the upper part of the modified regeneration membrane device (60) is communicated with the anaerobic pool (20), a self-cleaning filter (61) is arranged at the inlet of the modified regeneration membrane device (60), a self-cleaning filter sewage discharge pipeline (62) is arranged on the self-cleaning filter (61), and the self-cleaning filter sewage discharge pipeline (62) is communicated to the anaerobic pool (20);
the clean water tank (70), the clean water tank (70) is communicated with the modified regenerated membrane device (60), an online liquid level meter (71), an online nitrogen tester (72) and an online COD tester (73) are arranged on the clean water tank (70), and a hypochlorous acid conveying pipeline (74) and a clean water tank output pipeline (75) are also arranged on the clean water tank (70);
modified regeneration membrane device cleaning system (80), including chemical cleaning case (81) and backwash drain line (82), be equipped with backwash drain valve (821) on backwash drain line (82), modified regeneration membrane device cleaning system (80) are through backwash drain line (82) and equalizing basin (10) intercommunication, chemical cleaning case outlet pipe says (83) and modified regeneration membrane device entry intercommunication, chemical cleaning case outlet pipe says two (84) and modified regeneration membrane device export intercommunication, chemical cleaning case inlet pipe says (85) and clear water pond output pipeline (75) intercommunication.
8. The equipment for treating coal-fired sludge coupling wastewater of a thermal power plant according to claim 7, wherein the regulating tank (10) is a sunken concrete closed water tank, an online submerged pH meter (14) is arranged in the regulating tank, and a wastewater lift pump (131) is arranged on the wastewater conveying pipeline (13).
9. The thermal power plant coal-fired sludge coupled wastewater treatment equipment as claimed in claim 7, wherein the anaerobic tank (20) is a concrete water tank, and a mechanical submerged stirrer (21) is arranged in the anaerobic tank (20).
10. The equipment for treating coal-fired sludge coupling wastewater of thermal power plant as claimed in claim 7, wherein the aerobic tank (30) is a concrete open pond, and the branch pipe of the aeration pipeline (31) has an opening density of 2.5cm2And/m, elastic filler is arranged in the aerobic tank (30), the precision of a filter screen of the self-cleaning filter (61) is 100 mu m, a pressure difference meter (63) is arranged at an inlet and an outlet of the self-cleaning filter, and a blowdown valve (64) of the self-cleaning filter is arranged at the filtered water side.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1533992A (en) * | 2003-04-02 | 2004-10-06 | 董红敏 | High concentration oxganic effluent treatment composite process and its equipment |
| US20050109694A1 (en) * | 2003-11-21 | 2005-05-26 | Industrial Technology Research Institute | Method and system for treating wastewater containing organic compounds |
| CN101125721A (en) * | 2006-08-18 | 2008-02-20 | 东丽纤维研究所（中国）有限公司 | Technique for reusing sewage |
| CN101549907A (en) * | 2008-04-02 | 2009-10-07 | 天津膜天膜工程技术有限公司 | Membrane biologic reaction equipment and processing method for processing industrial waste water with high ammoniac nitrogen |
| CN106946417A (en) * | 2017-05-10 | 2017-07-14 | 神华集团有限责任公司 | Sewage-treatment plant |
| CN106957089A (en) * | 2017-04-17 | 2017-07-18 | 同济大学 | A kind of twice-modified method of discarded reverse osmosis membrane available for treatment of dyeing wastewater |
| CN110127818A (en) * | 2018-12-21 | 2019-08-16 | 广东博尔睿水处理技术有限公司 | A kind of twice-modified method of the discarded reverse osmosis membrane for Industrial Wastewater Treatment |
| CN213416591U (en) * | 2020-06-29 | 2021-06-11 | 浙江浙能嘉华发电有限公司 | Treatment facility of coal-fired mud coupling waste water of thermal power plant |
-
2020
- 2020-06-29 CN CN202010605903.8A patent/CN112093973A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1533992A (en) * | 2003-04-02 | 2004-10-06 | 董红敏 | High concentration oxganic effluent treatment composite process and its equipment |
| US20050109694A1 (en) * | 2003-11-21 | 2005-05-26 | Industrial Technology Research Institute | Method and system for treating wastewater containing organic compounds |
| CN101125721A (en) * | 2006-08-18 | 2008-02-20 | 东丽纤维研究所（中国）有限公司 | Technique for reusing sewage |
| CN101549907A (en) * | 2008-04-02 | 2009-10-07 | 天津膜天膜工程技术有限公司 | Membrane biologic reaction equipment and processing method for processing industrial waste water with high ammoniac nitrogen |
| CN106957089A (en) * | 2017-04-17 | 2017-07-18 | 同济大学 | A kind of twice-modified method of discarded reverse osmosis membrane available for treatment of dyeing wastewater |
| CN106946417A (en) * | 2017-05-10 | 2017-07-14 | 神华集团有限责任公司 | Sewage-treatment plant |
| CN110127818A (en) * | 2018-12-21 | 2019-08-16 | 广东博尔睿水处理技术有限公司 | A kind of twice-modified method of the discarded reverse osmosis membrane for Industrial Wastewater Treatment |
| CN213416591U (en) * | 2020-06-29 | 2021-06-11 | 浙江浙能嘉华发电有限公司 | Treatment facility of coal-fired mud coupling waste water of thermal power plant |
Non-Patent Citations (1)
| Title |
|---|
| 肖羽棠主编: "《城市污水处理技术》", 31 July 2015, 中国建材工业出版社 * |
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Application publication date: 20201218 |