CN111115978A - Leachate treatment system and method for waste incineration power plant - Google Patents
Leachate treatment system and method for waste incineration power plant Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 34
- 238000004056 waste incineration Methods 0.000 title claims abstract description 27
- 239000012528 membrane Substances 0.000 claims abstract description 67
- 239000010802 sludge Substances 0.000 claims abstract description 53
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 18
- 230000008569 process Effects 0.000 claims abstract description 18
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000004519 manufacturing process Methods 0.000 claims abstract description 13
- 238000011084 recovery Methods 0.000 claims abstract description 11
- 239000000243 solution Substances 0.000 claims description 46
- 238000000108 ultra-filtration Methods 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 21
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 18
- 238000005086 pumping Methods 0.000 claims description 18
- 239000012141 concentrate Substances 0.000 claims description 15
- 239000010813 municipal solid waste Substances 0.000 claims description 15
- 238000002347 injection Methods 0.000 claims description 14
- 239000007924 injection Substances 0.000 claims description 14
- 230000004907 flux Effects 0.000 claims description 12
- 238000000889 atomisation Methods 0.000 claims description 8
- 238000001223 reverse osmosis Methods 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 6
- 238000009292 forward osmosis Methods 0.000 claims description 6
- 150000003839 salts Chemical class 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 239000002957 persistent organic pollutant Substances 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 239000002033 PVDF binder Substances 0.000 claims description 3
- 239000000498 cooling water Substances 0.000 claims description 3
- 238000001125 extrusion Methods 0.000 claims description 3
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 3
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 3
- 229920002981 polyvinylidene fluoride Polymers 0.000 claims description 3
- 238000012958 reprocessing Methods 0.000 claims description 3
- 230000008901 benefit Effects 0.000 abstract description 6
- 239000000463 material Substances 0.000 abstract description 5
- 239000003344 environmental pollutant Substances 0.000 abstract description 4
- 231100000719 pollutant Toxicity 0.000 abstract description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 3
- 239000003546 flue gas Substances 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 238000004064 recycling Methods 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 2
- 208000028659 discharge Diseases 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000003204 osmotic effect Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 239000000149 chemical water pollutant Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000008595 infiltration Effects 0.000 description 1
- 238000001764 infiltration Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 238000009270 solid waste treatment Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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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
-
- 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
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F1/445—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by forward osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
-
- 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
-
- 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
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
-
- 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
- C02F3/28—Anaerobic digestion processes
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a leachate treatment system and a leachate treatment method for a waste incineration power plant, which comprise an adjusting tank, an anaerobic device, an anaerobic water production tank, an AMBR membrane device, a membrane advanced treatment device and a water production tank which are sequentially connected through a pipeline, wherein the system also comprises a sludge tank and a concentrated solution collecting tank, the anaerobic device and the AMBR membrane device are respectively connected with the sludge tank through pipelines, and the membrane advanced treatment device is connected with the concentrated solution collecting tank through a pipeline. The method has the advantages of low concentrated solution yield and short process flow, and the ammonia nitrogen in the percolate is concentrated and enriched and then is recycled as a denitration reducing agent, so that the pollutant treatment cost is reduced, the resource recovery is realized, and the material consumption in the flue gas denitration stage is saved.
Description
Technical Field
The invention belongs to the field of wastewater treatment, and particularly relates to a leachate treatment system and method for a waste incineration power plant.
Background
The landfill leachate is generated in the solid waste treatment projectThe high-concentration organic wastewater, wherein the leachate of the domestic garbage incineration plant is the wastewater collected by seeping from the garbage storage pit in the domestic garbage incineration plant, and has the characteristics of high pollutant concentration, high water quality, large water quantity fluctuation, high hardness, high alkalinity and the like. Common COD in waste incineration plantsCrThe concentrations of ammonia nitrogen, TN and SS are 40000-70000mg/L, 1200-2500mg/L, 1300-3000mg/L and 3000-10000mg/L respectively, and the pH value is generally acidic.
At present, the leachate treatment of a domestic garbage incineration plant basically needs to reach the zero discharge standard, the standard reaching water is used as the make-up water of an open cooling circulating water system, the main process is 'anaerobic + two-stage nitrification and denitrification + ultrafiltration + membrane advanced treatment', firstly, denitrification and degradation are carried out through the anaerobic and two-stage nitrification and denitrification processes, biochemical COD is degraded, then, mud and water separation is realized through the ultrafiltration process, the intercepted sludge flows back to the nitrification and denitrification system, the sludge concentration in the system is maintained, and the obtained clear liquid enters a rear-end membrane advanced treatment device for treatment, the COD and metal ions are intercepted, and the final clear liquid is obtained and discharged after reaching the standard. The process is mature, the operation is stable, the effluent quality can stably reach the standard, but the process can generate 25 to 40 percent of concentrated solution, and the concentrated solution generated by advanced treatment is synergistically consumed in modes of lime pulping, fly ash sequestration, furnace entry and back spray and the like; however, the large yield of the concentrated solution is difficult to synergistically dissolve, and as for the concentrated solution evaporation process, the investment of an evaporation system is large, the operation cost is high, and the method is economically infeasible. In addition, because the aerobic system needs to supply a large amount of oxygen for microorganisms to remove organic pollutants and ammonia nitrogen, the aerobic system has high energy consumption and high operation cost.
Therefore, the prior art is subject to further improvement and development.
Disclosure of Invention
In order to solve the above problems, a system and a method for treating leachate from a waste incineration power plant are proposed.
The invention provides the following technical scheme:
the utility model provides a refuse incineration power plant leachate treatment system, wherein, includes equalizing basin, anaerobism device, the anaerobism water production jar that connects gradually through the pipeline, AMBR membrane device, membrane advanced treatment unit and produce the pond, the system still includes sludge impoundment and concentrate collecting pit, anaerobism device and AMBR membrane device are respectively through pipe connection sludge impoundment, membrane advanced treatment unit passes through pipe connection concentrate collecting pit.
The utility model provides a waste incineration power plant leachate treatment system, wherein, the system still includes marsh gas collection device, anaerobism device passes through pipe connection marsh gas collection device, marsh gas collection device passes through fan and power plant incinerator marsh gas combustor intercommunication.
The utility model provides a refuse incineration power plant leachate treatment system, wherein, the system still includes sludge dewatering device and clear solution pond, sludge impoundment, sludge dewatering device and clear solution pond connect gradually through the pipeline, and sludge dewatering device is through the pipe connection power plant refuse incineration workshop that is provided with the sludge pump, clear solution pond and anaerobic apparatus pass through the pipeline intercommunication.
The utility model provides a waste incineration power plant filtration liquid processing system, wherein, AMBR membrane device is external tubular ultrafiltration device or submergence formula ultrafiltration device, external tubular ultrafiltration device adopts the PVDF membrane as external tubular ultrafiltration membrane, and external tubular ultrafiltration device's design flux is not higher than 50LMH, submergence formula ultrafiltration device adopts the PTFE membrane as submergence formula ultrafiltration membrane, and submergence formula ultrafiltration device's design flux is not higher than 10 LMH.
The utility model provides a waste incineration power plant filtration liquid processing system, wherein, membrane advanced treatment unit passes through pipe connection power plant cooling circulation pond, and membrane advanced treatment unit is reverse osmosis unit or positive osmotic device, reverse osmosis unit is the two-stage DTRO device, positive infiltration is the MBC device.
A leachate treatment system of a waste incineration power plant is disclosed, wherein a DTRO membrane selected in a two-stage DTRO device has a rejection rate of monovalent salt of not less than 95% at 25 ℃, wherein the design flux of a primary DTRO is 8-15LMH, and the design recovery rate is 75-80%; the design flux of the secondary DTRO is 25-35LMH, and the recovery rate is not lower than 90%;
the removal rate of ammonia nitrogen of a forward osmosis membrane selected in the MBC device is not lower than 95% at 25 ℃, and the TDS of a concentrated solution is not lower than 100000 mg/L.
The utility model provides a waste incineration power plant filtration liquid processing system, wherein, the concentrate collecting pit passes through pipe connection denitration reductant atomizing injection apparatus, denitration reductant atomizing injection apparatus corresponds the power plant and burns burning furnace setting, and the injection position sets up in overgrate air supply mouth top, and wherein, the concentrate ammonia nitrogen concentration that the concentrate collecting pit was collected reaches 8000mg/L-25000 mg/L.
The utility model provides a waste incineration power plant filtration liquid processing system, wherein, sludge dewatering device is one of screw extrusion hydroextractor, centrifugal dehydrator, pile spiral shell machine.
A method for treating percolate of a waste incineration power plant comprises the following steps:
step S1: pumping the percolate in the regulating tank into an anaerobic device, removing suspended matters and organic matters in water in the anaerobic device, overflowing the percolate into an anaerobic water production tank, and simultaneously delivering generated biogas into a biogas collecting device to be delivered to a power plant incinerator for use;
step S2: and (4) carrying out mud-water separation on the anaerobic effluent in the step S1 by using an AMBR membrane device, enabling the obtained produced water to enter a membrane advanced treatment device, discharging the separated sludge and the sludge discharged by the anaerobic device into a sludge tank, pumping the separated sludge and the sludge into a sludge dewatering device for dewatering, enabling clear liquid generated by dewatering to enter a clear liquid tank, pumping the clear liquid into the anaerobic device for reprocessing, and pumping sludge cakes generated by dewatering to a power plant garbage incineration workshop for incineration disposal.
Step S3: and (4) concentrating and separating the produced water obtained in the step S2 by using a membrane deep treatment device, discharging the obtained water reaching the standard to a water production pool, pumping the water to a circulating cooling water pool as make-up water, feeding the obtained concentrated solution into a concentrated solution collecting pool, pumping the concentrated solution to a denitration reducing agent atomization and injection device for use as a denitration reducing agent, and removing organic pollutants in the concentrated solution through high-temperature incineration.
A method for treating percolate from a waste incineration power plant is characterized in that in step S1, in the working process of a system, the temperature in an anaerobic device is controlled to be 35 +/-2 ℃, and the pH value is controlled to be 7.2-8; in the step S2, in the working process of the system, the working temperature of the AMBR membrane system adopting an external membrane is controlled to be 20-40 ℃, and the pressure is controlled to be below 6 bar; in step S3, in the working process of the system, the temperature of inlet water is controlled to be 20-35 ℃, the pH value is controlled to be 6-6.5, the recovery rate is controlled to be 75-90%, and the temperature of the position of concentrated solution sprayed back into the furnace is controlled to be 900-1000 ℃.
Advantageous effects
The invention relates to a system and a method for treating percolate of a garbage incineration power plant, which aim at full-volume and zero-discharge treatment of percolate of a household garbage incineration power plant, solve the problems of high yield and high consumption pressure of concentrated solution in the prior art, and have the following advantages:
1. an aerobic system is cancelled, the process flow is shortened, and the operation management difficulty is reduced;
2. the aerobic system is cancelled, so that related equipment is reduced, equipment investment, operation energy consumption, operation material consumption, process floor area and the like are greatly reduced, and investment and operation cost are saved;
3. the ammonia nitrogen in the leachate is concentrated and enriched and then recycled as a denitration reducing agent, so that the pollutant treatment cost is reduced, the resource recovery is realized, and the material consumption in the flue gas denitration stage is saved.
Drawings
FIG. 1 is a process flow diagram of a leachate treatment system of a waste incineration power plant according to an embodiment of the present invention;
FIG. 2 is a flow chart of a leachate treatment method in a waste incineration power plant according to an embodiment of the present invention.
Detailed Description
In order to make the technical solutions of the present invention better understood, the following description of the technical solutions of the present invention with reference to the accompanying drawings of the present invention is made clearly and completely, and other similar embodiments obtained by a person of ordinary skill in the art without any creative effort based on the embodiments in the present application shall fall within the protection scope of the present application. In addition, directional terms such as "upper", "lower", "left", "right", etc. in the following embodiments are directions with reference to the drawings only, and thus, the directional terms are used for illustrating the present invention and not for limiting the present invention.
A leachate treatment system of a waste incineration power plant is shown in figure 1 and comprises a regulating tank, an anaerobic device, an anaerobic water production tank, an AMBR membrane device, a membrane advanced treatment device and a water production tank which are sequentially connected through pipelines.
Specifically, the system still includes sludge impoundment and concentrate collecting pit, anaerobism device and AMBR membrane device pass through pipe connection sludge impoundment respectively, membrane advanced treatment unit passes through pipe connection concentrate collecting pit.
Specifically, the concentrated solution collecting tank is connected with the denitration reducing agent atomization and injection device through a pipeline, the denitration reducing agent atomization and injection device is arranged corresponding to the power plant incinerator, the injection position is arranged above the secondary air supply opening, the concentrated solution is sprayed back into the furnace through the denitration reducing agent atomization and back-injection device, injection equipment is saved, and project investment is saved. The ammonia nitrogen concentration of the concentrated solution collected by the concentrated solution collecting tank reaches 8000-25000 mg/L, and the concentrated solution can be used as a denitration reducing agent of SNCR in a flue gas treatment system. The concentrated solution is used as an SNCR denitration reducing agent, so that the recycling benefit of domestic waste treatment is improved while the final treatment of the concentrated solution is realized, the economic benefit brought by the concentrated solution treatment is greater than the cost caused by the final treatment of the concentrated solution, and certain economic benefit is realized.
Specifically, the system further comprises a biogas collecting device, the anaerobic device is connected with the biogas collecting device through a pipeline, and the biogas collecting device is communicated with the power plant incinerator biogas burner through a fan.
Specifically, the system still includes sludge dewatering device and clear solution pond, sludge dewatering device and clear solution pond connect gradually through the pipeline, and sludge dewatering device is through the pipe connection power plant msw incineration workshop that is provided with the sludge pump, the operation health of being convenient for. Clear liquid after sludge dewatering is lifted to an anaerobic device through a pump, one-time lifting is reduced, operation energy consumption is reduced, and the dewatered sludge is conveyed to a garbage hopper through the pump to be incinerated, so that the operation condition is sanitary, and the efficiency is high.
Specifically, the clear liquid pond passes through the pipeline intercommunication with anaerobic installation, and membrane advanced treatment unit passes through the pipe connection power plant cooling cycle pond, and membrane advanced treatment unit is reverse osmosis unit or just osmotic device, reverse osmosis unit is the two-stage DTRO device, just permeates to be the MBC device. And the two-stage DTRO device or the MBC device is provided with a membrane cleaning device, a newly-added methane collecting device and a dewatering clear liquid pool.
Compared with the traditional anaerobic device which has the advantages that the sludge is leaked due to the fact that water flows out of the traditional anaerobic device and then flows into a follow-up unit through overflow, the anaerobic water is separated through the MBR, the problem of sludge leakage in the anaerobic state can be thoroughly solved, the treatment efficiency of the anaerobic device is improved, and meanwhile the quality of the anaerobic water is better. Compared with the MBR membrane biological unit in the prior art, the invention belongs to the problems of an aerobic system, equipment increase, operation material consumption and the like, and the invention cancels the aerobic system through process innovation, reduces related equipment, greatly reduces equipment investment, operation energy consumption, operation material consumption, process occupied area and the like, and saves investment and operation cost.
Specifically, the AMBR membrane device is an external tubular ultrafiltration device or an immersed ultrafiltration device, the external tubular ultrafiltration device adopts a PVDF membrane as an external tubular ultrafiltration membrane, the design flux of the external tubular ultrafiltration device is not higher than 50LMH, the immersed ultrafiltration device adopts a PTFE membrane as an immersed ultrafiltration membrane, and the design flux of the immersed ultrafiltration device is not higher than 10 LMH; the AMBR membrane device can meet the safe and stable operation of MBR membrane under the condition that the concentration of organic matters is up to 10000mg/L, the AMBR can meet the separation requirements of anaerobic system sludge on high viscosity and difficult separation, the removal rate of the AMBR membrane device to SS can reach more than 95%, and the removal rate of the organic matters reaches more than 20%.
Preferably, the rejection rate of the selected DTRO membrane in the two-stage DTRO device to monovalent salt is not lower than 95% at 25 ℃, wherein the design flux of the first-stage DTRO is 8-15LMH, and the design recovery rate is 75% -80%; the design flux of the secondary DTRO is 25-35LMH, and the recovery rate is not lower than 90%; the two-stage DTRO process not only adopts the separation function of the RO device, but also focuses more on the concentration and enrichment function of the RO membrane on ammonia nitrogen in the percolate, and increases the ammonia nitrogen concentration in the concentrated solution. Except that adopting RO to carry out the concentrate still can adopt the MBC concentrate, the concentrate efficiency of MBC is higher, reduces the output of concentrate, promotes the ammonia nitrogen concentration in the concentrate and concentrate added value. Compared with the concentrated solution treated by an aerobic system in the prior art, the main pollutants are organic matters and salt, the concentrated solution is not subjected to nitrification and denitrification, and the ammonia nitrogen in the percolate is equivalent to ammonia water with the concentration of 1-3% after being concentrated and enriched by a membrane except the organic matters and salt, so that the concentrated solution can be used as an SNCR (selective non-catalytic reduction) denitration reducing agent, waste is changed into valuable, and waste recycling is realized.
Preferably, the forward osmosis membrane selected in the MBC device has the ammonia nitrogen removal rate of not less than 95% and the TDS of the concentrated solution of not less than 100000mg/L at 25 ℃.
Preferably, the sludge dewatering device is one of a screw extrusion dewaterer, a centrifugal dewaterer and a screw stacking machine.
Preferably, the anaerobic device is an efficient anaerobic device such as UASB or IC, and the removal rate of COD organic matters by the anaerobic device is not lower than 85%. The anaerobic water production tank is used as a water inlet tank of the buffering and AMBR membrane device, and the buffering capacity between systems is enhanced.
The method for treating leachate of a waste incineration power plant according to the present invention is specifically described below, and as shown in fig. 2, comprises the following steps:
step S1: pumping the percolate in the regulating tank into an anaerobic device, removing organic matters and suspended matters in the anaerobic device, overflowing the percolate into an anaerobic water production tank, and simultaneously delivering the generated marsh gas into a marsh gas collecting device to be delivered to a power plant incinerator for use;
specifically, the anaerobic device removes organic matters to reduce the COD value of the leachate.
Step S2: and (4) carrying out sludge-water separation on the anaerobic effluent in the step S1 by using an AMBR membrane device, feeding the obtained produced water into a reverse osmosis/forward osmosis device, discharging the separated sludge and the sludge discharged by the anaerobic device into a sludge tank, pumping the separated sludge and the sludge into a sludge dewatering device for dewatering, feeding clear liquid generated by dewatering into a clear liquid tank, pumping the clear liquid into the anaerobic device for reprocessing, and pumping sludge cakes generated by dewatering into a power plant garbage incineration workshop for incineration disposal.
Step S3: concentrating and separating the produced water obtained in the step S2 by using a membrane advanced treatment device, discharging the obtained produced water reaching the standard to a water production pool, pumping the produced water to a circulating cooling water pool as make-up water, simultaneously feeding the obtained concentrated solution to a concentrated solution collecting pool, pumping the concentrated solution to a denitration reducing agent atomization injection device for use as a denitration reducing agent, and simultaneously removing organic pollutants in the concentrated solution through high-temperature incineration;
preferably, in step S1, the temperature in the anaerobic apparatus is controlled to 35 ± 2 ℃ and the pH is controlled to be 7.2-8 during the operation of the system.
Preferably, in step S2, in the system operation process, the operating temperature of the AMBR membrane system is controlled to 20 ℃ to 40 ℃ when an external membrane is adopted, and the pressure is controlled to be below 6 bar.
Preferably, in step S3, in the working process of the system, the inlet water temperature is controlled to be 20-35 ℃, the pH value is controlled to be 6-6.5, the recovery rate is controlled to be 75-90%, and the temperature of the concentrated solution sprayed back into the furnace is controlled to be 900-1000 ℃.
The technical effects of the present invention will be further explained with reference to the following embodiments:
the leachate treatment system and the treatment method for the garbage incineration power plant are adopted to treat the leachate of a certain household garbage incineration plant, and the quality COD of the leachate of the household garbage incineration plant is CODCrThe concentrations of ammonia nitrogen, TN and SS are 40000-70000mg/L, 1500-2000mg/L, 1700-2500mg/L and 3000-10000mg/L respectively, and the water quality of the outlet water is designed as follows: COD is 60mg/L, ammonia nitrogen is 10mg/L, SS is 30mg/L, and chloride ion concentration is 250 mg/L.
After the leachate of the domestic garbage incineration plant is treated by the leachate treatment method of the garbage incineration power plant, the water production COD of the secondary DTRO/MBC device 5CrThe ammonia nitrogen and the chloride ions respectively reach 10-40mg/L, 0.1-5mg/L and 50-200mg/L, and meet the recycling standard.
The present invention has been described in detail, and it should be understood that the detailed description and specific examples, while indicating the preferred embodiment of the invention, are intended for purposes of illustration only and are not intended to limit the scope of the invention.
Claims (10)
1. The utility model provides a refuse incineration power plant leachate treatment system, its characterized in that includes equalizing basin, anaerobism device, the anaerobism water tank of producing that connects gradually through the pipeline, AMBR membrane device, membrane advanced treatment unit and produce the pond, the system still includes sludge impoundment and concentrate collecting pit, anaerobism device and AMBR membrane device are respectively through pipe connection sludge impoundment, membrane advanced treatment unit passes through pipe connection concentrate collecting pit.
2. The leachate treatment system of a waste incineration power plant of claim 1, further comprising a biogas collection device, wherein the anaerobic device is connected to the biogas collection device through a pipeline, and the biogas collection device is communicated with the power plant incinerator biogas burner through a fan.
3. The leachate treatment system of a waste incineration power plant according to claim 1, further comprising a sludge dewatering device and a clear liquid tank, wherein the sludge tank, the sludge dewatering device and the clear liquid tank are sequentially connected through a pipeline, the sludge dewatering device is connected with a waste incineration plant of the power plant through a pipeline provided with a sludge pump, and the clear liquid tank is communicated with the anaerobic device through a pipeline.
4. The leachate treatment system of the waste incineration power plant of claim 1, wherein the AMBR membrane device is an external tubular ultrafiltration device or an immersed ultrafiltration device, the external tubular ultrafiltration device employs a PVDF membrane as the external tubular ultrafiltration membrane, the design flux of the external tubular ultrafiltration device is not higher than 50LMH, the immersed ultrafiltration device employs a PTFE membrane as the immersed ultrafiltration membrane, and the design flux of the immersed ultrafiltration device is not higher than 10 LMH.
5. The leachate treatment system of a refuse incineration power plant according to claim 1, wherein the membrane advanced treatment unit is connected to the cooling circulation water tank of the power plant through a pipeline, the membrane advanced treatment unit is a reverse osmosis unit or a forward osmosis unit, the reverse osmosis unit is a two-stage DTRO unit, and the forward osmosis unit is an MBC unit.
6. The leachate treatment system of the waste incineration power plant of claim 5, wherein the DTRO membrane selected in the two-stage DTRO device has a rejection rate of monovalent salt of not less than 95% at 25 ℃, wherein the design flux of the primary DTRO is 8-15LMH, and the design recovery rate is 75-80%; the design flux of the secondary DTRO is 25-35LMH, and the recovery rate is not lower than 90%;
the removal rate of ammonia nitrogen of a forward osmosis membrane selected in the MBC device is not lower than 95% at 25 ℃, and the TDS of a concentrated solution is not lower than 100000 mg/L.
7. The leachate treatment system of a waste incineration power plant according to claim 1, wherein the concentrated solution collecting tank is connected with a denitration reducing agent atomization injection device through a pipeline, the denitration reducing agent atomization injection device is arranged corresponding to the power plant incinerator, and the injection position is arranged above a secondary air supply port, wherein the concentration of ammonia nitrogen in the concentrated solution collected by the concentrated solution collecting tank reaches 8000mg/L-25000 mg/L.
8. The leachate treatment system of a waste incineration power plant of claim 1, wherein the sludge dewatering device is one of a screw extrusion dewaterer, a centrifugal dewaterer, and a screw stacking machine.
9. A leachate treatment method for a waste incineration power plant implemented on the basis of the system according to any one of claims 1 to 8, characterized by comprising the following steps:
step S1: pumping the percolate in the regulating tank into an anaerobic device, removing organic matters and suspended matters in water in the anaerobic device, overflowing the percolate into an anaerobic water production tank, and simultaneously delivering the generated marsh gas into a marsh gas collecting device to be delivered to a power plant incinerator for use;
step S2: and (4) carrying out mud-water separation on the anaerobic effluent in the step S1 by using an AMBR membrane device, enabling the obtained produced water to enter a membrane advanced treatment device, discharging the separated sludge and the sludge discharged by the anaerobic device into a sludge tank, pumping the separated sludge and the sludge into a sludge dewatering device for dewatering, enabling clear liquid generated by dewatering to enter a clear liquid tank, pumping the clear liquid into the anaerobic device for reprocessing, and pumping sludge cakes generated by dewatering to a power plant garbage incineration workshop for incineration disposal.
Step S3: and (4) concentrating and separating the produced water obtained in the step S2 by using a membrane deep treatment device, discharging the obtained water reaching the standard to a water production pool, pumping the water to a circulating cooling water pool as make-up water, feeding the obtained concentrated solution into a concentrated solution collecting pool, pumping the concentrated solution to a denitration reducing agent atomization and injection device for use as a denitration reducing agent, and removing organic pollutants in the concentrated solution through high-temperature incineration.
10. The method for treating leachate in a waste incineration power plant according to claim 9, wherein in step S1, the temperature in the anaerobic apparatus is controlled to 35 ± 2 ℃ and the pH value is controlled to 7.2-8; in step S2, the working temperature of the AMBR membrane system adopting an external membrane is controlled to be 20-40 ℃, and the pressure is controlled to be below 6 bar; in step S3, in the working process of the system, the temperature of inlet water is controlled to be 20-35 ℃, the pH value is controlled to be 6-6.5, the recovery rate is controlled to be 75-90%, and the temperature of the position of concentrated solution sprayed back into the furnace is controlled to be 900-1000 ℃.
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