CN212293239U - Leachate treatment system for waste incineration plant - Google Patents
Leachate treatment system for waste incineration plant Download PDFInfo
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Abstract
The utility model relates to a sewage treatment technical field, concretely relates to refuse incineration plant leachate treatment system. The leachate treatment system of the waste incineration plant comprises an adjusting tank, a hydrolysis acidification tank, a UASB anaerobic reaction tank, an air floatation tank, a sedimentation tank, an analytic deamination tower, an A/O reaction tank, an MBR membrane tank, a coagulation tank, an ozone catalytic oxidation tank, a middle tank, a denitrification filter tank and an activated carbon filter tank which are sequentially connected along the water flow direction. The utility model discloses a leachate treatment system of waste incineration plant enables the leachate that the waste incineration plant produced to reach the emission limit value standard of "domestic waste landfill control standard" (GB 16889) through handling back quality of water, has that the treatment effect is good, the cost is lower, the operation is stable, do not produce the advantage of concentrated phase liquid behind the membrane, therefore has better application and promotion prospect, can be for the steady operation and the benefit reduction of waste incineration plant's driving and protecting navigation.
Description
Technical Field
The utility model relates to a sewage treatment technical field, concretely relates to refuse incineration plant leachate treatment system.
Background
In order to increase the calorific value of the garbage, the garbage incineration plant needs to ferment and mature the garbage and drain the water in the garbage, so that organic wastewater with extremely complex components, namely garbage leachate, can be formed. Besides high-concentration organic matters, the landfill leachate also contains ammonia nitrogen, various dissolved cations, heavy metals, salts and other harmful pollutants, and is polluted wastewater which is difficult to treat. Due to complex components, the landfill leachate cannot be effectively treated by using a single process or a traditional biochemical process. On the other hand, the treated effluent of the leachate needs to meet the discharge limit standard in table 2 of the control standard of domestic refuse landfill (GB 16889-2008). In areas with high development density and small environmental capacity, the effluent of leachate has to reach the strict discharge limit standard in GB16889-2008 table 3, which puts higher requirements on the treatment process of leachate. The existing percolate treatment process mainly has the problems of poor impact resistance, high operation cost, difficult treatment of concentrated phase liquid after the membrane and the like. Therefore, based on the garbage leachate discharge and pollutant characteristics, aiming at the problems, the combined treatment process which is economical and reasonable, has feasible technology and stable and reliable operation is developed, is the key for solving the pain point of the garbage incineration industry, and can be used for stable production, cost reduction, efficiency improvement and driving protection of an incineration plant.
Patent application with publication number CN110028210A discloses a process for treating landfill leachate based on UASB technology. The leachate enters a UASB anaerobic reactor after being pretreated, and a heating system is arranged in the UASB reactor, so that the automatic heating in the anaerobic reaction process can be realized. And enabling the effluent of the UASB to enter a two-stage A/O biochemical reaction tank. And the effluent of the two-stage A/O enters an ultrafiltration system, a nanofiltration system and a reverse osmosis system to enable the effluent to reach the discharge standard or be recycled. The method is a more conventional combined treatment process for the percolate, and mainly has the problem that concentrated phase liquid after the membrane is difficult to treat.
Patent application with publication number CN110577333A discloses a new technology for treating leachate. The landfill leachate enters a denitrification and secondary nitrification process after being pretreated and treated by a UASB reactor, and is subsequently treated by an ultrafiltration, DTRO and RO membrane process, so that produced water is recycled. The utility model discloses an increase low pressure reverse osmosis behind high pressure reverse osmosis, improved reverse osmosis's play water quality of water, still can't carry out proper treatment to the membrane after the concentrate that reverse osmosis unit produced.
Patent application with publication number CN110510825A discloses a zero-concentrate landfill leachate treatment method and system. The method mainly removes suspended matters, heavy metals and partial organic matters in water by adding alkali for coagulating sedimentation, simultaneously increases the pH value of the water to more than 10, and then converts ammonia nitrogen in the water into ammonium sulfate by a membrane deamination technology, reduces the concentration of the ammonia nitrogen in the water, and improves the C/N ratio of the effluent. The biochemical process adopts multistage AO + MBR to reduce the concentration of organic matters, ammonia nitrogen and total nitrogen in water, and the tail end uses countercurrent adsorption and dynamic filtration technology to ensure that the effluent reaches the standard and is discharged, and has the characteristics of no generation of concentrated solution, good treatment effect and lower treatment cost. However, the pretreatment process of the method at the front end of the membrane deamination is incomplete, so that the degassing membrane is easily polluted and blocked, the membrane is frequently cleaned, and the stable operation of the system is influenced. The ammonium sulphate solution produced in the deamination stage is of low concentration (not commercially valuable) and requires the additional use of an evaporator to concentrate and crystallize the solution to obtain ammonium sulphate solids, which undoubtedly increases the overall operating costs. The tail end adopts an adsorption and filtration mode to remove the residual pollutants in the water, on one hand, as the pollutant concentration of the MBR effluent is still high, the adsorbent is easy to adsorb and saturate, the adsorbent needs to be regenerated frequently, and the abraded adsorbent needs to be supplemented and replaced; on the other hand, the filter tank is easy to harden, needs frequent air-water backwashing, and is not easy to replace filter materials. After the costs of adsorbent regeneration, filter material replacement, etc. are distributed, the actual treatment cost will rise.
Patent application with publication number CN110510794A discloses a zero discharge treatment device and method for landfill leachate. The method mainly uses a membrane treatment system to remove most of COD, ammonia nitrogen and total hardness in water, and converts the ammonia nitrogen into ammonium salt for resource utilization. The concentrated solution generated by the membrane treatment is subjected to low-temperature evaporation and solidification treatment to achieve the effect of zero emission. The disadvantages of this method are: firstly, leachate directly enters a nanofiltration unit without pretreatment, organic matters and suspended matters in water are easy to cause membrane fouling and blocking, and membranes are frequently cleaned/replaced, so that the stability of the operation of the whole process is influenced; secondly, a large amount of alkali is added into the membrane deamination unit to adjust the pH value, so that the treatment cost is obviously increased. Thirdly, after the concentrated water enters the evaporation system, high-concentration organic matters in the concentrated water easily form an azeotrope, so that the evaporated condensed water contains a large amount of organic pollutants. The condensed water returns to the nanofiltration unit, and the organic matters in the condensed water aggravate the pollution and blockage of the unit.
SUMMERY OF THE UTILITY MODEL
The not enough to prior art, the utility model provides a leachate treatment system of msw incineration plant, the leachate that enables the msw incineration plant to produce quality of water reaches the emission limit value standard of "domestic waste landfill control standard" (GB 16889) 2008) after handling, has that the treatment effect is good, the cost is lower, the operation is stable, do not produce the advantage of dense phase liquid behind the membrane, therefore has better application promotion prospect, can be for the steady operation and the benefit reduction of msw incineration plant protect driving.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
the utility model provides a refuse incineration factory filtration liquid processing system, includes equalizing basin, hydrolysis-acidification pool, UASB anaerobic reaction jar, air supporting pond, sedimentation tank, analytic deamination tower, AO reaction tank, MBR membrane cisterna, coagulating basin, ozone catalytic oxidation pond, intermediate tank, denitrification filtering pond and active carbon filtering pond that connect gradually along the rivers direction.
Preferably, among the above-mentioned waste incineration plant leachate treatment system, still include sludge dewatering device, the sludge outlet of UASB anaerobic reaction tank, the dross export in air supporting pond, the sludge outlet of sedimentation tank, the sludge outlet in A/O reaction tank, the sludge outlet in MBR membrane cisterna, the sludge outlet in coagulation basin all with sludge dewatering device connects.
Preferably, among the above-mentioned waste incineration plant leachate treatment system, still include the heat exchanger, the play water of sedimentation tank passes through earlier the heat exchanger is connected to analysis deamination tower, the tower bottom play water of analysis deamination tower passes through earlier the heat exchanger is connected to the A/O reaction tank again.
Preferably, in the leachate treatment system of the waste incineration plant, the lower part of the desorption deamination tower is provided with a steam inlet, and the steam inlet of the desorption deamination tower is connected with a waste heat steam supply pipeline of the waste incineration plant.
Preferably, in the leachate treatment system of the waste incineration plant, a dephlegmator is arranged at the top of the resolving deamination tower, and a top gas outlet of the resolving deamination tower is connected to an inlet of the dephlegmator.
Preferably, in the leachate treatment system of a waste incineration plant, a gas outlet of the ozone catalytic oxidation tank is connected to the activated carbon filter.
Preferably, in the leachate treatment system of the waste incineration plant, the MBR membrane tank is an external MBR membrane tank, and a curtain type MBR membrane module is arranged in the external MBR membrane tank.
Preferably, in the leachate treatment system of the waste incineration plant, a stirring device is arranged in the intermediate tank.
The utility model also provides an adopt foretell waste incineration plant filtration liquid processing system to carry out the method that filtration liquid was handled, include following step in proper order:
(1) the percolate enters a regulating tank to regulate the water quantity and the water quality;
(2) the effluent of the regulating reservoir enters a hydrolysis acidification tank for hydrolysis acidification treatment, and macromolecular organic matters are decomposed into micromolecular organic matters;
(3) the effluent of the hydrolysis acidification tank enters a UASB anaerobic reaction tank for anaerobic treatment;
(4) the effluent of the UASB anaerobic reaction tank enters an air floatation tank for air floatation treatment to remove part of suspended matters and surfactants;
(5) the effluent of the air floatation tank enters a sedimentation tank;
(6) the effluent of the sedimentation tank enters an analytic deamination tower to remove ammonia nitrogen;
(7) the effluent of the resolving deamination tower enters an A/O reaction tank for biochemical treatment;
(8) the effluent of the A/O reaction tank enters an MBR membrane tank for treatment;
(9) the effluent of the MBR membrane tank enters a coagulation tank for coagulation treatment;
(10) the effluent of the coagulation tank enters an ozone catalytic oxidation tank to remove and decompose refractory organic matters;
(11) the effluent of the ozone catalytic oxidation tank enters an intermediate tank to remove residual ozone in water;
(12) the effluent of the intermediate tank enters a denitrification filter tank for denitrification treatment;
(13) and the effluent of the denitrification filter enters an activated carbon filter, and is subjected to adsorption treatment by activated carbon in the activated carbon filter and then discharged after reaching the standard.
Preferably, in the method, a steam inlet of the desorption deamination tower is connected with a waste heat steam supply pipeline of a waste incineration plant, and low-temperature and low-pressure steam generated by a waste incineration waste heat boiler is used for negative pressure desorption deamination.
The utility model discloses the beneficial effect who gains:
(1) utilize the utility model provides a processing system and method are handled the filtration liquid of msw incineration factory, and no membrane back dense phase liquid produces, solves the membrane back dense phase liquid treatment difficult problem that current filtration liquid treatment process exists, possesses the operation simultaneously and stabilizes, and the cleaning cycle interval time is long, produces the guaranteed advantage of water quality.
(2) The utility model discloses utilize the low temperature low pressure steam of msw incineration factory to carry out the analytic deamination of negative pressure, the deamination is efficient, and is fast, can effectively reduce energy consumption and treatment cost. Meanwhile, compared with the traditional ammonia stripping method and ammonia evaporation method, on one hand, alkali is not needed to be added to adjust the pH value in the resolving deamination process, the medicament usage amount and the sludge generation amount are reduced, and the treatment cost of a deamination unit is further reduced; on the other hand, the concentration of the removed ammonia gas is higher, ammonia water is easy to collect and prepare, the ammonia gas can be further used for a flue gas denitration unit of a burning plant, and the percolate treatment cost and the overall operation cost of a waste burning plant can be effectively reduced; the C/N ratio of the leachate can be obviously improved by deamination, favorable conditions are created for the subsequent biochemical process, and the hydraulic retention time and aeration energy consumption in the biochemical process section are reduced, so that the treatment cost is reduced.
(3) The tail gas discharged by the ozone catalytic oxidation unit and residual ozone in the tail gas are fully utilized to wash and regenerate the active carbon in the active carbon filter tank, so that the service time of the active carbon is prolonged, and the energy consumption and the cost of the leachate tail end treatment are reduced.
Drawings
Figure 1 shows a schematic view of a leachate treatment system of a waste incineration plant according to the present invention.
Detailed Description
In order to facilitate understanding of the present invention, the leachate treatment system of the waste incineration plant of the present invention is further described with reference to the drawings and the following examples, which are not intended to limit the scope of the present invention.
Fig. 1 shows a schematic view of a leachate treatment system of a waste incineration plant according to the utility model, comprising successively connected:
(1) a regulating pool: the leachate enters an adjusting tank to adjust the water quantity and the water quality, so that the fluctuation of the production quantity and the water quality of the leachate caused by seasonal changes is reduced, and the balance and the stability of the water quantity and the water quality of a leachate treatment facility are ensured;
(2) a hydrolysis acidification pool: the effluent of the regulating reservoir enters a hydrolysis acidification pool, and the long-chain high molecular polymer in the water is destroyed and degraded in the hydrolysis acidification pool, so that the B/C ratio in the water is improved. After hydrolysis and acidification, the pH value of water is reduced to about 5.4, and the pH value is adjusted to 6.8-7.2 by using sodium carbonate so as to meet the condition of methanation in the UASB anaerobic reaction tank;
(3) UASB anaerobic reaction jar: the effluent of the hydrolysis acidification tank enters a UASB anaerobic reaction tank to remove most organic matters in the water;
(4) an air floatation tank: and (3) enabling the effluent of the UASB anaerobic reaction tank to enter an air floatation tank, removing a surfactant, floating oil and part of suspended matters which may exist in the effluent, and simultaneously realizing foam separation. The gas-water ratio is controlled to be 10: 1-30: 1, and the ascending flow rate is controlled to be 1.2-3 m/h;
(5) a sedimentation tank: the effluent of the air floatation tank enters a sedimentation tank for solid-liquid separation, so that the SS content in the supernatant is reduced;
(6) resolving the deamination tower: the supernatant of the sedimentation tank exchanges heat with the effluent of the desorption deamination tower in a condenser, and then the temperature of the supernatant is increased and the supernatant enters the desorption deamination tower. The method is characterized in that low-temperature and low-pressure steam (the temperature is 100-130 ℃, the absolute pressure is 0.3-0.5 MPa) generated by a waste incineration plant is utilized, under the condition of negative pressure (the absolute pressure is 0.04-0.08 MPa), alkali is not needed to be added for adjusting the pH of water, most of ammonia nitrogen in the water is removed, the C/N ratio is increased to 6-9: 1, and the subsequent biochemical process is facilitated. The water after deamination and the inlet water of the desorption deamination tower enter a subsequent biochemical unit after heat exchange and temperature reduction in a condenser. Ammonia-containing steam discharged from the top of the desorption and deamination tower is condensed in a partial condenser at the top of the tower to generate ammonia water, and the ammonia water with the concentration of 8-16% is prepared by controlling the reflux amount of the ammonia water and the temperature of the partial condenser at the top of the tower and is used for a flue gas denitration unit of an incineration plant;
the embodiment of the present invention provides an analysis deamination tower, which is applied in 2019, 07/19 th, and published in 2019, 10/08 th, CN 110304779A-chinese published patent application "a method and a treatment system for materialization deamination of anaerobic effluent of landfill leachate", which is a negative pressure deamination tower, applied in: zhongxiao engineering and technology research institute, ltd. For the sake of brevity, this is incorporated by reference, but all technical disclosure of the above-mentioned applications should be considered as a part of the technical disclosure of the present invention.
(7) A/O + MBR biochemical treatment unit: the effluent of the resolving deamination tower enters an A/O + MBR biochemical treatment unit. The sludge concentration in the A/O reaction tank is 4-6 g/L, the anoxic zone mainly performs denitrification on nitrate in water, and the dissolved oxygen in the anoxic zone is controlled to be 0.2-0.5 mgand/L, removing organic matters in the water and carrying out nitration reaction in the aerobic zone, wherein the dissolved oxygen in the aerobic zone is controlled to be 3-5 mg/L. The MBR membrane tank is externally arranged, a curtain type MBR ultrafiltration membrane is arranged in the membrane tank, and the membrane flux is 0.1-0.2 m3/(m2·d)；
(8) A coagulation tank: and (3) enabling effluent of the AO + MBR biochemical treatment unit to enter a coagulation tank, and adding a certain amount of coagulant to realize solid-liquid separation in the coagulation tank so as to remove suspended matters and part of COD in water. The coagulant is one or more of polymeric ferric sulfate, polymeric aluminum chloride and polyacrylamide, and the adding amount is 0.1-2 g/L;
(9) an ozone catalytic oxidation tank: and (3) enabling the supernatant of the coagulation tank to enter an ozone catalytic oxidation tank, wherein the adding amount of ozone is 0.1-5 g/L, and hydroxyl radicals and the like generated by ozone under the action of a catalyst are utilized to destroy organic matters which are difficult to degrade in water, so that the organic matters are changed into micromolecular organic matters, and the B/C ratio in water is further improved. The ozone catalytic oxidation tank is filled with filler (catalyst), the catalyst is granular activated carbon, zeolite or aluminum oxide loaded with one or more metal elements of Mn, Co, Ni and the like, and the catalyst has a catalytic effect and can adsorb suspended matters possibly existing in the effluent of the coagulation unit, so that the quality of the influent water of the subsequent filter unit is improved. The ozone source is an ozone generator, and the air source used by the ozone generator is air or industrial oxygen. When air is used as the air source of the ozone generator, an air compressor and an air separation device are required to be arranged, so that moisture in the air is removed, and the oxygen concentration in the air is increased to more than 90%. When industrial oxygen (liquid oxygen) is used as a gas source, an air compressor and an air separation device do not need to be equipped, but the liquid oxygen needs to be supplemented periodically;
(10) an intermediate tank: the effluent of the ozone catalytic oxidation tank enters an intermediate tank, and a stirring device is matched with the intermediate tank and used for removing residual ozone in water and reducing the dissolved oxygen in water;
(11) a denitrification filter tank: the effluent of the intermediate tank enters a denitrification filter tank for denitrification;
(12) an activated carbon filter: and the effluent of the denitrification filter enters an active carbon filter, and is discharged after reaching the standard after being subjected to active carbon adsorption treatment.
Furthermore, the tail gas containing ozone discharged from the ozone catalytic oxidation tank is introduced into the activated carbon filter tank to regenerate the activated carbon, so that the service cycle of the activated carbon is prolonged, the replacement frequency of the activated carbon is reduced, and the tail end treatment cost is reduced. The ozone in the tail gas is completely decomposed in the activated carbon filter and can be directly emptied.
Further, sludge and scum produced by the UASB anaerobic tank, the sedimentation tank, the AO + MBR unit, the coagulation tank and the air flotation tank are collected, dehydrated to the water content of below 60 percent and put into an incinerator of a garbage incineration plant for incineration treatment.
Example 1
The basic water quality of the percolate of a certain garbage incineration plant in Hebei is as follows: the pH value is 6.5-6.8; the COD concentration is 60000-80000 mg/L; the ammonia nitrogen concentration is 600-800 mg/L; the total nitrogen concentration is about 1100-1400 mg/L. Utilize the utility model discloses a filtration liquid processing system carries out filtration liquid and handles, and concrete method step is as follows:
1. the percolate enters a regulating tank to regulate the water quantity and the water quality;
2. the effluent of the regulating tank enters a hydrolysis acidification tank, after hydrolysis acidification, the pH value of the water is reduced to about 5.2, and the pH value is regulated to 6.8-7.2 by using sodium carbonate so as to meet the condition of methanation produced in the UASB anaerobic reaction tank;
3. the effluent of the hydrolysis acidification tank enters a UASB anaerobic reaction tank to remove most organic matters in the water. The pH value of the effluent is 7.6-8.0, the COD concentration is 8000-10000 mg/L, the ammonia nitrogen concentration is 2400-2900 mg/L, and the SS is 10-12 g/L;
4. the effluent of the UASB anaerobic reaction tank enters an air floatation tank, the air-water ratio is controlled at 18:1, and the ascending flow rate is controlled at 2.5 m/h;
5. the effluent of the air floatation tank enters a sedimentation tank;
6. the effluent of the sedimentation tank is subjected to heat exchange with the effluent of the desorption deamination tower, the temperature is raised to 42 ℃, and the effluent enters the desorption deamination tower. The deamination is carried out under the conditions of 0.06MPa of pressure and 75 ℃ of water by using low-temperature and low-pressure steam (100-130 ℃ of temperature and 0.3-0.5 MPa of pressure) generated by a waste incineration plant to provide heat. The ammonia nitrogen concentration of the water after deamination is reduced to be below 800mg/L, and the ammonia nitrogen is subjected to heat exchange with inlet water of an analytic deamination tower and is cooled to about 35 ℃ to enter a subsequent biochemical unit. Condensing ammonia-containing steam discharged from the top of the resolving deamination tower in a partial condenser at the tower top to prepare ammonia water with the concentration of 10%;
7. the effluent of the resolving deamination tower enters an A/O + MBR biochemical treatment unit. The sludge concentration in the A/O reaction tank is 5g/L, the dissolved oxygen in the anoxic zone is controlled to be 0.3-0.4 mg/L, and the dissolved oxygen in the aerobic zone is controlled to be 4-4.5 mg/L. The membrane flux of the MBR membrane tank is 0.2m3/(m2D), effluent COD is 500-620 mg/L, ammonia nitrogen concentration is 20-40 mg/L, total nitrogen concentration is 60-80 mg/L, total phosphorus is 1-2 mg/L, and pH is 6.5-6.8;
8. the effluent of the A/O + MBR biochemical unit enters a coagulation tank, polymeric ferric sulfate and polyacrylamide are sequentially added, the adding amount is 1g/L and 1.5mg/L respectively, and the pH value of the supernatant is adjusted to about 8;
9. the supernatant of the coagulation tank enters an ozone catalytic oxidation tank, and the adding amount of ozone is 1.4 g/L;
10. the effluent of the ozone catalytic oxidation tank enters an intermediate tank to remove residual ozone in water;
11. the effluent of the intermediate tank enters a denitrification filter tank for denitrification;
12. the effluent of the denitrification filter enters an active carbon filter, and the final effluent quality has the following main indexes: the pH value is about 7, the COD concentration is 40-43 mg/L, the BOD concentration is 6-9 mg/L, the ammonia nitrogen concentration is 1.9-4.2 mg/L, the total nitrogen concentration is 11-15 mg/L, the total phosphorus concentration is about 0.4-0.8 mg/L, the SS is 12-20 mg/L, and the chroma is 18-22, and all meet the emission limit value standard in the table 3 of the control standard of a domestic garbage landfill (GB16889 and 2008).
In addition, the tail gas containing ozone discharged from the ozone catalytic oxidation tank is introduced into the activated carbon filter tank, the activated carbon is washed and regenerated, and the ozone in the tail gas is completely decomposed in the activated carbon filter tank and can be directly emptied; sludge and scum produced by a UASB anaerobic tank, a sedimentation tank, an AO + MBR unit, a coagulation tank and an air flotation tank are collected and dehydrated to the water content of below 60 percent, and then are put into an incinerator for incineration treatment.
Example 2
The basic water quality of the percolate of a certain garbage incineration plant in Hebei is as follows: the pH value is 6.2-6.6; the COD concentration is 40000-60000 mg/L; the ammonia nitrogen concentration is 500-650 mg/L; the total nitrogen concentration is about 860-1050 mg/L.
The leachate was treated as in example 1, with the difference that:
the pH value of the effluent of the adjusting tank is reduced to about 5.2, and the pH value is adjusted to 6.9-7.1 by using sodium carbonate;
the air-water ratio of the air floatation tank is controlled at 15:1, and the ascending flow rate is controlled at 3 m/h;
the effluent of the sedimentation tank is subjected to heat exchange with the effluent of the desorption deamination tower, the temperature is raised to 40 ℃, and the effluent enters the desorption deamination tower;
providing heat by using low-temperature and low-pressure steam (the temperature is 100-110 ℃, and the pressure is 0.3-0.4 MPa) generated by a waste incineration plant, and carrying out deamination under the conditions that the pressure is 0.068MPa and the water temperature is 80 ℃;
the sludge concentration in the A/O system is 4g/L, the dissolved oxygen in the anoxic zone is controlled to be 0.3-0.4 mg/L, and the dissolved oxygen in the aerobic zone is controlled to be 3.5-4 mg/L; the membrane flux of the MBR membrane tank is 0.16m3/(m2·d)；
And adding polymeric ferric sulfate and polyacrylamide into the coagulation tank, wherein the adding amount is 1.4g/L and 1.7mg/L respectively. The adding amount of ozone is 1.2 g/L;
after the leachate is treated, the final effluent quality has the following main indexes: the pH value is about 6.8, the COD concentration is 46-50 mg/L, the BOD concentration is 8-11 mg/L, the ammonia nitrogen concentration is 4-6 mg/L, the total nitrogen concentration is about 12-16 mg/L, the total phosphorus concentration is about 0.3-0.8 mg/L, the SS is 8-15 mg/L, and the chromaticity is 11-19, and all the emission limit value standards in table 3 of the domestic garbage landfill control standard (GB16889-2008) are met.
Comparative example 1
Compared with example 1, the difference is only that: does not contain an air floatation tank and a sedimentation tank, and the effluent of the UASB anaerobic reaction tank directly enters an analytic deamination tower. The concentration of SS in water is higher, so that the deamination unit is blocked and sludge is deposited after running for a period of time, the treatment effect is reduced, water inlet needs to be stopped, and water scale and sludge in the device are removed.
Comparative example 2
Compared with example 1, the difference is only that: does not contain an intermediate tank, and the effluent of the ozone catalytic oxidation tank directly enters the denitrification filter tank. As part of unreacted ozone still exists in the effluent and the dissolved oxygen in the effluent is higher, the biochemical reaction process of denitrifying bacteria in the denitrifying filter is inhibited, so that the denitrification effect is reduced, and the total nitrogen concentration is about 17-19 mg/L, which is close to the total nitrogen concentration emission limit standard of 20mg/L in table 3 of the domestic garbage landfill control Standard (GB 16889-2008).
Although the invention has been described in detail in the foregoing by way of general description, specific embodiments and experiments, it will be apparent to those skilled in the art that certain modifications and improvements may be made thereto based on the invention. Therefore, such modifications and improvements are intended to be within the scope of the invention as claimed.
Claims (8)
1. The utility model provides a refuse incineration factory filtration liquid processing system which characterized in that includes equalizing basin, hydrolysis-acidification pool, UASB anaerobic reaction jar, air supporting pond, sedimentation tank, analysis deamination tower, AO reaction tank, MBR membrane cisterna, coagulating basin, ozone catalytic oxidation pond, intermediate tank, denitrification filtering pond and active carbon filtering pond that connect gradually along the rivers direction.
2. The leachate treatment system of claim 1, further comprising a sludge dewatering device, wherein the sludge outlet of the UASB anaerobic reaction tank, the scum outlet of the flotation tank, the sludge outlet of the sedimentation tank, the sludge outlet of the A/O reaction tank, the sludge outlet of the MBR membrane tank, and the sludge outlet of the coagulation tank are connected to the sludge dewatering device.
3. The leachate treatment system of claim 1, further comprising a heat exchanger, wherein the effluent of the settling tank passes through the heat exchanger before being connected to the desorption deamination tower, and the effluent of the bottom of the desorption deamination tower passes through the heat exchanger before being connected to the A/O reaction tank.
4. The leachate treatment system of the waste incineration plant of claim 1, wherein a steam inlet is formed in the lower part of the desorption deamination tower, and the steam inlet of the desorption deamination tower is connected with a waste heat steam supply pipeline of the waste incineration plant.
5. The leachate treatment system of the waste incineration plant of claim 1, wherein a dephlegmator is arranged at the top of the desorption deamination tower, and a top gas outlet of the desorption deamination tower is connected to an inlet of the dephlegmator.
6. The landfill leachate treatment system of claim 1, wherein the gas outlet of the ozone catalytic oxidation tank is connected to the activated carbon filter tank.
7. The leachate treatment system of claim 1, wherein the MBR membrane tank is an external MBR membrane tank, and curtain MBR membrane modules are arranged in the external MBR membrane tank.
8. The leachate treatment system of claim 1, wherein a stirring device is disposed in the intermediate tank.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111847796A (en) * | 2020-07-31 | 2020-10-30 | 中节能工程技术研究院有限公司 | System and method for treating leachate of waste incineration plant |
| CN112645547A (en) * | 2021-01-19 | 2021-04-13 | 江西楚杭环保科技有限公司 | Sewage treatment process and system for refuse landfill |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111847796A (en) * | 2020-07-31 | 2020-10-30 | 中节能工程技术研究院有限公司 | System and method for treating leachate of waste incineration plant |
| CN111847796B (en) * | 2020-07-31 | 2024-04-09 | 中节能工程技术研究院有限公司 | Leachate treatment system and method for garbage incineration plant |
| CN112645547A (en) * | 2021-01-19 | 2021-04-13 | 江西楚杭环保科技有限公司 | Sewage treatment process and system for refuse landfill |
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