CN111847796B - Leachate treatment system and method for garbage incineration plant - Google Patents
Leachate treatment system and method for garbage incineration plant Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 76
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 53
- 230000009615 deamination Effects 0.000 claims abstract description 50
- 238000006481 deamination reaction Methods 0.000 claims abstract description 50
- 239000012528 membrane Substances 0.000 claims abstract description 41
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 37
- 238000006243 chemical reaction Methods 0.000 claims abstract description 32
- 238000004056 waste incineration Methods 0.000 claims abstract description 30
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 claims abstract description 24
- 238000004062 sedimentation Methods 0.000 claims abstract description 21
- 230000003197 catalytic effect Effects 0.000 claims abstract description 20
- 238000005345 coagulation Methods 0.000 claims abstract description 20
- 230000015271 coagulation Effects 0.000 claims abstract description 20
- 230000003647 oxidation Effects 0.000 claims abstract description 19
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 19
- 230000020477 pH reduction Effects 0.000 claims abstract description 17
- 230000003301 hydrolyzing effect Effects 0.000 claims abstract description 5
- 239000010802 sludge Substances 0.000 claims description 22
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 16
- 230000007062 hydrolysis Effects 0.000 claims description 12
- 238000006460 hydrolysis reaction Methods 0.000 claims description 12
- 239000007789 gas Substances 0.000 claims description 11
- 230000001105 regulatory effect Effects 0.000 claims description 9
- 239000002918 waste heat Substances 0.000 claims description 6
- 238000003756 stirring Methods 0.000 claims description 3
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- 230000000694 effects Effects 0.000 abstract description 6
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 18
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 15
- 230000008569 process Effects 0.000 description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 11
- 229910052760 oxygen Inorganic materials 0.000 description 11
- 239000001301 oxygen Substances 0.000 description 11
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 229910021529 ammonia Inorganic materials 0.000 description 7
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 6
- 235000011114 ammonium hydroxide Nutrition 0.000 description 6
- 239000000149 chemical water pollutant Substances 0.000 description 6
- 208000028659 discharge Diseases 0.000 description 6
- 239000006228 supernatant Substances 0.000 description 6
- 230000003851 biochemical process Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000001223 reverse osmosis Methods 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
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- 239000003344 environmental pollutant Substances 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
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- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 3
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 3
- 235000011130 ammonium sulphate Nutrition 0.000 description 3
- 238000003795 desorption Methods 0.000 description 3
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- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 3
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 3
- 238000001728 nano-filtration Methods 0.000 description 3
- 229910052698 phosphorus Inorganic materials 0.000 description 3
- 239000011574 phosphorus Substances 0.000 description 3
- 229920002401 polyacrylamide Polymers 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- 238000000108 ultra-filtration Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- 238000005842 biochemical reaction Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000000701 coagulant Substances 0.000 description 2
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- 238000010438 heat treatment Methods 0.000 description 2
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- 241000894006 Bacteria Species 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
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- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
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- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
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- 239000010457 zeolite Substances 0.000 description 1
Classifications
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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
-
- 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
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
-
- 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
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
- C02F1/586—Treatment of water, waste water, or sewage by removing specified dissolved compounds by removing ammoniacal nitrogen
-
- 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
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- 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
-
- 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
-
- 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
- C02F2101/30—Organic compounds
-
- 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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion 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
- C02F3/30—Aerobic and anaerobic processes
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
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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 Of Suspended Particles By Flocculating Agents (AREA)
- Water Treatment By Sorption (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention relates to the technical field of sewage treatment, in particular to a leachate treatment system and method for a waste incineration plant. The leachate treatment system of the waste incineration plant comprises an adjusting tank, a hydrolytic acidification tank, a UASB anaerobic reaction tank, an air floatation tank, a sedimentation tank, an analytical deamination tower, an A/O reaction tank, an MBR membrane tank, a coagulation tank, an ozone catalytic oxidation tank, an intermediate tank, a denitrification filter tank and an activated carbon filter tank which are sequentially connected along the water flow direction. The leachate treatment system of the garbage incineration plant can enable the water quality of leachate generated by the garbage incineration plant to reach the discharge limit standard of the control standard of the household garbage landfill (GB 16889-2008), has the advantages of good treatment effect, lower cost, stable operation and no generation of thick phase liquid after membrane, and has better application and popularization prospects, and can be used for stable operation, cost reduction, efficiency enhancement and protection navigation of the garbage incineration plant.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a leachate treatment system and method for a waste incineration plant.
Background
In order to increase the calorific value of the garbage, garbage incineration plants need to ferment and ripen the garbage and leach out water in the garbage, so that organic wastewater with extremely complex components, namely garbage leachate, is 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 a type of polluted wastewater which is difficult to treat. Due to the complex composition, the landfill leachate cannot be effectively treated by a single process or a traditional biochemical process. On the other hand, the effluent of the percolate after treatment needs to meet the emission limit standard in table 2 of domestic refuse landfill control standard (GB 16889-2008). In areas with higher development density and smaller environmental capacity in China, the effluent of the percolate must reach the stricter emission limit standard in GB16889-2008 table 3, and higher requirements are put on the treatment process of the percolate. The existing percolate treatment process mainly has the problems of poor shock resistance, high running cost, difficult treatment of concentrated phase liquid after membrane and the like. Therefore, based on the characteristics of landfill leachate discharge and pollutants, the combined treatment process which is economical and reasonable, feasible in technology and stable and reliable in operation is developed aiming at the problems, is a key for solving the pain point of the waste incineration industry, and can be used for stable production, cost reduction, synergy and driving protection of an incineration plant.
The patent application with publication number of CN110028210A discloses a process for treating landfill leachate based on UASB technology. The percolate enters the UASB anaerobic reactor after pretreatment, and a heating system is arranged in the UASB reactor, so that the automatic heating in the anaerobic reaction process can be realized. UASB effluent enters a two-stage A/O biochemical reaction tank. The effluent of the two stages of A/O enters an ultrafiltration, nanofiltration and 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 percolate, and mainly has the problem that concentrated phase liquid after membrane is difficult to treat.
The patent application with publication number of CN110577333A discloses a new technology for treating percolate. The garbage percolate is pretreated and treated by a UASB reactor, then enters a denitrification and secondary nitrification process, and is treated by ultrafiltration, DTRO and RO membrane processes, and then the produced water is recycled. The invention increases low-pressure reverse osmosis after high-pressure reverse osmosis, improves the effluent quality of reverse osmosis, but still can not properly treat the concentrate after the membrane generated by the reverse osmosis unit.
The patent application with publication number CN110510825A discloses a landfill leachate treatment method and system of zero concentrated solution. The method mainly removes suspended matters, heavy metals and partial organic matters in water through alkali adding and coagulating sedimentation, simultaneously increases the pH value of the water to more than 10, then converts ammonia nitrogen in the water into ammonium sulfate through a membrane deamination technology, reduces the ammonia nitrogen concentration in the water, and improves the C/N ratio of the water. 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 is discharged after reaching the standard, and has the characteristics of no 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 imperfect, which is easy to cause fouling and blocking of the deamination membrane, and frequent membrane cleaning is caused, thus affecting the stable operation of the system. The ammonia removal process stage produces a lower concentration (no commercial value) of ammonium sulfate solution, requiring additional use of an evaporator to concentrate and crystallize the solution to obtain ammonium sulfate solids, which would undoubtedly increase overall operating costs. The tail end is used for removing residual pollutants in water in an adsorption and filtration mode, on one hand, as the pollutant concentration of the MBR effluent is still higher, the adsorbent is easy to adsorb and saturate, and the adsorbent needs to be frequently regenerated and the worn adsorbent needs to be replenished and replaced; on the other hand, the filter tank is easy to harden, frequent air-water backwashing is needed, and the filter material is not easy to replace. After the costs of adsorbent regeneration, filter material replacement and the like are shared, the actual treatment cost is increased.
Patent application publication No. 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 produced by the membrane treatment achieves the effect of zero emission by using low-temperature evaporation and solidification treatment. The disadvantage of this method is that: 1. the percolate directly enters a nanofiltration unit without pretreatment, organic matters and suspended matters in water are easy to cause membrane fouling and blockage, and the membrane is frequently cleaned/replaced, so that the running stability of the whole process is influenced; 2. the membrane deamination unit needs to be added with a large amount of alkali to adjust the pH value, which causes significant increase of the treatment cost. 3. After the concentrated water enters the evaporation system, high-concentration organic matters in the concentrated water easily form an azeotrope, so that the evaporation condensed water contains a large amount of organic pollutant. The condensed water returns to the nanofiltration unit, and the organic matters therein will aggravate the fouling of the unit.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a leachate treatment system and a method for a waste incineration plant, which can ensure that the quality of the treated leachate generated by the waste incineration plant reaches the discharge limit standard of the domestic refuse landfill control standard (GB 16889-2008), has the advantages of good treatment effect, lower cost, stable operation and no generation of thick phase liquid after membrane, thus having better application and popularization prospects, and being capable of ensuring stable operation, cost reduction, efficiency improvement and driving protection of the waste incineration plant.
In order to achieve the above purpose, the invention adopts the following technical scheme:
a leachate treatment system of a waste incineration plant comprises an adjusting tank, a hydrolytic acidification tank, a UASB anaerobic reaction tank, an air floatation tank, a sedimentation tank, an analytical deamination tower, an A/O reaction tank, an MBR membrane tank, a coagulation tank, an ozone catalytic oxidation tank, an intermediate tank, a denitrification filter tank and an activated carbon filter tank which are sequentially connected along the water flow direction.
Preferably, in the leachate treatment system of a waste incineration plant, the system further comprises a sludge dewatering device, wherein a sludge outlet of the UASB anaerobic reaction tank, a scum outlet of the air floatation tank, a sludge outlet of the sedimentation tank, a sludge outlet of the A/O reaction tank, a sludge outlet of the MBR membrane tank and a sludge outlet of the coagulation tank are all connected with the sludge dewatering device.
Preferably, in the leachate treatment system of a waste incineration plant, the system further comprises a heat exchanger, wherein the effluent of the sedimentation tank passes through the heat exchanger and is then connected to the analytical deamination tower, and the effluent at the bottom of the analytical deamination tower passes through the heat exchanger and is then connected to the A/O reaction tank.
Preferably, in the leachate treatment system of a waste incineration plant, a steam inlet is formed in the lower portion of the analytical deamination tower, and the steam inlet of the analytical deamination tower is connected with a waste heat steam supply pipeline of the waste incineration plant.
Preferably, in the leachate treatment system of a waste incineration plant, a dephlegmator is arranged at the top of the analytical deamination tower, and an air outlet at the top of the analytical deamination tower is connected to an inlet of the dephlegmator.
Preferably, in the leachate treatment system of the garbage incineration plant, a gas outlet of the ozone catalytic oxidation tank is connected to the activated carbon filter tank.
Preferably, in the leachate treatment system of a waste incineration plant, the MBR membrane tank is an external MBR membrane tank, and a curtain-type MBR membrane assembly 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 invention also provides a method for treating the percolate by adopting the percolate treatment system of the garbage incineration plant, which sequentially comprises the following steps:
(1) The percolate enters an adjusting tank to adjust the water quantity and the water quality;
(2) The effluent of the regulating tank enters a hydrolysis acidification tank for hydrolysis acidification treatment, and the 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, and part of suspended matters and surfactant are removed;
(5) The effluent of the air floatation tank enters a sedimentation tank;
(6) The effluent of the sedimentation tank enters an analytical deamination tower to remove ammonia nitrogen;
(7) The effluent of the analytical 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 organic matters which are difficult to degrade;
(11) The effluent of the ozone catalytic oxidation pond enters an intermediate pond to remove residual ozone in the water;
(12) The effluent of the middle tank enters a denitrification filter to carry out denitrification treatment;
(13) The effluent of the denitrification filter enters an activated carbon filter, and is discharged after reaching the standard after being adsorbed by activated carbon in the activated carbon filter.
Preferably, in the above method, the steam inlet of the desorption deamination tower is connected with a waste heat steam supply pipeline of a waste incineration plant, and the low-temperature low-pressure steam generated by the waste incineration waste heat boiler is used for negative pressure desorption deamination.
The beneficial effects obtained by the invention are as follows:
(1) The treatment system and the treatment method provided by the invention are used for treating the leachate of the waste incineration plant, the thick phase liquid is generated after no membrane is arranged, the difficult problem of treatment of the thick phase liquid after the membrane in the existing leachate treatment process is solved, and meanwhile, the treatment system and the treatment method have the advantages of stable operation, long cleaning period interval time and guaranteed water quality of produced water.
(2) The invention uses low-temperature low-pressure steam of the garbage incineration plant to carry out negative pressure analysis deamination, has high deamination efficiency and high speed, and can effectively reduce energy consumption and treatment cost. Meanwhile, compared with the traditional ammonia stripping method and ammonia distillation method, on one hand, the pH value is not required to be adjusted by adding alkali in the process of resolving ammonia, the dosage of medicament and the sludge production are reduced, and the treatment cost of the ammonia stripping 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, and the ammonia water can be further used for a flue gas denitration unit of an incineration plant, so that the treatment cost of percolate and the overall operation cost of the garbage incineration plant can be effectively reduced; deamination of percolate can also obviously improve the C/N ratio in water, create favorable conditions for the subsequent biochemical process, and reduce the hydraulic retention time and aeration energy consumption in the biochemical process section, thereby reducing the treatment cost.
(3) The tail gas discharged by the ozone catalytic oxidation unit and residual ozone in the tail gas are fully utilized to flush and regenerate the activated carbon in the activated carbon filter tank, so that the service time of the activated carbon is prolonged, and the energy consumption and the cost of the treatment of the tail end of percolate are reduced.
Drawings
Fig. 1 shows a schematic diagram of a leachate treatment system of a waste incineration plant according to the present invention.
Detailed Description
In order to facilitate the understanding of the present invention, the following description of the system and method for treating leachate from a waste incineration plant will be given with reference to the accompanying drawings and examples, which are not intended to limit the scope of the present invention.
Fig. 1 shows a schematic diagram of a leachate treatment system of a waste incineration plant according to the present invention, comprising, in succession:
(1) And (3) an adjusting tank: the percolate enters an adjusting tank to adjust the water quantity and the water quality, so that fluctuation caused by seasonal change of the generated amount and the water quality of the percolate is reduced, and balance and stability of the water quantity and the water quality of a percolate treatment facility are ensured;
(2) Hydrolysis acidification tank: the effluent from the regulating tank enters a hydrolytic acidification tank, and long-chain high polymer in the degraded water is destroyed in the hydrolytic acidification tank, 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 sodium carbonate is used for adjusting the pH value to 6.8-7.2, so that the pH value meets the condition of methanation in a UASB anaerobic reaction tank;
(3) UASB anaerobic reaction tank: the effluent of the hydrolysis acidification tank enters a UASB anaerobic reaction tank to remove most organic matters in the water;
(4) And (3) an air floatation tank: the effluent of the UASB anaerobic reaction tank enters an air floatation tank to remove possible surfactant, floating oil and partial suspended matters in the water, and foam separation is realized. The air-water ratio is controlled to be 10:1-30:1, and the rising flow rate is controlled to be 1.2-3 m/h;
(5) And (3) 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) Analytical deamination tower: and after heat exchange is carried out on supernatant fluid of the sedimentation tank and effluent water of the analytical deamination tower in a condenser, the temperature is raised, and the supernatant fluid enters the analytical deamination tower. The low-temperature low-pressure steam (the temperature is 100-130 ℃ and the absolute pressure is 0.3-0.5 MPa) generated by a garbage incineration plant is utilized, the pH value of water is not required to be regulated by adding alkali under the condition of negative pressure (the absolute pressure is 0.04-0.08 MPa), most ammonia nitrogen in the water is removed, and the C/N ratio is improved to 6-9:1, so that the subsequent biochemical process is facilitated. The deaminated water and the inflow water of the analytical deamination tower are subjected to heat exchange in a condenser and then enter a subsequent biochemical unit. Resolving ammonia-containing steam discharged from the top of the deamination tower to form ammonia water in a tower top partial condenser, and preparing 8-16% ammonia water by controlling the reflux amount of the ammonia water and the temperature of the tower top partial condenser for a flue gas denitration unit of an incineration plant;
in the embodiment of the invention, as for the analytical deamination tower, see Guo Zhi et al, published in China as patent application No. CN110304779A, published in 2019, 10 and 08, applied in 2019, on 19, a negative pressure deamination tower in a refuse leachate anaerobic effluent materialization deamination method and treatment system, applicant: energy saving engineering institute of technology, inc. For the sake of brevity, only this is cited, but all technical disclosures of the above application are also considered as part of the technical disclosure of the present application.
(7) a/O+MBR biochemical treatment unit: the effluent of the analytical 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 is mainly used for denitrifying nitrate in water, the dissolved oxygen in the anoxic zone is controlled to be 0.2-0.5 mg/L, the organic matters in the water are removed and the nitrification reaction occurs in the aerobic zone, and the dissolved oxygen in the aerobic zone is controlled to be 3-5 mg/L. The MBR membrane tank is external, a curtain type MBR ultrafiltration membrane is arranged in the membrane tank, and the membrane flux is 0.1-0.2 m 3 /(m 2 ·d)；
(8) And (3) coagulating the pool: the effluent of the AO+MBR biochemical treatment unit enters a coagulation tank, and solid-liquid separation is realized in the coagulation tank by adding a certain amount of coagulant, so that suspended matters and partial COD in the water are removed. 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) Ozone catalytic oxidation pond: the supernatant fluid of the coagulation tank enters an ozone catalytic oxidation tank, the ozone adding amount 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 refractory organic matters in water, so that the refractory organic matters are changed into micromolecular organic matters, and the B/C ratio in the water is further improved. The ozone catalytic oxidation pond is filled with filler (catalyst), the catalyst is granular active carbon, zeolite or aluminum oxide loaded with one or more metal elements of Mn, co, ni and the like, and besides the catalyst has a catalytic effect, suspended matters possibly existing in the effluent of the coagulation unit can be adsorbed, so that the water quality of the water fed by 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 a gas 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 be more than 90%. When industrial oxygen (liquid oxygen) is used as a gas source, an air compressor and an air separation device are not required to be arranged, but the liquid oxygen is required to be periodically supplemented;
(10) Intermediate pool: the effluent of the ozone catalytic oxidation pond enters an intermediate pond, and a stirring device is matched in the intermediate pond and is used for removing residual ozone in the water and reducing the dissolved oxygen in the water;
(11) Denitrification filter: the effluent of the middle tank enters a denitrification filter to carry out denitrification;
(12) Activated carbon filter: the effluent of the denitrification filter enters an activated carbon filter, and is discharged after reaching the standard after being adsorbed by the activated carbon.
Further, the ozone-containing tail gas discharged from the ozone catalytic oxidation pond is led into an 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 terminal treatment cost is reduced. Ozone in the tail gas is completely decomposed in the activated carbon filter tank, and can be directly emptied.
Further, sludge and scum generated by a UASB anaerobic tank, a sedimentation tank, an AO+MBR unit, a coagulation tank and an air floatation tank are collected, dehydrated to a water content of below 60%, and then put into an incinerator of a garbage incineration plant for incineration treatment.
Example 1
The basic water quality of the percolate of a certain refuse incineration plant in Hebei is as follows: the pH is 6.5-6.8; 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. The percolate treatment system is used for treating percolate, and the specific method comprises the following steps:
1. the percolate enters an adjusting tank to adjust the water quantity and the water quality;
2. the effluent of the regulating tank enters a hydrolysis acidification tank, the pH value of the water is reduced to about 5.2 after hydrolysis acidification, and sodium carbonate is used for regulating the pH value to 6.8-7.2, so that the condition of methanation in a UASB anaerobic reaction tank is met;
3. and (3) the effluent of the hydrolysis acidification tank enters a UASB anaerobic reaction tank to remove most of 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 rising flow rate is controlled at 2.5m/h;
5. the effluent of the air floatation tank enters a sedimentation tank;
6. after heat exchange is carried out on the effluent of the sedimentation tank and the effluent of the analytical deamination tower, the temperature is increased to 42 ℃ and the effluent enters the analytical deamination tower. The low-temperature low-pressure steam (the temperature is 100-130 ℃ and the pressure is 0.3-0.5 MPa) generated by a garbage incineration plant is used for providing heat, and deamination is carried out under the conditions of the pressure of 0.06MPa and the water temperature of 75 ℃. The ammonia nitrogen concentration of the deaminated water is reduced to below 800mg/L, and the deaminated water exchanges heat with the inlet water of the desorption deamination tower to be cooled to about 35 ℃ and enters the subsequent biochemical unit. The ammonia-containing steam discharged from the top of the analytical deamination tower is condensed in a tower top partial condenser to prepare ammonia water with the concentration of 10%;
7. the effluent of the analytical 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. Membrane flux of MBR membrane tank is 0.2m 3 /(m 2 ·d) The COD of the effluent is 500-620 mg/L, the ammonia nitrogen concentration is 20-40 mg/L, the total nitrogen concentration is 60-80 mg/L, the total phosphorus concentration is 1-2 mg/L, and the pH is 6.5-6.8;
8. adding the water discharged from the A/O+MBR biochemical unit into a coagulation tank, sequentially adding polymeric ferric sulfate and polyacrylamide with the addition amounts of 1g/L and 1.5mg/L respectively, and regulating the pH of the supernatant to about 8;
9. the supernatant of the coagulation tank enters an ozone catalytic oxidation tank, and the ozone adding amount is 1.4g/L;
10. the effluent of the ozone catalytic oxidation pond enters an intermediate pond to remove residual ozone in the water;
11. the effluent of the middle tank enters a denitrification filter to carry out denitrification;
12. the effluent of the denitrification filter enters an activated carbon filter, and the final effluent quality is mainly indicated as follows: the pH 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, the chromaticity is 18-22, and the discharge limit standards in table 3 of the domestic garbage landfill control standard (GB 16889-2008) are all satisfied.
In addition, the ozone-containing tail gas discharged from the ozone catalytic oxidation pond is introduced into an activated carbon filter tank to flush and regenerate the activated carbon, and the ozone in the tail gas is completely decomposed in the activated carbon filter tank and can be directly emptied; sludge and scum generated by a UASB anaerobic tank, a sedimentation tank, an AO+MBR unit, a coagulation tank and an air floatation tank are collected and dehydrated to a water content below 60%, and then put into an incinerator for incineration treatment.
Example 2
The basic water quality of the percolate of a certain refuse incineration plant in Hebei is as follows: the pH is 6.2-6.6; COD concentration is 40000-60000 mg/L; the ammonia nitrogen concentration is 500-650 mg/L; the total nitrogen concentration is about 860 to 1050mg/L.
The percolate was treated in the manner of example 1, with the difference that:
the pH value of the effluent of the regulating tank is reduced to about 5.2, and sodium carbonate is used for regulating the pH value to 6.9-7.1;
the air-water ratio of the air floatation tank is controlled to be 15:1, and the rising flow rate is controlled to be 3m/h;
after heat exchange is carried out on the effluent of the sedimentation tank and the effluent of the analytical deamination tower, the temperature is increased to 40 ℃ and the effluent enters the analytical deamination tower;
low-temperature low-pressure steam (the temperature is 100-110 ℃ and the pressure is 0.3-0.4 MPa) generated by a garbage incineration plant is utilized to provide heat, and deamination is carried out under the conditions of the pressure of 0.068MPa and the water temperature of 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; membrane flux of MBR membrane tank is 0.16m 3 /(m 2 ·d)；
The polymeric ferric sulfate and the polyacrylamide are added into the coagulation tank, and the addition amounts are 1.4g/L and 1.7mg/L respectively. Ozone adding amount is 1.2g/L;
after the percolate is treated, the main indexes of the final effluent quality are as follows: the pH 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, the chromaticity is 11-19, and the discharge limit standard in table 3 of domestic garbage landfill control standard (GB 16889-2008) is satisfied.
Comparative example 1
Compared with example 1, the difference is only that: the water discharged from the UASB anaerobic reaction tank directly enters the analytical deamination tower without an air floatation tank and a sedimentation tank. Because the SS concentration in the water is higher, the deamination unit is blocked and deposited with sludge after running for a period of time, the treatment effect is reduced, the water inlet is required to be stopped, and the scale and the sludge in the device are removed.
Comparative example 2
Compared with example 1, the difference is only that: the water discharged from the ozone catalytic oxidation tank directly enters the denitrification filter without an intermediate tank. Because part of unreacted ozone still exists in the effluent and the dissolved oxygen in the water is higher, the biochemical reaction process of denitrifying bacteria in the denitrification filter is inhibited, the denitrification effect is reduced, the total nitrogen concentration is about 17-19 mg/L, and the total nitrogen concentration is close to 20mg/L of the total nitrogen concentration emission limit standard in the table 3 of the domestic garbage landfill control standard (GB 16889-2008).
While the invention has been described in detail in the foregoing general description, embodiments and experiments, it will be apparent to those skilled in the art that modifications and improvements can be made thereto. Accordingly, such modifications or improvements may be made without departing from the spirit of the invention and are intended to be within the scope of the invention as claimed.
Claims (8)
1. The leachate treatment system of the waste incineration plant is characterized by comprising an adjusting tank, a hydrolytic acidification tank, a UASB anaerobic reaction tank, an air floatation tank, a sedimentation tank, an analytical deamination tower, an A/O reaction tank, an MBR membrane tank, a coagulation tank, an ozone catalytic oxidation tank, an intermediate tank, a denitrification filter tank and an activated carbon filter tank which are sequentially connected along the water flow direction;
the lower part of the analytic deamination tower is provided with a steam inlet, and the steam inlet of the analytic deamination tower is connected with a waste heat steam supply pipeline of a garbage incineration plant;
and a gas outlet of the ozone catalytic oxidation pond is connected to the activated carbon filter pond.
2. The leachate treatment system of a waste incineration plant according to claim 1, further comprising a sludge dewatering device, wherein the sludge outlet of the UASB anaerobic reaction tank, the scum outlet of the floatation 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 all connected with the sludge dewatering device.
3. The leachate treatment system of a waste incineration plant according to claim 1, further comprising a heat exchanger, wherein effluent of the sedimentation tank passes through the heat exchanger before being connected to the analytical deamination tower, and bottom effluent of the analytical deamination tower passes through the heat exchanger before being connected to the a/O reaction tank.
4. The leachate treatment system of a waste incineration plant according to claim 1, wherein a dephlegmator is arranged at the top of the analytical deamination tower, and a top gas outlet of the analytical deamination tower is connected to an inlet of the dephlegmator.
5. The leachate treatment system of the waste incineration plant of claim 1, wherein the MBR membrane tank is an external MBR membrane tank, and a curtain-type MBR membrane assembly is arranged in the external MBR membrane tank.
6. The leachate treatment system of a waste incineration plant according to claim 1, wherein a stirring device is arranged in the intermediate tank.
7. A method for leachate treatment using the leachate treatment system of a waste incineration plant according to any one of claims 1 to 6, comprising the following steps in order:
(1) The percolate enters an adjusting tank to adjust the water quantity and the water quality;
(2) The effluent of the regulating tank enters a hydrolysis acidification tank for hydrolysis acidification treatment, and the 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, and part of suspended matters and surfactant are removed;
(5) The effluent of the air floatation tank enters a sedimentation tank;
(6) The effluent of the sedimentation tank enters an analytical deamination tower to remove ammonia nitrogen;
(7) The effluent of the analytical 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 organic matters which are difficult to degrade;
(11) The effluent of the ozone catalytic oxidation pond enters an intermediate pond to remove residual ozone in the water;
(12) The effluent of the middle tank enters a denitrification filter to carry out denitrification treatment;
(13) The effluent of the denitrification filter enters an activated carbon filter, and is discharged after reaching the standard after being adsorbed by activated carbon in the activated carbon filter.
8. The method according to claim 7, wherein the steam inlet of the analytical deamination tower is connected with a waste heat steam supply pipeline of a waste incineration plant, and the low-temperature low-pressure steam generated by the waste incineration waste heat boiler is utilized for negative pressure analytical deamination.
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