CN107840533A - A kind of processing method of garbage burning factory percolate - Google Patents
A kind of processing method of garbage burning factory percolate Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
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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
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
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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
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
- C02F5/06—Softening water by precipitation of the hardness using calcium compounds
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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
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/08—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents
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Abstract
The invention discloses a kind of processing method of garbage burning factory percolate, this method includes:(1) Anaerobic Treatment:Garbage burning factory percolate obtains treatment fluid I through UASB Anaerobic Treatments;(2) sofening treatment:Softening medicament is added into treatment fluid I, after carrying out Chemical softnessprocess, then through TMF membrane filtrations, obtains treatment fluid II;(3) deamination is handled:Treatment fluid II is pumped into negative pressure ammonia still, is passed through steam and is carried out deamination processing, obtains treatment fluid III;(4) film advanced treating:After treatment fluid III is cooled to≤35 DEG C, pH is to 6~7 for regulation, then through DTRO membrane filtrations, obtains producing water.The present invention can effectively be removed ammonia nitrogen, total nitrogen, the organic matter in percolate, be ensured stable water production qualified discharge or reuse using the group technology processing garbage burning factory percolate of " pretreatment+Anaerobic Treatment+TMF softenings+deamination processing+film advanced treating ".
Description
Technical field
The present invention relates to technical field of landfill leachate treatment, more particularly to a kind of processing side of garbage burning factory percolate
Method.
Background technology
Under " garbage-surrounded city " increasingly serious situation, waste incineration and generating electricity turns into " minimizing, innoxious, recycling " place
Put the best mode of house refuse.
The percolate of burning electricity generation factory is mainly produced by being fermented during precipitation and dumping.Percolate is
The extremely unstable organic wastewater of a kind of pollutant concentration height, complicated component, change, can cause serious secondary dirt to surrounding environment
Dye, and be detrimental to health.Containing substantial amounts of organic matter, nitrogen Phosphorous species and species is various and content overproof in percolate
Heavy metal classes material, wherein CODCr、BOD5, heavy metal, ammonia nitrogen, total nitrogen and salt content it is all very high so that total nitrogen and difficult degradation
Organic matter is treated as difficult point.
At present, the processing method on percolate is numerous, such as:
Publication No. is that CN102826726A patent of invention document discloses a kind of garbage burning factory percolate treating process,
The technique comprises the following steps:1) percolate introduces grid setting pot, after removing the suspension and silt in percolate, oozes
Filtrate overflow is to regulating reservoir;2) start the bottom submersible agitator for being arranged on regulating reservoir, percolate is stirred, through water pump after 5~7 days
It is pumped into preliminary sedimentation tank;3) percolate enters preliminary sedimentation tank with flow velocity less than 30mm/s in regulating reservoir, in preliminary sedimentation tank the sedimentation time be 1~
1.5h, to precipitating sludge and organic matter, percolate enters the intermediate pool I of UASB reactors from preliminary sedimentation tank overflow;4) by
Between percolate in pond with UASB ponds are pumped into, to intermediate pool II, intermediate pool I's is upper for the production water overflow in UASB ponds
Layer a part of overflow of clear liquid forms in UASB and circulated, protect the water temperature in UASB reactors in circulating inside to intermediate pool II
30 DEG C~35 DEG C are held, intermediate pool II another part water, oxygen compatibility pool is delivered to by pumping;5) the water outlet overflow of UASB reactors is extremely
Oxygen compatibility pool, starting the underwater stirrer being arranged in oxygen compatibility pool, sewage is sufficiently stirred hydrolysis, then overflow enters aeration tank,
Organic matter in the waste water abundant nitration reaction in the presence of microorganism in aeration tank, during nitration reaction pH value control exist
7.5, the water that nitrification liquid flows back into oxygen compatibility pool from aeration tank is to enter 5-10 times of aeration tank water by oxygen compatibility pool direct current, exposure
The water outlet in gas pond carries out mud-water separation through second pond;6) second pond supernatant overflow removes second pond to coagulation-flocculation pond is entered
SS and COD in supernatantCrAfterwards, pumped through water pump to film processing system;7) into film processing system clear water by ultrafiltration and
Directly discharged into clear water well after nanofiltration filtering.
Publication No. is that CN201620094U patent of invention document discloses a kind of municipal solid waste incinerator percolate processing
System, the processing system include regulating reservoir, and the regulating reservoir connects UBF ponds and A/O ponds respectively, and the UBF ponds connect A/O ponds,
The A/O ponds connect follow-up processing pond.The utility model enters according to raw water and the C/N of UBF ponds water outlet ratios, regulation sewage
UBF ponds and the sewage ratio that A/O ponds are directly entered without UBF ponds, reach the rational C/N for being advantageous to ammonia nitrogen removal
Than the ammonia nitrogen in sewage being removed, so that it is guaranteed that the NH of percolate3- N can be discharged with stably reaching standard.
In addition, conventional garbage leachate treatment process also has " pretreatment+anaerobism+MBR (A/O+UF)+film depth
The technique that processing " is combined, the ammonia nitrogen in percolate is mainly removed by nitration denitrification, COD contents are reduced, using film depth
Processing removes the COD of difficult degradation.Mineralized nitrogen is then converted to by technique mesophytization processing using nitration denitrification for nitrate nitrogen
Nitrogen removes, and floor space is big, and energy consumption is big;In addition, system does not remove effect to calcium therein, magnesium, silicon, heavy metal plasma
Fruit, cause to reach the precipitation of saturation solubility product after the dense side concentration of film after entering film advanced treating, cause fouling membrane, influence film depth
The producing water ratio and service life of processing.
The content of the invention
The invention provides a kind of processing method of garbage burning factory percolate, the processing method can effectively remove percolate
In ammonia nitrogen, total nitrogen, organic matter, improve producing water ratio, reduce operating cost.
A kind of processing method of garbage burning factory percolate, including:
(1) Anaerobic Treatment:Garbage burning factory percolate obtains treatment fluid I through UASB Anaerobic Treatments;
(2) sofening treatment:Softening medicament is added into treatment fluid I, after carrying out Chemical softnessprocess, then through TMF membrane filtrations,
Obtain treatment fluid II;
(3) deamination is handled:Treatment fluid II is pumped into negative pressure ammonia still, is passed through steam and is carried out deamination processing, obtains treatment fluid
III;
(4) film advanced treating:Treatment fluid III is cooled to≤35 DEG C, and pH is to 6~7, then through DTRO membrane filtrations for regulation, obtains
Produce water.
Anaerobic Treatment, chemical tendering, ammonia still process processing and DTRO film advanced treatings are combined by processing method of the present invention, and
Using specific improved UASB reactor, TMF films, negative pressure ammonia still, DTRO, can effectively remove in garbage burning factory percolate
COD, BOD, ammonia nitrogen, total nitrogen, Ca2+、Mg2+、SiO2Deng.
For the condensed recovery of the ammonia that dissociates in step (3) of the present invention through ammonia still into ammoniacal liquor, ammoniacal liquor is back to incineration plant cigarette
Qi exhaustion nitre.
Preferably, the residence time of the UASB Anaerobic Treatments is 15~20d, temperature is 35 DEG C ± 0.5 DEG C.Selected temperature
Spend for anaeration in normal temperature running temperature, under conditions of high disposal effect is ensured, energy consumption is low, the appropriate extension residence time, ensures
Effluent quality, when the residence time is in 15~20d, water outlet COD clearance can be made to be not less than 95%.Using it is new online can be more
Change formula water-locator, water body makes water body form eddy flow by tangentially entering tank body, ensure waterpower evenly distributing on cross section and
Stirring;Preferably, the upflow velocity of the UASB Anaerobic Treatments is 2~3m3/m2·h。
Preferably, the softening medicament is at least one of calcium hydroxide, sodium carbonate and sodium hydroxide;Work as treatment fluid
In I during basicity > calcium hardness, the softening medicament is calcium hydroxide and sodium hydroxide;When basicity < calcium hardness in treatment fluid I,
The softening medicament is sodium hydroxide and/or sodium carbonate.
Preferably, in step (2), it is 10.5~11 that softening medicament to pH value is added into treatment fluid I.
Preferably, in step (2), described TMF films are PVDF sintered membranes, and membrane flux is 250~350LMH, membrane area
For 2.58~4.25m2/, film pressure is 0.07~0.7MPa, and film acid and alkali-resistance can be pH 0~14.
Preferably, in step (3), the temperature of the negative pressure ammonia still is 80~90 DEG C, absolute pressure is 20~
40kPa, steam consumption quantity 80-120kg/t, NH in the water outlet of negative pressure ammonia still3 -N≤40mg/L。
Preferably, during the DTRO membrane filtrations, membrane flux is 10~15LMH, membrane area 9.405m2/,
Operating pressure is 5~10MPa.
Compared with prior art, the invention has the advantages that:
(1) present invention uses the group technology of " pretreatment+Anaerobic Treatment+sofening treatment+deamination processing+film advanced treating "
Handle garbage burning factory percolate, can effectively remove ammonia nitrogen, total nitrogen, the organic matter in percolate, improve producing water ratio up to 85% with
On, reduce operating cost.
(2) processing method of the present invention eliminates MBR system (i.e. denitrification+nitrification+UF) technique in original technique, significantly
Reduce investment and running cost.
(3) processing method anaerobic system clearance of the present invention is high, and methane yield is big, and methane gas can be recycled to burner hearth
Combustion-supporting or marsh gas power generation utilizes.
(4) ammonia nitrogen in processing method waste water of the present invention produces 10~15% ammoniacal liquor after ammonia still recovery condensation, returns
For the processing of incineration plant denitrating flue gas.
(5) the production water that processing method of the present invention obtains can reach《Urban sewage reutilization industry water standard》GB/T
19923-2005 cools down recycle water standard.
(6) processing method of the present invention because cancel MBR (denitrification+nitrification+UF) technique, greatly reduce system investment,
Operating cost and Noise upon Environment secondary pollution (need to consume substantial amounts of oxygen in nitrifying process, need high-power roots blower oxygen supply,
Roots blower noise is more than 85db);In addition, anaerobism, which requires that clearance is higher, can produce more biogas (return combustion or natural pond
Gas liquefied gas) and the condensate ammonia Water circulation isolated through ammonia still in denitration, reach resource recycling, substantially reduce operation
Expense.
Brief description of the drawings
Fig. 1 is the schematic flow sheet of the processing method of embodiment 1.
Embodiment
The following example and comparative example choose identical garbage burning factory percolate and are handled and compared, wherein, because of rubbish
The factors such as percolate influent quality and component of refuse and weather are related, and the influent quality of percolate fluctuates in certain scope,
Acquired results data are with average value.
Embodiment 1
A kind of processing method of garbage burning factory percolate, is comprised the following steps that:
(1) Anaerobic Treatment:Garbage burning factory percolate is pumped into UASB reactors, carries out Anaerobic Treatment, UASB anaerobism
The residence time of processing is 18d, and temperature is 35 DEG C ± 0.5 DEG C, upflow velocity 2-3m3/m2·h;Water outlet use addition for
50-200ppm PAC carries out flocculation sediment as flocculant, obtains treatment fluid I and sludge I;
Partial sludge backflow reenters the sludge concentration of stable UASB in UASB reactors, and it is dense that excess sludge is passed through sludge
Contracting is concentrated in pond, and obtains dewatered sludge through dewatering system, then carries out harmless treatment.
(2) sofening treatment:It is 10.5~11 that softening medicament to pH value is added into treatment fluid I, and control process liquid I pH is
Basicity and calcium hardness content in 10.5~11, measure treatment fluid II, when obtaining that basicity < calcium is hard in treatment fluid II, using hydroxide
Sodium and sodium carbonate, mass ratio are 8~5:1, sofening treatment is carried out, then through TMF membrane filtrations, obtain treatment fluid II and concentrate I;Its
In, the TMF films use PVDF sintered membranes, membrane flux 250LMH, membrane area 2.58m2/, pressure be 0.07~
0.7Mpa, film acid and alkali-resistance can be pH 0-14;
Concentrate I is precipitated, supernatant is obtained and is passed through in gray- water pond, it is equal to reenter progress homogeneous in regulating reservoir
Amount, and carry out follow-up process;Precipitating sludge obtains dewatered sludge through dewatering system, then carries out harmless treatment.
(3) deamination is handled:Treatment fluid II is pumped into negative pressure ammonia still, is 80~90 using temperature in automatic steam control tower
DEG C, absolute pressure is 20~40kPa, and steam consumption quantity is 80~120kg/t, carries out deamination processing, obtains treatment fluid III (NH3 -N
≤ 40mg/L) and ammoniacal liquor;Ammoniacal liquor can re-start industrial reuse.
(4) film advanced treating:After pending liquid III is cooled to≤35 DEG C, after regulation treatment fluid III pH to 6~7, then
Through DTRO membrane filtrations, obtain producing water (overall producing water ratio is 90%);Wherein, the membrane flux of DTRO films is 15LMH, and membrane area is
9.405m2/, 5~10MPa of operating pressure, the Membrane cleaning cycle is 4-6 weeks.
The effluent index of measure water inlet index and each step, as a result as shown in table 1.
Table 1 is using the water inlet index of the processing method of embodiment 1 and the effluent index of each step
Comparative example 1
For this comparative example in addition to step 2 and step 3 is lacked, remaining content is same as Example 1;Same measure water inlet index with
And the effluent index of each step, as a result as shown in table 2;In step (4), the cleaning frequency of film is 2-4 weeks;Overall producing water ratio is
60%.
Table 2 is using the water inlet index of the processing method of comparative example 1 and the effluent index of each step
Comparative example 2
For this comparative example in addition to step 2 is lacked using TMF, remaining content is same as Example 1;Same measure water inlet index with
And the effluent index of each step, as a result as shown in table 3;In step (4), the cleaning frequency of film is 4-6 weeks;Overall producing water ratio is
65%.
Table 3 is using the water inlet index of the processing method of comparative example 2 and the effluent index of each step
Comparative example 3
For this comparative example in addition to step 3 is lacked, remaining content is same as Example 1;Same measure water inlet index and each step
Rapid effluent index, as a result as shown in table 4;In step (4), the cleaning frequency of film is 2-4 weeks;Overall producing water ratio is 85%.
Table 4 is using the water inlet index of the processing method of comparative example 3 and the effluent index of each step
Comparative example 4
For this comparative example in addition to step 2 and step 3 are substituted for into biochemical treatment, remaining content is same as Example 1;It is same to survey
Surely the effluent index for index and each step of intaking, as a result as shown in table 4;In step (4), the cleaning frequency of film is 4-6 weeks;It is whole
Body producing water ratio is 75%.
Wherein, comprise the following steps that:
(1) Anaerobic Treatment:Garbage burning factory percolate is pumped into UASB reactors, carries out Anaerobic Treatment, UASB anaerobism
The residence time of processing is 18d, and temperature is 35 DEG C ± 0.5 DEG C, upflow velocity 2-3m3/m2H, water outlet obtain treatment fluid I.
(2) biochemical treatment:Treatment fluid I enters two level A/O biochemical treatment systems, and two level A/O total residence times are 10 days, temperature
Spend for 30-35 DEG C, A ponds dissolved oxygen < 0.5mg/L, O pond dissolved oxygen is 2mg/L, and water outlet obtains treatment fluid II.
(3) UF processing systems:Treatment fluid II obtains treatment fluid III through UF membrane filtrations;Wherein, the membrane flux of UF films is
70LMH, membrane area 27.2m2/, operating pressure 0.4-0.6MPa.
(4) film advanced treating:Treatment fluid III obtains producing water through DTRO membrane filtrations;Wherein, the membrane flux of DTRO films is
15LMH, membrane area 9.405m2/, operating pressure 5-10MPa.
The effluent index of measure water inlet index and each step, as a result as shown in table 5.
Table 5 is using the water inlet index of the processing method of comparative example 4 and the effluent index of each step
Claims (8)
- A kind of 1. processing method of garbage burning factory percolate, it is characterised in that including:(1) Anaerobic Treatment:Garbage burning factory percolate obtains treatment fluid I through UASB Anaerobic Treatments;(2) sofening treatment:Softening medicament is added into treatment fluid I, after carrying out Chemical softnessprocess, then through TMF membrane filtrations, is obtained Treatment fluid II;(3) deamination is handled:Treatment fluid II is pumped into negative pressure ammonia still, is passed through steam and is carried out deamination processing, obtains treatment fluid III;(4) film advanced treating:Treatment fluid III is cooled to≤35 DEG C, and pH is to 6~7 for regulation, then through DTRO membrane filtrations, obtains producing water.
- 2. processing method as claimed in claim 1, it is characterised in that the residence time of the UASB Anaerobic Treatments be 15~ 20d, temperature are 35 DEG C ± 0.5 DEG C.
- 3. processing method as claimed in claim 1, it is characterised in that the upflow velocity of the UASB Anaerobic Treatments is 2~3m3/ m2·h。
- 4. processing method as claimed in claim 1, it is characterised in that the softening medicament is calcium hydroxide, sodium carbonate and hydrogen At least one of sodium oxide molybdena;When basicity > calcium hardness in treatment fluid I, the softening medicament is calcium hydroxide and hydroxide Sodium;When basicity < calcium hardness in treatment fluid I, the softening medicament is sodium hydroxide and/or sodium carbonate.
- 5. processing method as claimed in claim 1, it is characterised in that in step (2), softening medicament is added into treatment fluid I It is 10.5~11 to pH value.
- 6. processing method as claimed in claim 1, it is characterised in that in step (2), described TMF films are PVDF sintered membranes, Membrane flux is 250~350LMH, and membrane area is 2.58~4.25m2/, film pressure is 0.07~0.7MPa, and film acid and alkali-resistance can be PH 0~14.
- 7. processing method as claimed in claim 1, it is characterised in that in step (3), the temperature of the negative pressure ammonia still is 80 ~90 DEG C, absolute pressure is 20~40kPa, steam consumption quantity 80-120kg/t, NH in the water outlet of negative pressure ammonia still3 -N≤40mg/ L。
- 8. processing method as claimed in claim 1, it is characterised in that during the DTRO membrane filtrations, membrane flux 10 ~15LMH, membrane area 9.405m2/, operating pressure is 5~10MPa.
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Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN108516651A (en) * | 2018-05-04 | 2018-09-11 | 北京天地人环保科技有限公司 | Processing method for incineration plant landfill leachate |
CN108928980A (en) * | 2018-07-04 | 2018-12-04 | 张家港澳卓尔生物技术装备有限公司 | Percolate coprocessing system and percolate cooperative processing method |
CN110500585A (en) * | 2019-07-18 | 2019-11-26 | 光大环保技术研究院(南京)有限公司 | A kind of waste incineration and generating electricity waste heat ammonia steaming system |
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 |
CN112573776A (en) * | 2020-12-23 | 2021-03-30 | 上海康恒环境股份有限公司 | Novel percolate deamination system and deamination method thereof |
CN112591984A (en) * | 2020-11-24 | 2021-04-02 | 南京万德斯环保科技股份有限公司 | Zero-discharge treatment method and system for landfill leachate |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2004230273A (en) * | 2003-01-30 | 2004-08-19 | Mitsubishi Kakoki Kaisha Ltd | Method for treating organic waste |
CN202658046U (en) * | 2012-06-01 | 2013-01-09 | 赵义武 | Landfill leachate treating system |
CN102976543A (en) * | 2012-12-18 | 2013-03-20 | 深圳市能源环保有限公司 | Garbage leachate disposal method and system |
CN103570157A (en) * | 2013-10-25 | 2014-02-12 | 浙江博世华环保科技有限公司 | Method for processing percolate membrane treatment concentrated solution of refuse landfill |
CN104591432A (en) * | 2014-12-31 | 2015-05-06 | 浙江博世华环保科技有限公司 | Processing method of landfill leachate film concentrated solution |
-
2017
- 2017-10-19 CN CN201710979953.0A patent/CN107840533B/en active Active
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2004230273A (en) * | 2003-01-30 | 2004-08-19 | Mitsubishi Kakoki Kaisha Ltd | Method for treating organic waste |
CN202658046U (en) * | 2012-06-01 | 2013-01-09 | 赵义武 | Landfill leachate treating system |
CN102976543A (en) * | 2012-12-18 | 2013-03-20 | 深圳市能源环保有限公司 | Garbage leachate disposal method and system |
CN103570157A (en) * | 2013-10-25 | 2014-02-12 | 浙江博世华环保科技有限公司 | Method for processing percolate membrane treatment concentrated solution of refuse landfill |
CN104591432A (en) * | 2014-12-31 | 2015-05-06 | 浙江博世华环保科技有限公司 | Processing method of landfill leachate film concentrated solution |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN108516651A (en) * | 2018-05-04 | 2018-09-11 | 北京天地人环保科技有限公司 | Processing method for incineration plant landfill leachate |
CN108928980A (en) * | 2018-07-04 | 2018-12-04 | 张家港澳卓尔生物技术装备有限公司 | Percolate coprocessing system and percolate cooperative processing method |
CN110500585A (en) * | 2019-07-18 | 2019-11-26 | 光大环保技术研究院(南京)有限公司 | A kind of waste incineration and generating electricity waste heat ammonia steaming system |
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 |
CN112591984A (en) * | 2020-11-24 | 2021-04-02 | 南京万德斯环保科技股份有限公司 | Zero-discharge treatment method and system for landfill leachate |
CN112573776A (en) * | 2020-12-23 | 2021-03-30 | 上海康恒环境股份有限公司 | Novel percolate deamination system and deamination method thereof |
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