CN111704314A - High ammonia nitrogen type landfill leachate treatment process - Google Patents

High ammonia nitrogen type landfill leachate treatment process Download PDF

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CN111704314A
CN111704314A CN202010527701.6A CN202010527701A CN111704314A CN 111704314 A CN111704314 A CN 111704314A CN 202010527701 A CN202010527701 A CN 202010527701A CN 111704314 A CN111704314 A CN 111704314A
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water
ammonia nitrogen
leachate
treatment
effluent
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张晋华
于飞
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Nanjing University of Science and Technology
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Nanjing University of Science and Technology
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • 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
    • 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
    • C02F1/285—Treatment of water, waste water, or sewage by sorption using synthetic organic 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
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
    • 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
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • 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
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • 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
    • C02F2101/10—Inorganic compounds
    • C02F2101/20—Heavy metals or heavy metal compounds
    • 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
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/005—Processes using a programmable logic controller [PLC]
    • 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
    • C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Physical Water Treatments (AREA)

Abstract

The invention relates to a high ammonia nitrogen type landfill leachate treatment process, which comprises the steps of lifting leachate from a landfill collecting tank to enter an adjusting tank for reaction, pumping the reacted mixed solution into a deamination tower, and enabling the deamination tower effluent to enter a denitrification device after the effluent meets the standards determined by an RTOS system; in the denitrification device, the organic matters in the inlet water and the nitrate radical refluxed by the MBR are subjected to denitrification process, the removal of COD and TN of the organic matters is synchronously realized, and the muddy water is separated by a separation membrane of the MBR unit; the separated water further enters an NF system to complete the separation of a part of salt and organic matters, and the NF produced water is pumped into an RO unit to complete the final purification process. The process can effectively solve the impact influence of the water inlet index on the system, greatly improve the treatment efficiency of the waste leachate, realize the stable standard-reaching operation of the system and be based on the characteristics of the waste water, particularly when the ammonia nitrogen index has large fluctuation and the adjusting tank cannot buffer.

Description

High ammonia nitrogen type landfill leachate treatment process
Technical Field
The invention belongs to the technical field of high ammonia nitrogen type waste leachate treatment, and particularly relates to a high ammonia nitrogen type waste leachate treatment process.
Background
Currently, the biological treatment technology is mainly used for treating the Chinese waste leachate, and the research and the application of the physicochemical treatment technology are mainly used for treating the foreign waste leachate. For waste water with high concentration and complex components, the waste leachate cannot be treated by biotechnology to reach the discharge standard, and particularly for the waste leachate of old age, the biological treatment has no effect basically.
In fact, the leachate treatment of most sanitary landfills in china is discharged without reaching the standards established in china, which causes serious groundwater pollution. In the physical and chemical treatment technology of the leachate, most suspended matters and macromolecular organic matters in the leachate can be removed by coagulating sedimentation, but the generated chemical sludge is difficult to treat. The activated carbon adsorption only has adsorption removal capacity for substances with molecular weight less than 1000 in the leachate, and the adsorption treatment cost is very high. The membrane treatment technology has extremely high one-time investment and operation cost, and is not suitable for leachate treatment of most of Chinese landfill sites except leachate treatment of a few small scale in China and high effluent quality requirement.
The electrochemical oxidation and photocatalytic oxidation technology has high treatment cost and can not meet the requirement of large-scale treatment, and a reaction device is extremely difficult to realize in practical engineering application. In contrast, the chemical catalytic oxidation technology of leachate has the problem that the price of common oxidants (ozone and hydrogen peroxide) is higher, but the consumption of the oxidants can be reduced and the utilization rate of the oxidants can be improved by synthesizing a novel catalyst, so that the cost for treating the leachate is reduced.
Through the domestic industry development and the technical development in recent years, the mainstream process is basically determined as follows: adjusting, coagulating sedimentation pretreatment, activated sludge method treatment, membrane method advanced treatment and discharging; however, domestic waste leachate is influenced obviously by the types of the contained waste and geographical climatic conditions, the quality deviation of the produced leachate is extremely large, the deviation of the water quality change in the operation process is extremely large, the operation of a waste water treatment system is extremely unstable and exceeds the standard almost to the normal state, particularly, the treatment technology for the high ammonia nitrogen type waste leachate is incomplete, when the ammonia nitrogen index has large deviation, a rear-end biochemical system is influenced obviously, the integral operation state is influenced to cause an over-standard accident, even the biochemical system is crashed to cause long-time production stop loss, and in order to solve the problem of stable operation of the system, a conventional DCS (distributed control system) needs more manual intervention management, and at least 10 operators are configured.
Disclosure of Invention
The invention aims to provide a treatment process of high ammonia nitrogen type waste leachate.
The technical scheme for realizing the purpose of the invention is as follows:
a treatment process of high ammonia nitrogen type waste leachate comprises the following steps
The leachate is lifted from a garbage field collecting tank and enters an adjusting tank, the adjusting tank temporarily stores the entering garbage leachate, the garbage leachate is mechanically stirred to prevent substance deposition, the adjusting tank is subjected to steam temperature rise, and three medicaments of organic sulfur, PAC and PAM are added;
pumping the reacted mixed liquid into a deamination tower, wherein the whole deamination tower is of a carbon steel corrosion-resistant structure, ammonia blown off by the deamination tower enters an ammonia absorption tower for absorption, part of the absorbed ammonia water flows back to the deamination tower for water inlet, the ammonia nitrogen concentration entering the deamination tower is improved, ammonia separation is promoted, part of the ammonia water is crystallized and transported out, and the effluent of the deamination tower enters a denitrification device after the index of the effluent of the deamination tower is judged to be qualified by an RTOS system;
in the denitrification device, the influent organic matter and the nitrate radical refluxed by the MBR are subjected to denitrification process, the removal of COD and TN of the organic matter is synchronously realized, the effluent of the denitrification device enters the MBR unit for further biodegradation of COD, the residual ammonia nitrogen is completely converted into the nitrate radical, and the mud and water are separated by a separation membrane of the MBR unit;
the separated water further enters an NF system to complete the separation of partial salt and organic matters, the NF produces water and is pumped into an RO unit to complete the final purification process, the NF concentrated water flows back to a denitrification tank to be reprocessed, the RO unit produces water which can completely meet the discharge standard, and the RO concentrated water is discharged into a refuse landfill and is absorbed and filtered through a soil layer of the landfill and then enters an adjusting tank to be processed. (RO concentrated water is salt, heavy metal and residual COD.)
Further, in the regulating tank:
the residence time is 1-2h, two pools are arranged and alternately run.
The steam is heated to 30-40 ℃ to promote the separation of ammonia in water.
The addition amount of organic sulfur is 100-120mg/l for absorbing heavy metals.
PAC dosage of 150-200mg/l is used for flocculating suspended matters.
PAM is added in an amount of 1-2mg/l to help coagulate suspended matter.
Further, in the deamination tower:
water is fed from the top, air is fed from the bottom, mud and water are separated from the desliming part, and NH3-N of the deamination effluent is less than or equal to 100 mg/l.
And (3) degassing part: the velocity of the overflowing gas is 10-12m/s, and the high gas velocity is helpful for stirring water bloom in the multilayer plate filler, so that gas-water separation is realized.
A desliming section; hydraulic load 2-3m3The square meter is divided into three parts, namely, per square meter, the settling time is 3-4h, the longer settling time and the settling height can effectively reduce the disturbance of water inflow to a settling layer, and the settling effect is improved.
Filling a multilayer board: the arrangement angle is 60-70 deg.C, and the arrangement area of every plate is 0.5-0.8 square meter.
Filling with an inclined plate: the plate spacing is 50-80mm, and the height of the filler layer is 1-1.2 m.
And (3) pH condition: 9-11.
Gas-water ratio: 3500: 1.
ammonia reflux ratio of ammonia absorption tower: 15 percent.
Further, in the denitrification tank:
the TN of the effluent is less than or equal to 30 mg/l.
Denitrification rate: 0.02-0.03(kgNO 3-N)/(kgMLSS. d).
Reaction temperature: 20-40 ℃.
Depth of the pool body: 4-6 m.
The carbon-nitrogen ratio is as follows: 10-11: 1.
and (3) pH condition: 7-10.
Further, in MBR unit
COD of the effluent is less than or equal to 100mg/l, and NH3-N is less than or equal to 5 mg/l.
COD load factor: 0.05-0.07kgBOD 5/(kgMLSS. d).
MLSS concentration: 12000-15000 mg/l.
Cleaning cycle: 1 time/6 months.
Reaction temperature: 20-40 ℃.
Membrane flux: 150 plus 200L/square meter.
Membrane module requirements: CSMBR biofilm.
Further, in NF systems
COD of the effluent is less than or equal to 50mg/l, NH3-N is less than or equal to 0.1mg/l, and TDS is less than or equal to 2000 mg/l.
Water yield: 95 percent.
The arrangement in the NF system is as follows: the first-stage NF directly discharges water, the concentrated water of the first-stage NF enters the second-stage NF for treatment, and the second-stage NF simultaneously treats the water inlet with the same quantity as the first-stage NF
And (3) filtering pressure: 5-6kpa
Further, the RO unit sets:
COD of effluent is less than or equal to 10mg/l, NH3-N is less than or equal to 0.1mg/l, TDS is less than or equal to 0.1mg/l
Water yield: 85 percent of
The arrangement mode is as follows: two stage filtration
And (3) filtering pressure: 10-14kpa
RTOS system:
in the aspect of a supervision system, each stage of the invention needs intellectualization and automation, an RTOS system is introduced, corresponding detection equipment and a PLC sensor are arranged in each processing link, corresponding information is transmitted to a general control center, a corresponding alarm system is arranged, if the processing requirement is not met or an abnormal working state exists, an alarm is automatically given, and the shutdown and the inspection of the processing system are carried out.
And each stage is provided with online monitoring, the subsequent index prediction is completed through a particle swarm algorithm, the key index limit is preset in advance, and the emergency program of the system is carried out when the system exceeds the standard.
Compared with the prior art, the invention has the following remarkable advantages:
1. the method can effectively resist the water quality impact of inlet water, particularly the ammonia nitrogen index impact, and before entering a biochemical section, the main index is not changed along with the change of raw water and is basically constant, so that the requirement of limiting the index of the inlet water of the system in the running process is avoided;
2. the deamination system completes three-substance separation of suspended matters, dissolved ammonia and water in one step, shortens process units, reduces investment, operation and management cost, can improve the removal rate of ammonia nitrogen effluent indexes (compared with the traditional stripping) by more than 50 percent, and simultaneously reduces the operation PH range and temperature range, thereby realizing energy consumption reduction;
3. compared with the prior art, the maintenance period of the adopted MBR is prolonged by 1 time, the biochemical sludge amount is reduced to 0NF water yield and is improved by 15 percent, and the investment and maintenance cost of an NF system are reduced;
4. the system is provided with the RTOS control system, and the on-line indexes of the system are predicted in the next step while being monitored, so that the problem that the system exceeds the standard is effectively prevented, the automatic control operation capacity of the system is improved, and the number of operators is reduced.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Fig. 2 is a schematic diagram of the operation of a deamination tower unit.
FIG. 3 is a diagram illustrating operation of the RTOS system.
Detailed Description
The invention will be further explained with reference to the drawings
The invention relates to a treatment process of high ammonia nitrogen type waste leachate, which can eliminate the influence on the change of water inlet indexes, and particularly can effectively solve the impact influence of the water inlet indexes on a system when the ammonia nitrogen indexes fluctuate greatly and an adjusting tank cannot buffer, thereby greatly improving the treatment efficiency of the waste leachate, realizing the stable standard operation of the system and being based on the characteristics of the waste water.
The process technology can reduce the operation cost by more than 20 percent, reduce the operation personnel to 4 persons by an RTOS (real-time operating system) control system and realize the automatic control operation capability of the system
A process for treating high ammonia nitrogen type waste leachate is shown in figure 1, and comprises the following steps
The leachate is lifted from a garbage field collecting tank and enters an adjusting tank, the adjusting tank temporarily stores the entering garbage leachate, the garbage leachate is mechanically stirred to prevent substance deposition, the adjusting tank is subjected to steam temperature rise, and three medicaments of organic sulfur, PAC and PAM are added;
pumping the reacted mixed liquid into a deamination tower, wherein the whole deamination tower is of a carbon steel corrosion-resistant structure, ammonia blown off by the deamination tower enters an ammonia absorption tower for absorption, part of the absorbed ammonia water flows back to the deamination tower for water inlet, the ammonia nitrogen concentration entering the deamination tower is improved, ammonia separation is promoted, part of the ammonia water is crystallized and transported out, and the effluent of the deamination tower enters a denitrification device after the index of the effluent of the deamination tower is judged to be qualified by an RTOS system; the deamination tower operates as shown in figure 2.
In the denitrification device, the influent organic matter and the nitrate radical refluxed by the MBR are subjected to denitrification process, the removal of COD and TN of the organic matter is synchronously realized, the effluent of the denitrification device enters the MBR unit for further biodegradation of COD, the residual ammonia nitrogen is completely converted into the nitrate radical, and the mud and water are separated by a separation membrane of the MBR unit;
the separated water further enters an NF system to complete the separation of partial salt and organic matters, the NF produces water and is pumped into an RO unit to complete the final purification process, the NF concentrated water flows back to a denitrification tank to be reprocessed, the RO unit produces water which can completely meet the discharge standard, and the RO concentrated water is discharged into a refuse landfill and is absorbed and filtered through a soil layer of the landfill and then enters an adjusting tank to be processed. (RO concentrated water is salt, heavy metal and residual COD.)
In the regulating reservoir:
the residence time is 1-2h, two pools are arranged and alternately run.
The steam is heated to 30-40 ℃ to promote the separation of ammonia in water.
The addition amount of organic sulfur is 100-120mg/l for absorbing heavy metals.
PAC dosage of 150-200mg/l is used for flocculating suspended matters.
PAM is added in an amount of 1-2mg/l to help coagulate suspended matter.
In the deamination tower:
water is fed from the top, air is fed from the bottom, mud and water are separated from the desliming part, and NH3-N of the deamination effluent is less than or equal to 100 mg/l.
And (3) degassing part: the velocity of the overflowing gas is 10-12m/s, and the high gas velocity is helpful for stirring water bloom in the multilayer plate filler, so that gas-water separation is realized.
A desliming section; hydraulic load 2-3m3The square meter is divided into three parts, namely, per square meter, the settling time is 3-4h, the longer settling time and the settling height can effectively reduce the disturbance of water inflow to a settling layer, and the settling effect is improved.
Filling a multilayer board: the arrangement angle is 60-70 deg.C, and the arrangement area of every plate is 0.5-0.8 square meter.
Filling with an inclined plate: the plate spacing is 50-80mm, and the height of the filler layer is 1-1.2 m.
And (3) pH condition: 9-11.
Gas-water ratio: 3500: 1.
ammonia reflux ratio of ammonia absorption tower: 15 percent.
In the denitrification tank:
the TN of the effluent is less than or equal to 30 mg/l.
Denitrification rate: 0.02-0.03(kgNO 3-N)/(kgMLSS. d).
Reaction temperature: 20-40 ℃.
Depth of the pool body: 4-6 m.
The carbon-nitrogen ratio is as follows: 10-11: 1.
and (3) pH condition: 7-10.
In MBR unit
COD of the effluent is less than or equal to 100mg/l, and NH3-N is less than or equal to 5 mg/l.
COD load factor: 0.05-0.07kgBOD 5/(kgMLSS. d).
MLSS concentration: 12000-15000 mg/l.
Cleaning cycle: 1 time/6 months.
Reaction temperature: 20-40 ℃.
Membrane flux: 150 plus 200L/square meter.
Membrane module requirements: CSMBR biofilm.
In NF system
COD of the effluent is less than or equal to 50mg/l, NH3-N is less than or equal to 0.1mg/l, and TDS is less than or equal to 2000 mg/l.
Water yield: 95 percent.
The arrangement in the NF system is as follows: the first-stage NF directly discharges water, the concentrated water of the first-stage NF enters the second-stage NF for treatment, and the second-stage NF simultaneously treats the water inlet with the same quantity as the first-stage NF
And (3) filtering pressure: 5-6kpa
And (3) RO system:
COD of effluent is less than or equal to 10mg/l, NH3-N is less than or equal to 0.1mg/l, TDS is less than or equal to 0.1mg/l
Water yield: 85 percent of
The arrangement mode is as follows: two stage filtration
And (3) filtering pressure: 10-14kpa
RTOS system:
in the aspect of a supervision system, each stage of the invention needs intellectualization and automation, an RTOS system is introduced, corresponding detection equipment and a PLC sensor are arranged in each processing link, corresponding information is transmitted to a general control center, a corresponding alarm system is arranged, if the processing requirement is not met or an abnormal working state exists, an alarm is automatically given, and the shutdown and the inspection of the processing system are carried out. As shown in particular in figure 3.
And each stage is provided with online monitoring, the subsequent index prediction is completed through a particle swarm algorithm, the key index limit is preset in advance, and the emergency program of the system is carried out when the system exceeds the standard.
The prediction results of the invention by adopting the particle swarm optimization are shown in the following table 1
TABLE 1 prediction results table of particle swarm algorithm
Figure BDA0002534233790000071
The invention carries out process modification deamination device, changes the material of the membrane, uses a nanofiltration system and optimizes a supervision system on the traditional process of a certain project, and carries out comparative analysis on the processing results of the modified system and the system before modification, wherein the specific results are shown in tables 2, 3, 4, 5, 6 and 7.
TABLE 2 Water discharge index before and after System reconstruction
Figure BDA0002534233790000081
TABLE 3 contaminant removal Rate before and after System retrofit
Figure BDA0002534233790000082
Table 4 energy saving situation of running of front and rear fans
Figure BDA0002534233790000083
Table 5 aspects of sludge discharge before and after reforming
Figure BDA0002534233790000084
TABLE 6 PAM usage
Figure BDA0002534233790000085
TABLE 7 data sheet (mg/l) of main index of water output in the first half of 8 months before and after reconstruction
Figure BDA0002534233790000091

Claims (10)

1. A treatment process of high ammonia nitrogen type waste leachate is characterized by comprising the following steps:
the leachate is lifted from a garbage field collecting tank and enters an adjusting tank, the adjusting tank temporarily stores the entering garbage leachate, the garbage leachate is mechanically stirred to prevent substance deposition, the adjusting tank is subjected to steam temperature rise, and three medicaments of organic sulfur, PAC and PAM are added;
pumping the reacted mixed liquid into a deamination tower, wherein the whole deamination tower is of a carbon steel corrosion-resistant structure, ammonia blown off by the deamination tower enters an ammonia absorption tower for absorption, part of the absorbed ammonia water flows back to the deamination tower for water inlet, the ammonia nitrogen concentration entering the deamination tower is improved, ammonia separation is promoted, part of the ammonia water is crystallized and transported out, and the effluent of the deamination tower enters a denitrification device after the index of the effluent of the deamination tower is judged to be qualified by an RTOS system;
in the denitrification device, the influent organic matter and the nitrate radical refluxed by the MBR are subjected to denitrification process, the removal of COD and TN of the organic matter is synchronously realized, the effluent of the denitrification device enters the MBR unit for further biodegradation of COD, the residual ammonia nitrogen is completely converted into the nitrate radical, and the mud and water are separated by a separation membrane of the MBR unit;
the separated water further enters an NF system to complete the separation of partial salt and organic matters, the NF produces water and is pumped into an RO unit to complete the final purification process, the NF concentrated water flows back to a denitrification tank to be reprocessed, the RO unit produces water meeting the discharge standard, and the RO concentrated water is discharged into a refuse landfill and is subjected to adsorption filtration through a soil layer of the landfill and then enters an adjusting tank to be processed.
2. The process for the treatment of landfill leachate of high ammonia nitrogen type according to claim 1, characterized in that in the conditioning tank:
the retention time is 1-2h, two pools are arranged and alternately run; raising the temperature of the steam to 30-40 ℃ to promote the separation of ammonia in water; the adding amount of organic sulfur is 100-120mg/l for absorbing heavy metal; PAC dosage of 150-; PAM is added in an amount of 1-2mg/l to help coagulate suspended matter.
3. The process for treatment of landfill leachate of high ammonia nitrogen type according to claim 1, characterized in that in the deamination tower:
water is fed from the top, air is fed from the bottom, mud and water are separated from the desliming part, and NH3-N of the deamination effluent is less than or equal to 100 mg/l;
and (3) degassing part: the velocity of the overflowing gas is 10-12m/s, and the high gas velocity is beneficial to stirring water bloom in the multilayer plate filler, so that gas-water separation is realized;
a desliming part: hydraulic load 2-3m3Per square meter, settling time is 3-4 h;
filling a multilayer board: the arrangement angle is 60-70 ℃, and the arrangement area of each plate is 0.5-0.8 square meter; filling with an inclined plate: the plate spacing is 50-80mm, and the height of the filler layer is 1-1.2 m;
and (3) pH condition: 9-11;
gas-water ratio: 3500: 1;
ammonia reflux ratio of ammonia absorption tower: 15 percent.
4. The process for the treatment of landfill leachate of high ammonia nitrogen type according to claim 1, characterized in that in the denitrification tank:
the TN of the effluent is less than or equal to 30 mg/l;
denitrification rate: 0.02-0.03(kgNO 3-N)/(kgMLSS. d);
reaction temperature: 20-40 ℃;
depth of the pool body: 4-6 m;
the carbon-nitrogen ratio is as follows: 10-11: 1;
and (3) pH condition: 7-10.
5. The process for treatment of landfill leachate of high ammonia nitrogen type according to claim 1, characterized in that in the MBR unit:
COD of the effluent is less than or equal to 100mg/l, and NH3-N is less than or equal to 5 mg/l;
COD load factor: 0.05-0.07kgBOD 5/(kgMLSS. d);
MLSS concentration: 12000-15000 mg/l;
cleaning cycle: 1 time/6 months;
reaction temperature: 20-40 ℃;
membrane flux: 150 plus 200L/square meter x d;
membrane module requirements: CSMBR biofilm.
6. The process for treatment of high ammonia nitrogen type landfill leachate according to claim 1, wherein in the NF system:
COD of the effluent is less than or equal to 50mg/l, NH3-N is less than or equal to 0.1mg/l, and TDS is less than or equal to 2000 mg/l;
water yield: 95 percent.
7. The process for treating waste leachate of high ammonia nitrogen type according to claim 6, wherein the arrangement mode in the NF system is as follows: the first-stage NF directly discharges water, the concentrated water of the first-stage NF enters the second-stage NF for treatment, and the second-stage NF simultaneously treats the water inlet with the same quantity as the first-stage NF; and (3) filtering pressure: 5-6 kpa.
8. The waste leachate treatment process of high ammonia nitrogen type according to claim 6, wherein the RO unit is configured to:
COD of the effluent is less than or equal to 10mg/l, NH3-N is less than or equal to 0.1mg/l, and TDS is less than or equal to 0.1 mg/l;
water yield: 85 percent;
the arrangement mode is as follows: two-stage filtration;
and (3) filtering pressure: 10-14 kpa.
9. The technology for treating high ammonia nitrogen type landfill leachate according to claim 1, wherein an RTOS system is provided specifically as follows:
introducing an RTOS system at each stage of the treatment process, arranging corresponding detection equipment and a PLC sensor in each treatment link, then transmitting corresponding information to a general control center, arranging a corresponding alarm system, and automatically alarming to stop and check the treatment system if the treatment requirement is not met or an abnormal working state exists.
10. The high ammonia nitrogen type landfill leachate treatment process according to claim 9, wherein each stage is provided with online monitoring, and the subsequent index prediction is completed through a particle swarm algorithm, and key index limits and emergency procedures of the overproof system are preset in advance.
CN202010527701.6A 2020-06-11 2020-06-11 High ammonia nitrogen type landfill leachate treatment process Pending CN111704314A (en)

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Application publication date: 20200925