CN212532677U - Landfill leachate treatment system - Google Patents
Landfill leachate treatment system Download PDFInfo
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- CN212532677U CN212532677U CN202021359835.3U CN202021359835U CN212532677U CN 212532677 U CN212532677 U CN 212532677U CN 202021359835 U CN202021359835 U CN 202021359835U CN 212532677 U CN212532677 U CN 212532677U
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Abstract
The utility model discloses a garbage filtrate treatment system; belonging to the technical field of garbage filtrate treatment; the system comprises a pretreatment unit, an ammonia removal unit, a biochemical treatment unit and a deep treatment unit which are connected in sequence; the pretreatment unit consists of an electrolytic Fenton reactor and a flocculation sedimentation tank which are connected in sequence, and the garbage leachate enters the electrolytic Fenton reactor in the composite bed through a water inlet pipe; the ammonia removal unit consists of a deamination device and an ammonia absorption tower which are connected in sequence; the deamination device is respectively connected with the flocculation sedimentation tank and the biochemical treatment unit; the utility model aims at providing a garbage leachate treatment system with reasonable structure and good use effect; the method is used for treating the garbage filtrate.
Description
Technical Field
The utility model relates to a sewage treatment system, more specifically say, especially relate to a landfill leachate treatment system.
Background
At present, the direct-discharge standard-reaching treatment processes of percolate which are widely applied in China are divided into three main types: physicochemical pretreatment, membrane advanced treatment, full membrane treatment, evaporation and ion exchange.
1. Physicochemical pretreatment and membrane advanced treatment: the operation of the biochemical system is influenced by a plurality of factors, and the biochemical system must be correctly adjusted according to the water quality condition and the climate condition of raw water, and the coordination among all units needs higher technical level. The growth of the microorganisms is greatly influenced by climate, and the operation of the biological strains needs to be cultured and domesticated; the operation is continuous and the operation cannot be stopped for a long time.
2. The whole membrane treatment is sensitive to the quality of raw water, the water outlet rate is greatly influenced by ss in inlet water, and the conductivity and the temperature are greatly influenced; the pre-stage is greatly influenced by pretreatment, the first-stage reverse osmosis is easy to block, the replacement frequency is high, the control is not easy, the membrane replacement cost is extremely high, and the operation cost is increased; the design exchange period of the primary membrane and the secondary membrane is difficult to control; the water yield is low, the recharge difficulty is high, the concentration and the conductivity of leachate in the later period of the landfill are increased, the membrane service cycle is short, the pressure difference of a required high-pressure pump is larger, and the operation cost is increased. And concentrated water is generated to cause secondary pollution.
3. The MVR evaporation and ion exchange evaporation process is relatively complex in operation and high in energy consumption, the main part is power consumption, and the energy is difficult to save by adjusting the running condition; the discharged gas may generate toxic gas or gas difficult to treat according to different components of the leachate, and whether the discharged gas completely reaches the standard needs to be verified; the requirement on the material of equipment is high, strong acid resistance is needed, if the concentration is too high, the evaporating pot needs to be cleaned by strong acid once, the cost of the medicament is high, and the cleaning is frequent.
4. Along with the development of the modern urbanization process, the production amount of municipal domestic garbage is multiplied, and the garbage leachate is increased continuously. The landfill leachate belongs to high-concentration organic wastewater. Because the landfill leachate contains a large amount of pollutants such as ammonia nitrogen, COD, heavy metal ions and the like, the landfill leachate is not suitable for being directly subjected to biochemical treatment. The conventional methods adopt a flocculation-precipitation method or a flocculation-air floatation method for pretreatment, but the treatment efficiency is low.
5. It not only has high COD, but also has extremely high ammonia nitrogen, and is generally between 500-2000 mg/L. The traditional physical treatment method of high ammonia nitrogen is a catalytic deaminizing method, and the principle is that a single-stage deaminizing tower is built, landfill leachate to be treated is adjusted to be alkaline, air is blown in, and stripping is carried out under a high gas-liquid ratio, so that ammonia nitrogen in waste liquid is forced to enter the atmosphere, and the purpose of treating ammonia nitrogen is achieved.
6. In cold areas, due to low temperature in winter, the growth of microorganisms in a biochemical system is slow, so that the treatment efficiency of the biochemical system is low. The COD of the effluent is obviously increased.
7. Therefore, the research of the utility model is reliable, the impact resistance is strong, the operation is stable, the treatment efficiency is high, the heat energy utilization and the ammonia removal recovery can be realized, and the secondary pollution is avoided.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to the not enough of above-mentioned prior art, provide a landfill leachate processing system rational in infrastructure, excellent in use effect.
The technical scheme of the utility model is realized like this: a landfill leachate treatment system comprises a pretreatment unit, an ammonia removal unit, a biochemical treatment unit and a deep treatment unit which are connected in sequence;
the pretreatment unit consists of an electrolytic Fenton reactor and a flocculation sedimentation tank which are connected in sequence, and the garbage leachate enters the electrolytic Fenton reactor in the composite bed through a water inlet pipe;
the ammonia removal unit consists of a deamination device and an ammonia absorption tower which are connected in sequence; the deamination device is respectively connected with the flocculation sedimentation tank and the biochemical treatment unit.
In the above landfill leachate treatment system, the electrolytic Fenton reactor in the composite bed comprises a first reaction chamber, a second reaction chamber and a third reaction chamber which are arranged in sequence, and air inlet pipes are arranged at the inner bottoms of the first reaction chamber, the second reaction chamber and the third reaction chamber.
An anode plate is arranged at the lower part of the first reaction chamber along the horizontal direction, a porous insulation plate is arranged on the anode plate, a cathode plate is arranged in the first reaction chamber at the upper side of the porous insulation plate along the vertical direction, and the anode plate and the cathode plate are respectively connected with the anode and the cathode of a double-pulse direct current power supply; the first reaction chamber at the upper end of the porous insulating plate is filled with a filler layer.
The water inlet pipe is communicated and connected to the side wall of the first reaction chamber on the lower side of the anode plate, the upper parts of the first reaction chamber and the second reaction chamber are communicated with each other, the lower parts of the second reaction chamber and the third reaction chamber are communicated with each other, and the landfill leachate in the first reaction chamber enters the second reaction chamber from the upper part and then enters the third reaction chamber from the lower part of the second reaction chamber; an effluent weir which is communicated and connected with the flocculation sedimentation tank is arranged at the upper part of the third reaction chamber.
An exhaust port is arranged at the top of the first reaction chamber and connected with a gas collection and treatment module, a gas outlet of the gas collection and treatment module is connected with a hydrogen conveying pipe, and the free end of the hydrogen conveying pipe is positioned at the lower part in the second reaction chamber; an ORP meter and a hydrogen peroxide addition device are provided in the third reaction chamber.
The gas collecting and processing module is composed of a carbon dioxide remover and a hydrogen storage device which are sequentially arranged along the gas flowing direction.
In the above landfill leachate treatment system, the deamination device comprises a primary deamination tower, a secondary deamination tower, an intermediate water tank and a water pump; the intermediate water tank and the water pump are sequentially arranged on a pipeline between the liquid outlet of the primary deamination tower and the liquid inlet of the secondary deamination tower along the liquid flowing direction; the liquid outlet pipeline of the secondary deamination tower is connected with the biochemical treatment unit.
The upper near end parts of the first-stage deamination tower and the second-stage deamination tower are connected with an ammonia absorption tower through ammonia collecting pipes.
In the landfill leachate treatment system, the biochemical treatment unit consists of a reverse regulation tank, a UBF reactor, a secondary composite filler aerobic contact oxidation tank and a secondary sedimentation tank which are sequentially communicated and connected along the forward direction of the landfill leachate.
In the above landfill leachate treatment system, a pipeline at an air outlet at the top of the UBF reactor is connected with a biogas recycling unit, and the biogas recycling unit consists of a dehydrator, a desulfurizing tower, an air storage tank, a biogas boiler and a heat exchanger which are sequentially connected in a conducting manner through pipelines along the flowing direction of biogas; the heat exchanger is arranged on a pipeline between the liquid outlet of the flocculation sedimentation tank and the liquid inlet of the primary deamination tower; the biogas boiler is respectively connected with the heat exchanger and the constant temperature controller on the UBF reactor through pipelines.
In the landfill leachate treatment system, the advanced treatment unit consists of a sand filter, an activated carbon filter column, an ion exchange device and a disinfection tank which are sequentially communicated and connected through a pipeline along the liquid flowing direction; a water pump is arranged on the pipeline between the sand filter and the active carbon filter column.
The utility model adopts the above structure after, compared with the prior art, have following advantage:
(1) the utility model discloses handle high concentration landfill leachate, go out water quality of water and reach "domestic waste landfill pollution control standard" emission standard to energy utilization and chemical fertilizer recovery have been realized. Effectively reduces the energy consumption and realizes the effect of resource recovery. The utility model discloses a redox technology, remove ammonia recycle and handle the landfill leachate that high concentration is difficult to handle.
(2) The oxidation-reduction adopts a composite bed internal electrolysis Fenton reactor, passes through a porous insulating plate from bottom to top, then enters the filler of the first reaction chamber for electrolysis and internal electrolysis, and simultaneously, air enters from an air inlet and goes up along with water flow, so that the air not only plays a role of stirring and uniformly mixing, but also participates in electrolysis and internal electrolysis reaction in the process, and the reaction process is acceleratedAfter finishing the reaction, the reaction product enters a second reaction chamber to carry out Fenton reaction, and the residual ferrous ions in the first reaction chamber are additionally added with H2O2The Fenton reaction is carried out, the wastewater enters a water outlet of a water collecting tank after the reaction and is discharged, in the process, under the multiple actions of electrolysis, internal electrolysis, electric flocculation, electrooxidation, reduction reaction and Fenton reaction, electrode redox reaction and free radical oxidation reaction occur, the multiple composite actions complement each other, toxic and harmful substances are destroyed and degraded, and pollutants such as COD, chromaticity and the like are effectively removed. The power supply of the reactor adopts a bidirectional pulse direct current power supply, the pulse direct current can prevent the surface of the anode from generating a complete oxidation film, the reversing current realizes the periodic automatic reversing of the cathode and the anode, so that the oxidation reaction and the reduction reaction are alternately carried out, the passivation film generated by the oxidation reaction is effectively eliminated, and the reaction activity is restored again. And the residual iron ions in the first reaction chamber are used as the catalyst of the third reaction chamber, the reaction pH value conditions of the two chambers are the same, and H is additionally added under the condition of controlling ORP value2O2Carry out the fenton reaction and saved the medicament and used, the hydrogen that first reaction chamber produced gets into hydrogen recovery unit reuse. Compared with the multi-stage flocculation precipitation of the vein breaking, the multi-stage air flotation of the vein breaking saves a large amount of medicament usage.
(3) Removing ammonia and recycling: the ammonia nitrogen is transferred from liquid phase to gas phase by adopting a fine dispersion bipolar reverse ammonia-removing tower ammonia absorption tower, and the waste liquid is properly dispersed, so that the power consumption is reduced. Meanwhile, the treatment efficiency is improved, and ammonia nitrogen is absorbed through the circulating ammonia absorption tower, so that the treatment can not pollute the air, and the nitrogen fertilizer can be used as the nitrogen fertilizer. According to the ratio of the carbon source to the nitrogen source of a biochemical system, the biochemical performance of the leachate of the domestic garbage is a main denitrification path under the condition of insufficient carbon source in the deamination treatment process. By adopting the process of the utility model, 1kg of ammonia nitrogen can recover 7.65kg of fertilizer.
(4) The biogas is recycled, and the biogas just generated by the UBF reactor is a mixed gas containing saturated steam, and contains combustible gas methane and inert gas CO2 as well as hydrogen sulfide, wherein the hydrogen sulfide is toxic and highly corrosive. The process utilizes electrolysis treatment in a composite bed to remove most sulfides. The biogas desulfurization adopts biological desulfurization, and has the advantages of no need of catalyst, no need of chemical sludge treatment, little biological sludge generation, low energy consumption and high removal efficiency. The gas storage cabinet is arranged to realize the imbalance adjustment of the methane generation rate. Biogas is used as energy to enter a gas boiler to be converted into heat energy, a heat exchanger is used for heating the percolate, the temperature of the percolate is increased, the ammonia removal efficiency is improved, the UBF and a subsequent biochemical system are kept warm, proper temperature is maintained in winter, power consumption is reduced, the biochemical efficiency is improved, and the operating cost is reduced. 1kgCODcr can produce 0.5 cubic methane.
Drawings
The present invention will be described in further detail with reference to the following examples, which are not intended to limit the invention.
Fig. 1 is a schematic structural diagram of the present invention;
fig. 2 is a schematic structural diagram of the electrolytic fenton reactor in the composite bed of the present invention.
In the figure: 1. a pre-processing unit; 2. an ammonia removal unit; 3. a biochemical treatment unit; 3a, a reverse regulation pool; 3b, a UBF reactor; 3c, a secondary composite filler aerobic contact oxidation tank; 3d, a secondary sedimentation tank; 4. a depth processing unit; 4a, a sand filter; 4b, an active carbon filter column; 4c, an ion exchange device; 4d, a disinfection tank; 5. an electrolytic Fenton reactor in the composite bed; 5a, a first reaction chamber; 5b, a second reaction chamber; 5c, a third reaction chamber; 5d, an air inlet pipe; 5e, an anode plate; 5f, a porous insulating plate; 5g, a cathode plate; 5h, a double-pulse direct-current power supply; 5i, a filler layer; 5j, an effluent weir; 5k, an exhaust port; 5l, a gas collecting and processing module; 5m, a hydrogen conveying pipe; 5n, an ORP measuring instrument; 5o, a hydrogen peroxide adding device; 5p, a carbon dioxide remover; 5q, a hydrogen storage device; 6. a flocculation sedimentation tank; 7. a water inlet pipe; 8. a deamination device; 8a, a first-stage deamination tower; 8b, a secondary deamination tower; 8c, an intermediate water tank; 8d, a water pump; 8e, an ammonia gas collecting pipe; 9. an ammonia absorption tower; 10. a methane recycling unit; 10a, a dehydrator; 10b, a desulfurizing tower; 10c, an air storage tank; 10d, a biogas boiler; 10e, a heat exchanger.
Detailed Description
Referring to fig. 1 and 2, the present invention provides a landfill leachate treatment system, which comprises a pretreatment unit 1, an ammonia removal unit 2, a biochemical treatment unit 3 and a deep treatment unit 4 connected according to the sequence.
The pretreatment unit 1 consists of an electrolytic Fenton reactor 5 and a flocculation sedimentation tank 6 which are connected in sequence, and the landfill leachate enters the electrolytic Fenton reactor 5 in the composite bed through a water inlet pipe 7.
The ammonia removal unit 2 consists of a deamination device 8 and an ammonia absorption tower 9 which are connected in sequence; the deamination device 8 is respectively connected with the flocculation sedimentation tank 6 and the biochemical treatment unit 3.
Specifically, the electrolytic fenton reactor 5 in the composite bed includes a first reaction chamber 5a, a second reaction chamber 5b and a third reaction chamber 5c, which are sequentially arranged, and air inlet pipes 5d are respectively arranged at the bottom of the first reaction chamber 5a, the second reaction chamber 5b and the third reaction chamber 5 c. Preferably, the reactor is provided with a solar infrared lamp near the air inlet end of the air inlet pipe, and the solar infrared lamp is turned on in winter, so that the air blown into the reactor is hot air to accelerate the reaction rate.
An anode plate 5e is arranged at the lower part of the first reaction chamber 5a along the horizontal direction, a porous insulating plate 5f is arranged on the anode plate 5e, a cathode plate 5g is arranged in the first reaction chamber 5a at the upper side of the porous insulating plate 5f along the vertical direction, and the anode plate 5e and the cathode plate 5g are respectively connected with the anode and the cathode of a double-pulse direct-current power supply 5 h; the first reaction chamber 5a at the upper end of the porous insulating plate 5f is filled with a packing layer 5 i.
The water inlet pipe 7 is connected on the side wall of the first reaction chamber 5a at the lower side of the anode plate 5e in a conduction way, the upper parts of the first reaction chamber 5a and the second reaction chamber 5b are communicated with each other, the lower parts of the second reaction chamber 5b and the third reaction chamber 5c are communicated with each other, and the landfill leachate in the first reaction chamber 5a enters the second reaction chamber 5b from the upper part and then enters the third reaction chamber 5c from the lower part of the second reaction chamber 5 b; an effluent weir 5j which is communicated and connected with the flocculation sedimentation tank 6 is arranged at the upper part of the third reaction chamber 5 c.
An exhaust port 5k is formed in the top of the first reaction chamber 5a, the exhaust port 5k is connected with a gas collection processing module 5l, a gas outlet of the gas collection processing module 5l is connected with a hydrogen conveying pipe 5m, and the free end of the hydrogen conveying pipe 5m is located at the lower portion in the second reaction chamber 5 b; the third reaction chamber 5c is provided with an ORP measuring instrument 5n and a hydrogen peroxide adding device 5 o.
The gas collection processing module 5l is composed of a carbon dioxide remover 5p and a hydrogen storage 5q which are arranged in sequence along the gas flow direction.
In this embodiment, the deamination device 8 is composed of a primary deamination tower 8a, a secondary deamination tower 8b, an intermediate water tank 8c and a water pump 8 d; the middle water tank 8c and the water pump 8d are sequentially arranged on a pipeline between a liquid outlet of the first-stage deamination tower 8a and a liquid inlet of the second-stage deamination tower 8b along the liquid flowing direction; the liquid outlet pipeline of the second-stage deamination tower 8b is connected with the biochemical treatment unit 3. The upper near end parts of the first-stage deamination tower 8a and the second-stage deamination tower 8b are connected with an ammonia absorption tower 9 through an ammonia collecting pipe 8 e.
Preferably, the biochemical treatment unit 3 consists of a reverse regulation tank 3a, a UBF reactor 3b, a secondary composite filler aerobic contact oxidation tank 3c and a secondary sedimentation tank 3d which are sequentially communicated and connected along the forward direction of the landfill leachate.
Preferably, the advanced treatment unit 4 consists of a sand filter 4a, an activated carbon filter column 4b, an ion exchange device 4c and a disinfection tank 4d which are sequentially communicated and connected through pipelines along the flowing direction of liquid; a water pump is arranged on the pipeline between the sand filter 4a and the active carbon filter column 4 b.
Further, the purposes of improving the resource utilization rate and realizing energy conservation and emission reduction are achieved. A pipeline of an air outlet at the top of the UBF reactor 3b is connected with a biogas recycling unit 10, and the biogas recycling unit 10 consists of a dehydrator 10a, a desulfurizing tower 10b, a gas storage tank 10c, a biogas boiler 10d and a heat exchanger 10e which are sequentially communicated and connected through pipelines along the flowing direction of biogas; the heat exchanger 10e is arranged on a pipeline between the liquid outlet of the flocculation sedimentation tank 6 and the liquid inlet of the primary deamination tower 8 a; the biogas boiler 10d is respectively connected with the heat exchanger 10e and the thermostatic controller on the UBF reactor 3b through pipelines.
The marsh gas containing saturated vapor output from the UBF reactor is purified by desulfurization and gas-water separation in an integrated gas storage cabinet. The biogas desulfurization adopts a biological desulfurization method, and colorless sulfur bacteria, such as thiobacillus thiooxidans, thiobacillus ferrooxidans and the like are utilized to oxidize sulfides into elemental sulfur under the condition of micro-oxygen. The purified methane is used as energy and is converted into heat energy through combustion of a gas boiler, the heat energy is transmitted to a deamination heat exchanger to heat percolate so as to reach the appropriate temperature for removing ammonia in a deamination tower, and the heat energy is transmitted to a biochemical system to keep the temperature of the biochemical system at 27-35 ℃ through control of a temperature controller.
A landfill leachate treatment method adopting the system comprises the following steps:
(1) the landfill leachate is pressurized from a water inlet pipe through a pump, added with acid through a pipeline mixer to adjust the pH value to 3-4, enters an electrolytic Fenton reactor in a composite bed, passes through a porous insulating plate from bottom to top, enters a filler of a first reaction chamber to perform electrolysis and internal electrolysis reaction for 20-60 min, and simultaneously enters air through an air inlet pipe and goes up along with water flow, so that the air not only plays a role of stirring and uniformly mixing, but also participates in the electrolysis and internal electrolysis reaction to accelerate the reaction process, enters a second reaction chamber after the reaction is completed, and the second reaction chamber utilizes new ecological H generated by the first reaction chamber2Reducing part of pollutants in the percolate for 15-30 min;
after the reaction in the second reaction chamber, the reaction solution enters a third reaction chamber to carry out Fenton reaction, and the Fenton reaction utilizes the ferrous ions left after the reaction in the first reaction chamber to control H through an ORP (oxidation-reduction potential) measuring instrument2O2The addition amount is that the oxidation-reduction potential of the landfill leachate is controlled within the range of 250-300mv, the reaction time is 1-3h, and the landfill leachate enters an effluent weir after reaction and is discharged to a flocculation sedimentation tank. In the process, under the multiple actions of electrolysis, internal electrolysis, electric flocculation, electrooxidation, reduction reaction and Fenton reaction, the wastewater generates electrode redox reaction and free radical oxidation reaction, nascent hydrogen reduction reaction and multiple composite actions complement each other, poisonous and harmful substances are destroyed and degraded, and COD and chromaticity are effectively degraded.
The power supply of the reactor adopts a bidirectional pulse direct current power supply, and the pulse direct current power supplyThe current can prevent the anode surface from generating a complete oxidation film, and the reversing current realizes the periodic automatic reversing of the cathode and the anode, so that the oxidation reaction and the reduction reaction are alternately carried out, the passivation film generated by the oxidation reaction is effectively eliminated, and the reaction activity is restored again. And the nascent state H2 of the electrolytic reaction in the composite bed is used as a reducing agent of a second reaction chamber, the residual iron ions in the first reaction chamber are used as a catalyst of a third reaction chamber, the reaction pH value conditions of the first reaction chamber and the third reaction chamber are the same, and H is controlled by an ORP (oxidation-reduction potential) meter2O2The addition amount is controlled to be within the range of 250-300mv of the oxidation-reduction potential of the landfill leachate. This reaction saves on the use of pharmaceutical agents. The basic reaction is as follows:
the first reaction chamber basically reacts:
Fe+H2SO4→FeSO4+H2↓ (generating new ecological hydrogen gas entering the second reaction chamber)
H++2e-→H2↑
Fe→Fe2++2e-
H2O→.OH+H++e-
O2+2H++2e-→H2O2
H2O2+Fe2+→Fe3++.OH+OH-
Fe3++e-→Fe2+
Fe3++H2O2→Fe2++HO2 .+H+
RH+.OH→…→CO2+H2O
The second reaction chamber basically reacts:
The third reaction chamber basically reacts:
Fe2++H2O2→Fe3++.OH+OH-(Fe2+from the first reaction chamber)
Fe2++.OH→Fe3++OH-
Fe3++H2O2→Fe2++HO2 .+H+
HO2 .+H2O2→O2+H2O+.OH
RH+.OH→…→CO2+H2O
(2) The landfill leachate entering the flocculation sedimentation tank is firstly adjusted to the pH value of 10.5-11, then iron ions generated by an electrolytic Fenton reactor in a composite bed are used as a flocculating agent, and a coagulant aid is added to remove most harmful substances including sulfide, so that the chromaticity of the wastewater is improved, and the use of medicaments is saved. The coagulant aid is preferably PAM (polyacrylamide) solution with the concentration of 0.5 percent, and the addition amount of the coagulant aid is 4 to 6 liters per ton of landfill leachate.
(3) The garbage percolate from the flocculation sedimentation tank enters a deamination device for deamination, and the deaminated garbage percolate sequentially passes through a biochemical treatment unit and an advanced treatment unit and then is discharged; and ammonia-containing waste gas generated in the deamination device enters an ammonia absorption tower to be absorbed and finally converted into chemical fertilizer to be recovered. When the landfill leachate flows through the biochemical treatment unit, the landfill leachate firstly enters a reverse regulation tank, acid is added to regulate the pH value to be neutral, and then the landfill leachate enters a subsequent biochemical treatment process. The whole biochemical treatment process adopts a mode of UBF high-efficiency anaerobic reaction combined with aerobic contact oxidation reaction. The leachate after biochemical treatment enters a filter column firstly to remove part of suspended particles, then enters an ion exchange deamination for further ammonia removal, and an ion exchange regeneration liquid is circulated to an ammonia absorption tower to recover and prepare the nitrogen fertilizer.
Specifically, the deamination device specifically deaminates: the landfill leachate firstly enters a heat exchanger, and is heated by the heat exchanger under the action of a temperature controller, the heat exchanger uses methane generated by anaerobic as energy for heating, and the temperature of the landfill leachate is increased to 32-38 ℃ by a temperature sensor; the heated landfill leachate sequentially enters a primary deamination tower, an intermediate water tank and a secondary deamination tower, the gas-liquid ratio in the tower is controlled between 3000-3800, the pressure of a spray head is 2.5-2.8 Mpa, and the particle size of water drops is as follows: 3mm-4mm, and controlling the pH value of the percolate at 10-11; the ammonia stripping rate is more than 90 percent. After the leachate is blown off by ammonia, a large amount of free ammonia is removed, and part of COD is also removed, thereby being beneficial to the subsequent biochemical treatment. In the process, in order to select proper nozzle pressure to be matched with parameters of water drop particle size and temperature, research and development personnel repeatedly perform experiments to finally obtain the parameters under the condition of determining the nozzle pressure through creative labor. During testing, the optimal pressure of the spray head is selected, then the particle size and the temperature of water drops are changed continuously, the ammonia nitrogen removal rate is increased continuously along with the continuous increase of the temperature, and when the temperature reaches about 35 ℃, the removal rate changes gently and changes less and less. Meanwhile, the removal rate of different water drop particle sizes is very obviously different. As a person skilled in the art, it is generally considered that the smaller the diameter of the water drop, the better the ammonia nitrogen removal effect, but experiments show that this is not the case, and when the diameter of the water drop is 3-4mm, the best effect is achieved, and the diameter reaches more than 90%.
The ammonia recovery of the ammonia absorption tower comprises the following specific steps: the ammonia absorption tower absorbs ammonia by adopting a sulfuric acid absorbent, the pressure of a spray head of an absorbent spray pump is 1.5-2.5 Mpa, and the particle size of water drops is as follows: 1.8mm-3mm, and the gas flow velocity in the tower is 2-3m/S. By adopting the process, tests show that about 7.65kg of fertilizer can be recovered from 1kg of ammonia nitrogen. In the field, it is generally believed that the smaller the particle size of the water droplets, the better the atomization effect, and the better the fertilizer recovery effect. However, experiments show that the fertilizer recovery rate is best when the particle size of water drops is in the range of 1.8-3 mm. The fertilizer recovery rate is in a parabolic shape along with the continuous increase of the particle size of water drops, and is not gradually increased or decreased.
Meanwhile, the biochemical treatment unit comprises a UBF reactor, a large amount of methane gas is generated through reaction and decomposition, the methane gas is recycled through the methane recycling unit, and the methane serving as fuel is converted into heat energy by a methane combustion device in the methane recycling unit.
A heat exchanger is arranged on a pipeline between the flocculation sedimentation tank and the deamination device, heat energy generated by the biogas combustion device is respectively sent into the heat exchanger and a constant temperature controller on the UBF reactor, the temperature of the landfill leachate entering the deamination device is increased to 32-38 ℃ by matching a temperature sensor with the heat exchanger, and the temperature of the landfill leachate in the biochemical treatment unit is kept constant to 27-35 ℃ by matching the constant temperature controller with the heat energy generated by the biogas combustion device. In the biochemical treatment process, the conventional temperature value in the field is between 15 and 25 ℃, but experiments show that the ammonia nitrogen removal rate fluctuates greatly, and technicians perform a large amount of long-term experimental tests for determining the optimal temperature of the landfill leachate in the biochemical treatment unit to achieve the optimal removal rate. According to a large amount of statistical data, the ammonia nitrogen removal rate is gradually increased when the temperature is increased from 3 ℃ to 17 ℃. However, the reason why the removal rate is decreased and then increased at 17 ℃ to about 19 ℃ is not described in detail. Then when the temperature is increased to about 27 ℃ at 19 ℃, the removal rate also has the trend of wavy lines and overall increasing, and when the temperature is 32 ℃, the removal rate reaches the peak value and tends to be smooth. From this, it is understood that the relationship between the temperature and the removal rate is not regularly and linearly changed, and has a certain irregularity.
Meanwhile, in the experimental process, COD is detected simultaneouslycrAnd BOD removal rate and temperature. When the temperature is increased from 3 ℃ to about 9 ℃, the COD iscrThe removal rate of the wastewater is not greatly changed from BOD removal rate and is similar to that of BOD removal rate, and when the temperature is increased from 9 ℃ to about 14 ℃, COD is generatedcrAnd BOD removal rate sharply rise and both values are almost the same. However, from 14 ℃ to about 16 ℃, the COD iscrThe removal rate continues to increase but the BOD removal rate decreases. Then the removal rates of the two indexes gradually rise from about 16 ℃ to 27 ℃, and after 27 ℃, the removal rate values of the two indexes reach peak values and tend to be stable.
Through the two experiments described above, the final choice was to thermostatize the landfill leachate temperature in the biochemical treatment unit to 27-35 ℃. The UBF reactor takes activated carbon granules and combined packing in the device as a fluidizing carrier. The sewage is used as a flowing medium, anaerobic microorganisms are bonded on the surfaces of the activated carbon and the combined filler in a biofilm mode, the activated carbon has an adsorption effect in the middle stage of biochemical treatment to accelerate the biochemical process, and methane gas generated in the circulating pump/sewage treatment process is automatically mixed to enable the sewage to be in a flowing state. When the sewage flows through the bed body in an up-flow mode, the sewage is continuously contacted and reacted with the carrier attached with the anaerobic biomembrane on the bed body, and the purposes of anaerobic reaction decomposition and organic matter adsorption in the sewage are achieved.
The filler adopted by the biochemical system can be a combined filler and a soft filler which are conventional in the field, and can also be other fillers with better disclosed performance, for example, an active composite suspension filler disclosed by patent No. 2012100405988 (publication No. CN 102583719B; publication No. 2014.04.09) is adopted, the filler creatively bonds the surface layer of the activated carbon to the porous high-viscosity layer, has a surface area which is incomparable with other fillers, and has unique adsorbability and an active function, so that the biofilm culturing efficiency is greatly improved, and the biological culturing time is shortened. Meanwhile, the floating support is used for the filler, so that the filler is convenient to install, can be replaced and maintained without production stop, and enhances the contact effect of the filler on the water body in advance.
In the process of decomposing organic matters by anaerobic microorganisms in the UBF reactor, a large amount of methane, carbon dioxide and other gases can be generated, wherein the methane accounts for 75-85%, and 1kg of CODcr can generate 0.5 cubic methane. The biogas generated by the unit enters a biogas recycling device, the biogas is used as energy to be burnt and converted into heat energy to heat wastewater to realize heat preservation of a biochemical system, the temperature is increased by 10 ℃ in a proper temperature range, microorganisms can grow 1 time faster, the removal rate of organic matters is further increased, the viscosity of feed liquid is reduced due to the temperature increase, the contact chance of the microorganisms and the organic matters is further increased, the biological treatment process can be promoted under the condition that the temperature is properly increased, the removal of COD and BOD is facilitated, the removal rate of COD and BOD is increased by 15% from low temperature heating to medium temperature, the removal rate of ammonia nitrogen can be increased by about 4 times, and methane bacteria can be promoted to generate more methane gas under a higher temperature environment. Therefore, the biogas recycling unit is added, so that the purposes of energy conservation and environmental protection are realized, and the treatment effect of the landfill leachate can be obviously improved.
Experimental example 1
In order to test the remarkable effect brought by the original structure of the electrolytic Fenton reactor in the composite bed, an experimenter adopts a mode of fully opening the first reaction chamber, the second reaction chamber and the third reaction chamber and partially separating the reaction chambers to test.
The first, second and third chambers of the electrolytic Fenton reactor in the composite bed are all started, and the pretreatment removal rate reaches the best COD (chemical oxygen demand) effectcrThe removal rate reaches 85 percent, the chroma removal rate reaches 96 percent, and NH is added3the-N removal rate reaches 58%.
The electrolytic Fenton reactor in the composite bed is only started in the first chamber and the second chamber, the third chamber is not started, the removal rate of the pretreatment chroma is slightly reduced, the chroma removal rate is about 92 percent, and the COD iscr、NH3the-N removal rate is relatively obviously reduced compared with the three-chamber full start-up. CODcrRemoval rate of 68% NH3-N removal 37%.
The first chamber of the electrolytic Fenton reactor in the composite bed is not started, the second chamber and the third chamber are started, and COD is pretreatedcr、NH3N, the chroma removal rate is obviously reduced.
Starting the electrolytic Fenton reactor in the composite bed for one or three chambers, not starting the second chamber, and pretreating CODcr、NH3N, the chroma is reduced compared with the total start-up removal rate, and the chroma removal rate is obviously reduced.
The present invention will be described in further detail with reference to specific examples.
Example one: the leachate of a refuse landfill in a certain market is subjected to pilot plant test, and the landfill leachate is dark brown, has the chroma of 2582 and the COD of 6877mg/L and BOD52200mg/L, ammonia nitrogen: 1673.2mg/L and SS 580mg/L, and the process is adopted to carry out pilot test on the product.
The method comprises the following specific steps: the landfill leachate is pressurized from a water inlet pipe through a pump, the pH value of the landfill leachate is adjusted to 3-4 through a pipeline mixer, then the landfill leachate enters the electrolytic Fenton reactor in the composite bed, and the third reaction chamber controls H through an ORP (oxidation-reduction potential) tester2O2The addition amount is that the oxidation-reduction potential of the landfill leachate is controlled within the range of 250-300mv, the pH of the effluent is firstly adjusted back to 10.5 and then enters the flocculation precipitation, the effluent enters the fine dispersion bipolar reverse ammonia absorption and deamination tower, the gas-liquid ratio is controlled at 3000-3800, and the flow rate in the tower is controlled at 2.5-3 m/S.
The gas removed by the deamination and deamination tower enters an ammonia absorption tower, and the flow rate in the tower is controlled to be 2-3m/S. Adding acid into the deaminated percolate to adjust the pH value to be neutral and then entering a subsequent biochemical system, wherein the biochemical system adopts UBF high-efficiency anaerobic and aerobic contact oxidation, the filler of the biochemical system adopts novel active composite filler, the biochemical system keeps the temperature constant to 27-35 ℃ through a constant temperature device, and the UBF ascending flow rate is controlled as follows: 0.9-1.1m/h, volume load 7kgC0D/m3D; the ratio of the aerobic contact oxidation gas to the aerobic contact oxidation gas is controlled to be 20: 1. Biogas generated by UBF efficient anaerobic reaction enters a biogas recycling device, the purified biogas is reused as energy for a heater to heat effluent water after reaction of a biochemical system, the effluent water enters an ion exchange system to further remove ammonia, and then the effluent water enters a disinfection tank for disinfection.
The process is completely started, then the residence time of the electrolytic Fenton reactor in the composite combined bed is controlled to be 2.5h, the temperature of the fine dispersion bipolar reverse ammonia absorption tower is controlled to be 35 ℃, the pressure of a spray head is controlled to be 2.5-2.8 Mpa, and the particle size of water drops is as follows: 3mm-4 mm. The ammonia absorption tower adopts sulfuric acid as an absorbent, and the pressure of a pump head of an absorbent spray pump is as follows: 1.5MPa-2.5MPa, the water drop particle diameter is as follows: 1.5mm-2 mm. The leachate after reaction enters a subsequent treatment system, and the effluent quality is superior to the first-level emission standard of the pollution control standard for landfill of domestic garbage (GB 16889-1997).
Example two: the daily treatment capacity of the landfill leachate in a certain landfill in the autonomous county of the Changyang soil family is 100t, the landfill leachate is dark brown, the chroma is between 2000 and 4000, the CODcr is 4000 and 7000mg/L, and the BOD is BOD53000-5000mg/L, ammonia nitrogen: 1200-1800mg/L, and SS-500-800 mg/L.
By adopting the process, the quality of the effluent water is kept stable since the system is operated, and the quality of the treated water is superior to the first-level emission standard of the domestic garbage landfill pollution control standard (GB 16889-1997).
The landfill leachate is pressurized from a water inlet pipe through a pump, the pH value of the landfill leachate is adjusted to 3-4 through a pipeline mixer, then the landfill leachate enters an electrolytic Fenton reactor in a composite bed to be subjected to oxidation reduction treatment for 2.5 hours, and the pH value is controlled to 3-4.
The second reaction chamber utilizes the new ecological H generated by the first reaction chamber2The leachate which is used as a reducing agent for reduction reaction enters a third reaction chamber after being reacted in the second reaction chamber, and H is controlled by an ORP (oxidation-reduction potential) measuring instrument in the third reaction chamber2O2The adding amount is that the oxidation-reduction potential of the landfill leachate is controlled within the range of 250-300mv, the pH of the effluent leachate is firstly adjusted back to 10.5 and then enters flocculation precipitation, the residual iron ions in the electrolytic Fenton reactor in the composite bed are used as a flocculating agent and added into a coagulant aid for reaction, and the reaction time is 1h, so that the small particles which are difficult to precipitate are converted into large particles which are easy to precipitate and then enter an inclined plate precipitation tank for residence time of 2 h.
The leachate after flocculation precipitation enters pH adjustment, alkali is added to control the pH to be 10.5, then the leachate is heated to 35 ℃ through a heat exchanger under the control of a temperature controller and enters a deamination tower, the deamination tower adopts bipolar reverse series operation to improve the removal rate of ammonia, the gas-liquid ratio of ammonia stripping is controlled between 3000 and 3800, the flow rate in the tower is controlled to be 2.5-3m/S, the pressure of a spray nozzle is 2.5-2.8 MPa, and the particle size of water drops is 3-4 mm.
The generated waste gas enters an ammonia absorption tower, sulfuric acid is used as an absorbent of the absorbent, the head of an absorbent spray pump is 1.5-2.5 Mpa, and the particle size of water drops is as follows: 1.8mm-3 mm; the gas flow velocity in the tower is 2-3m/S, and 6.12-7.65kg of fertilizer can be recovered by 1kg of ammonia nitrogen through the sulfuric acid absorption liquid as fertilizer.
And (3) metering the pretreated percolate into a pH adjusting tank to adjust the pH back to neutral, allowing the percolate to enter a high-efficiency anaerobic UBF reactor, reacting through the UBF reactor to achieve anaerobic decomposition, adsorbing organic matters in the sewage and effectively degrading toxic substances. The ascending flow rate is as follows: 0.9-1.1m/h, volume load 7kgC0D/m3·d。
Biogas generated by the high-efficiency anaerobic reaction enters a biogas recycling device, and the purified biogas is reused as a heater to be heated as energy. 1kgCODcrCan generate 0.5kg of methane. The leachate after the reaction of the high-efficiency anaerobic reactor enters a subsequent secondary aerobic biochemical treatment systemThe ratio of gas to water is 20: 1. The temperature of the biochemical system is heated to 27-35 ℃ by a heating device. The leachate wastewater after biochemical treatment enters an ion exchange system for further ammonia removal, and then the effluent enters a disinfection tank for disinfection and is discharged after reaching the standard.
The effluent is superior to the first-level emission standard of the pollution control standard for landfill of domestic garbage (GB 16889-1997).
The oxidation reduction process adopts a composite bed internal electrolysis Fenton reactor, overcomes the defect of reduced treatment effect caused by hardening in the traditional internal electrolysis, and uses the new ecological H generated by the first reaction chamber in the second reaction chamber2The third reaction chamber is used as a reducing agent for reduction reaction, and the iron ions left in the reaction of the first reaction chamber are used as a catalyst, so that the existing resources are fully utilized, the treatment cost is reduced, and the treatment effect is improved.
The process utilizes iron ions generated by an electrolytic Fenton reactor in the composite bed as a flocculating agent for flocculation and precipitation, thereby saving the cost of the medicament. The UBF and aerobic biochemical treatment system filler adopts novel active composite filler, the filler creatively bonds the surface layer of the active carbon to the porous high-viscosity layer, has incomparable surface area, unique adsorbability and active function of other fillers, greatly improves the film hanging efficiency, and shortens the biological culture time. Meanwhile, the floating support is used for the filler, so that the filler is convenient to install, production is not stopped, replacement and maintenance are carried out in actual operation, the contact effect of the filler and a water body is enhanced, and the oxygen utilization rate and the treatment rate are improved.
Hydrogen recycle, marsh gas recycle have saved the energy, have ensured the low risk of biochemical system treatment effect because of winter is cold simultaneously. The ammonia removal and recovery realize the resource utilization.
The above-mentioned embodiments are only for convenience of description, and are not intended to limit the present invention in any way, and those skilled in the art will understand that the technical features of the present invention can be modified or changed by other equivalent embodiments without departing from the scope of the present invention.
Claims (7)
1. A landfill leachate treatment system is characterized by comprising a pretreatment unit (1), an ammonia removal unit (2), a biochemical treatment unit (3) and a deep treatment unit (4) which are connected in sequence;
the pretreatment unit (1) consists of an electrolytic Fenton reactor (5) and a flocculation sedimentation tank (6) which are connected in sequence, and the landfill leachate enters the electrolytic Fenton reactor (5) in the composite bed through a water inlet pipe (7);
the ammonia removal unit (2) consists of a deamination device (8) and an ammonia absorption tower (9) which are connected in sequence; the deamination device (8) is respectively connected with the flocculation sedimentation tank (6) and the biochemical treatment unit (3).
2. The landfill leachate treatment system according to claim 1, wherein the composite bed internal electrolysis Fenton reactor (5) comprises a first reaction chamber (5a), a second reaction chamber (5b) and a third reaction chamber (5c) which are arranged in sequence, and air inlet pipes (5d) are arranged at the bottom in the first reaction chamber (5a), the second reaction chamber (5b) and the third reaction chamber (5 c);
an anode plate (5e) is arranged at the lower part of the first reaction chamber (5a) along the horizontal direction, a porous insulating plate (5f) is arranged on the anode plate (5e), a cathode plate (5g) is arranged in the first reaction chamber (5a) at the upper side of the porous insulating plate (5f) along the vertical direction, and the anode plate (5e) and the cathode plate (5g) are respectively connected with the positive electrode and the negative electrode of a double-pulse direct-current power supply (5 h); a filler layer (5i) is filled in a first reaction chamber (5a) at the upper end of a porous insulating plate (5 f);
the water inlet pipe (7) is connected to the side wall of the first reaction chamber (5a) on the lower side of the anode plate (5e) in a conduction mode, the upper parts of the first reaction chamber (5a) and the second reaction chamber (5b) are communicated with each other, the lower parts of the second reaction chamber (5b) and the third reaction chamber (5c) are communicated with each other, and landfill leachate in the first reaction chamber (5a) enters the second reaction chamber (5b) from the upper part and then enters the third reaction chamber (5c) from the lower part of the second reaction chamber (5 b); an effluent weir (5j) which is communicated and connected with the flocculation sedimentation tank (6) is arranged at the upper part of the third reaction chamber (5 c);
an exhaust port (5k) is arranged at the top of the first reaction chamber (5a), the exhaust port (5k) is connected with a gas collection processing module (5l), a gas outlet of the gas collection processing module (5l) is connected with a hydrogen conveying pipe (5m), and the free end of the hydrogen conveying pipe (5m) is positioned at the inner lower part of the second reaction chamber (5 b); an ORP meter (5n) and a hydrogen peroxide addition device (5o) are provided in the third reaction chamber (5 c).
3. The landfill leachate treatment system according to claim 2, wherein the gas collection treatment module (5l) comprises a carbon dioxide remover (5p) and a hydrogen storage (5q) arranged in this order along the gas flow direction.
4. The landfill leachate treatment system of claim 1, wherein the deamination device (8) consists of a primary deamination tower (8a), a secondary deamination tower (8b), an intermediate water tank (8c) and a water pump (8 d); the middle water tank (8c) and the water pump (8d) are sequentially arranged on a pipeline between the liquid outlet of the first-stage deamination tower (8a) and the liquid inlet of the second-stage deamination tower (8b) along the liquid flowing direction; a liquid outlet pipeline of the secondary deamination tower (8b) is connected with the biochemical treatment unit (3);
the upper near end parts of the first-stage deamination tower (8a) and the second-stage deamination tower (8b) are connected with an ammonia absorption tower (9) through ammonia gas collecting pipes (8 e).
5. The landfill leachate treatment system according to claim 4, wherein the biochemical treatment unit (3) comprises a reverse regulation tank (3a), a UBF reactor (3b), a secondary composite filler aerobic contact oxidation tank (3c) and a secondary sedimentation tank (3d) which are sequentially connected in a conducting manner along the forward direction of the landfill leachate.
6. The landfill leachate treatment system according to claim 5, wherein a pipeline at the top gas outlet of the UBF reactor (3b) is connected with a biogas recycling unit (10), and the biogas recycling unit (10) comprises a dehydrator (10a), a desulfurizing tower (10b), a gas storage tank (10c), a biogas boiler (10d) and a heat exchanger (10e) which are sequentially connected in a conducting manner through pipelines along the flowing direction of biogas; the heat exchanger (10e) is arranged on a pipeline between the liquid outlet of the flocculation sedimentation tank (6) and the liquid inlet of the primary deamination tower (8 a); the biogas boiler (10d) is respectively connected with the heat exchanger (10e) and the thermostatic controller on the UBF reactor (3b) through pipelines.
7. The landfill leachate treatment system according to claim 1, wherein the advanced treatment unit (4) comprises a sand filter (4a), an activated carbon filter column (4b), an ion exchange device (4c) and a disinfection tank (4d) which are sequentially connected in a pipeline conduction manner along the liquid flow direction; a water pump is arranged on the pipeline between the sand filter (4a) and the active carbon filter column (4 b).
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