CN116119888A - Combined treatment system and treatment method for post-concentration liquid of landfill leachate membrane - Google Patents
Combined treatment system and treatment method for post-concentration liquid of landfill leachate membrane Download PDFInfo
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- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
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- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
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- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention provides a combined treatment system and a treatment method for post-concentrated solution of a landfill leachate membrane, wherein the combined treatment system for the post-concentrated solution of the landfill leachate membrane comprises a coagulating sedimentation tank, a PH regulating tank, a secondary coagulating sedimentation tank, an ozone advanced catalytic oxidation tank, a Fenton reaction tank, an electrocatalytic oxidation tank and a sludge concentration tank for receiving sludge discharged by the coagulating sedimentation tank, the PH regulating tank, the secondary coagulating sedimentation tank and the Fenton reaction tank. The combined treatment system has low investment and operation cost and good treatment effect, and can effectively reduce the concentration of organic matters and the content of other pollutants such as salt and the like in the concentrated solution, so that the landfill leachate membrane concentrated solution is treated and then discharged after reaching the standard.
Description
Technical Field
The invention belongs to the technical field of wastewater treatment, and particularly relates to a combined treatment system and a treatment method for post-concentration liquid of a landfill leachate membrane.
Background
The landfill leachate is high-concentration organic wastewater leachate which is formed by deducting saturated water holding capacity of garbage and a soil covering layer from water contained in garbage in a landfill site, rain and snow water and other water entering the landfill site and passing through the garbage layer and the soil covering layer, has the characteristics of complex components, high content of organic pollutants and ammonia nitrogen, high content of heavy metals, high chromaticity, high malodor, high COD (chemical oxygen demand) and BOD (biochemical oxygen demand) concentration and the like, and belongs to the field of water treatment and wastewater degradation with high difficulty.
The traditional advanced treatment mode of the landfill leachate is generally a combined technology of nanofiltration and reverse osmosis, but a large amount of membrane concentrate can be generated after the landfill leachate is subjected to advanced treatment by a nanofiltration and reverse osmosis system. The main components of the landfill leachate membrane concentrate are humus substances, undegraded organic matters remained in secondary treatment effluent, soluble Microorganism Products (SMP) and other substances, the COD of the concentrate is usually 5000mg/L, the ammonia nitrogen concentration is about 50-200 mg/L, and the conductivity is about 20000-50000 mu s/cm; the COD of the concentrated solution produced by the reverse osmosis process is generally above 1000mg/L, the total hardness is above 1500mg/L, and the conductivity is about 30000-50000 mu s/cm.
At present, the main methods for treating the membrane concentrated solution at home and abroad are as follows: back spraying, recharging, evaporating, advanced oxidation and incineration. The recharging landfill site can enrich organic pollutants in the landfill leachate, so that the treatment efficiency of the primary treatment process is reduced, the primary treatment process is finally crashed, and meanwhile, the recharging process is controlled by the country, so that the process of recharging the post-membrane concentrated solution of the landfill leachate to the landfill site has a trend of being abandoned; the evaporation process solves the defects caused by continuous reflux of the membrane concentrated solution, but the evaporation process has the problems of high cost, serious corrosion and scaling of the evaporator and easy secondary pollution; the membrane concentrate is directly incinerated, so that the total operation cost is very high.
Disclosure of Invention
In view of the above, the invention provides a combined treatment system and a combined treatment method for a landfill leachate membrane, which are low in investment and running cost, good in treatment effect, and capable of effectively reducing the concentration of organic matters and other pollutants such as salt in the landfill leachate membrane concentrate, so that the landfill leachate membrane concentrate can reach the discharge standard after being treated.
In order to achieve the above purpose, the technical scheme of the invention is realized as follows:
the invention provides a combined treatment system for a post-concentrated solution of a landfill leachate membrane, which comprises a coagulating sedimentation tank, a PH regulating tank, a secondary coagulating sedimentation tank, an ozone advanced catalytic oxidation tank, a Fenton reaction tank, an electrocatalytic oxidation tank and a sludge concentration tank, wherein the coagulating sedimentation tank, the PH regulating tank, the secondary coagulating sedimentation tank and the sludge concentration tank are sequentially connected.
The concentrated solution is subjected to coagulating sedimentation treatment in a coagulating sedimentation tank after a landfill leachate membrane, and the main purpose of the concentrated solution is to remove suspended particles, part of macromolecular organic matters and heavy metals in wastewater;
the PH adjusting tank is used for adjusting the PH of the water body, so that the PH of the water discharged from the PH adjusting tank is maintained at about 7;
the secondary coagulating sedimentation tank has the main functions of further removing fine particles generated in the PH adjusting process and residual sludge generated by the comprehensive coagulating sedimentation tank, and simultaneously strengthening and removing a part of organic pollutants and heavy metals;
the ozone advanced catalytic oxidation pond can further carry out oxidative decomposition on refractory organic matters to degrade residual COD, and has good removal effect on chromaticity and smell, so that the quality of effluent water is higher;
in the Fenton reaction tank, the organic pollutants which are difficult to degrade and contained in the effluent of the ozone advanced catalytic oxidation tank are removed through the reinforcement of hydroxyl radicals generated by Fenton;
the electrocatalytic oxidation pond is a treatment process for ensuring the effluent to reach the standard stably, the effluent of the front-end Fenton treatment process basically meets the discharge standard, and in order to ensure the wastewater to reach the standard stably and have certain shock resistance, the wastewater is subjected to electrochemical treatment by utilizing an electrochemical reactor consisting of a titanium dioxide polar plate group, so that the wastewater reaches the standard and is discharged;
the sludge in the sludge concentration tank is sent to a landfill site for harmless landfill after being dehydrated;
through coagulating sedimentation pretreatment, and based on a novel ozone advanced oxidation process, through combining a Fenton treatment process and a micro-electrolysis process, the standard discharge of the treated concentrated solution after the landfill leachate membrane can be realized.
In some preferred embodiments of the combined treatment system of the present invention, the coagulant added to the coagulating sedimentation tank is an iron salt coagulant (e.g., polymeric ferric sulfate, ferric trichloride); the coagulant added into the secondary coagulating sedimentation tank is a non-ferric salt coagulant.
In general, the post-membrane concentrate of the landfill leachate contains residual sludge after biochemical treatment, macromolecular organic pollutants difficult to biochemically degrade and the like; on one hand, suspended particles and macromolecular organic matters can be removed through coagulating sedimentation, so that the removal rate of organic pollutants in the subsequent ozone advanced oxidation process is further improved; on the other hand, fe contained in the iron salt coagulant 3+ The method can complex some macromolecular organic matters, change the molecular bond energy structure, promote the degradation of macromolecular organic pollutants by ozone, improve the ozone utilization rate and the removal efficiency of the macromolecular organic matters, and realize better synergistic effect of ozone and coagulating sedimentation; therefore, through the coagulating sedimentation effect of ferric salt, the method not only achieves the aim of removing a part of organic pollutants, but also provides a promoting effect for the ozone advanced catalytic oxidation reaction in the subsequent ozone advanced catalytic oxidation pond, and the connection of the two sections of processes greatly improves the organic pollutant removal efficiency of the concentrated solution after the garbage percolate film, and ensures that the treatment of the organic pollutants in the wastewater by the subsequent process reaches the standard;
the coagulant applicable to the secondary coagulating sedimentation tank is a coagulant (for example: PAC) without ferric salt, and the adding of excessive ferric salt coagulant is easy to influence the subsequent treatment process, and can cause yellowing of the effluent of the ozone advanced catalytic oxidation tank, so that the coagulant added in the secondary coagulating sedimentation tank is a non-ferric salt coagulant.
In some preferred embodiments of the combined treatment system of the present invention, the flocculant added to the coagulating sedimentation tank is PAM; the coagulant added into the secondary coagulating sedimentation tank is aluminum salt coagulant, and the flocculant added into the secondary coagulating sedimentation tank is PAM.
In some preferred embodiments of the combined treatment system of the present invention, the post-landfill leachate membrane concentrate has a COD concentration of 3500-5000 mg/L and a concentration of ammonia nitrogen to total nitrogen of no more than 150mg/L.
In some more preferred embodiments of the combined treatment system of the present invention, the coagulant in the coagulating sedimentation tank is added in an amount of 10 to 16g/L, and is added after being prepared into a solution; the flocculant is PAM flocculant, and is prepared into a solution with the mass concentration of 0.1%, and the adding amount is 2-6 ml.
After coagulating sedimentation of the concentrated solution after the membrane of the landfill leachate, the COD of the effluent is basically about 1500 mg/L.
In some more preferred embodiments of the combined treatment system of the present invention, the PH of the PH adjusting tank effluent is neutral.
As the iron salt is added into the coagulating sedimentation tank, the coagulating sedimentation water becomes acidic, and the pH value is regulated to about 7 by adding sodium hydroxide.
In some more preferred embodiments of the combined treatment system of the present invention, the coagulant is added in an amount of 0.5 to 3g/L to the secondary coagulating sedimentation tank, and then added after being prepared into a solution; the flocculant is PAM flocculant, and is prepared into a solution with the mass concentration of 0.1%, and the adding amount is 2-6 ml;
after the secondary coagulating sedimentation, the COD of the effluent is basically about 1200 mg/L.
In some more preferred embodiments of the combined treatment system of the present invention, the ozone dissolving device in the ozone advanced catalytic oxidation unit is an electromagnetic EM ozone dissolving device.
In an ozone advanced catalytic oxidation pond, the electromagnetic EM ozone dissolving device is utilized to efficiently blend ozone into a water body; the main principle of the electromagnetic EM ozone gas dissolving device is that the cluster structure in the water body is changed through the strong electromagnetic shear field action of the electromagnetic EM, so that particles are wrapped or other organic pollutant aggregates are fully opened to release single pollutants, and the organic matters which are difficult to degrade are further oxidized and decomposed through the strong oxidizing property of ozone and the high-efficiency catalytic activity of an ozone catalyst contained in a reaction tank; the residual COD is degraded, and the chromaticity and the smell are well removed, so that the water quality of the effluent is higher;
in the process stage, the ozone adding mode is jet aeration, water modified by an electromagnetic EM system is mixed with ozone through a venturi tube to form high-concentration ozone water, and then the high-concentration ozone water is added into a water body in a jet mode; high ozone utilization rate, delta COD/O 3 The ratio of the wastewater to the wastewater is 1:1.2-1.5, the degradation degree of pollutants is high, and the removal efficiency which cannot be achieved by the traditional ozone advanced oxidation pond is realized;
in the process stage, as the coagulant added in the coagulating sedimentation treatment is ferric salt coagulant, the water body contains more iron ions, part of organic pollutants can be coupled, the molecular bond energy of the organic pollutants is changed, and meanwhile, the electromagnetic EM ozone dissolving device is combined, so that the efficiency of removing the organic pollutants by ozone is improved, the treatment pressure of the subsequent process is reduced, and the efficiency of removing the organic pollutants by the process flow is improved;
the COD of the effluent of the advanced catalytic oxidation of ozone is basically about 220 mg/L.
In some more preferred embodiments of the combined treatment system of the present invention, the PH in the Fenton reaction tank is adjusted to 3-3.5, and the adding mass ratio of ferrous sulfate to hydrogen peroxide is 2-3: 1, the PH of the effluent is neutral.
The COD of the effluent after Fenton treatment is basically about 100mg/L.
In some more preferred embodiments of the combined treatment system of the invention, the electrocatalytic oxidation cell effluent COD is not higher than 100mg/L.
Preferably, the COD of the effluent after chemical treatment is about 55mg/L, which meets the emission standard.
In yet another aspect, the invention provides a combined treatment method for post-landfill leachate membrane concentrate, comprising the steps of:
the concentrated solution after the garbage leachate membrane is treated by a coagulating sedimentation tank, a PH regulating tank, a secondary coagulating sedimentation tank, an ozone advanced catalytic oxidation tank, a Fenton reaction tank and an electrocatalytic oxidation tank in sequence to obtain a water body which can reach the discharge standard; the sludge discharged by the coagulating sedimentation tank, the PH regulating tank, the secondary coagulating sedimentation tank and the Fenton reaction tank enters a sludge concentration tank, is dehydrated and then is sent to a sludge harmless landfill;
wherein the COD concentration of the concentrated solution after the landfill leachate membrane is 3500-5000 mg/L, and the concentration of ammonia nitrogen and total nitrogen is not more than 150mg/L; adding an iron salt coagulant into the coagulating sedimentation tank, and adding a non-iron salt coagulant into the secondary coagulating sedimentation tank; the COD of the final effluent is not higher than 100mg/L, preferably about 50mg/L.
In some preferred combined treatment method embodiments of the invention, the adding amount of the iron salt coagulant in the coagulating sedimentation tank is 10-16 g/L, and the iron salt coagulant is added after being prepared into solution; the flocculant is PAM flocculant, and is prepared into a solution with the mass concentration of 0.1%, the adding amount is 2-6 ml, and the hydraulic retention time is 3-8 h.
In some preferred embodiments of the combined treatment methods of the present invention, the PH of the water is adjusted in the PH adjustment tank to neutral PH of the effluent.
In some preferred combined treatment method embodiments of the invention, the addition amount of the non-ferric salt coagulant in the secondary coagulating sedimentation tank is 0.5-3 g/L, and the non-ferric salt coagulant is added after being prepared into a solution; the flocculant is PAM flocculant, and is prepared into a solution with the mass concentration of 0.1%, the adding amount is 2-6 ml, and the hydraulic retention time is 6-8 h.
In some preferred combined treatment method embodiments of the invention, ozone is added into the ozone advanced catalytic oxidation tank in a jet aeration mode of an electromagnetic EM ozone dissolving device, and the jet pump water flow reflux ratio is 1:3; the hydraulic retention time is 1.5-2 h; heterogeneous catalyst filler, preferably aluminum-based loaded manganese oxide and alpha-ferric oxide, is arranged in the ozone advanced catalytic oxidation tank.
In some preferred embodiments of the combined treatment method, the PH of the Fenton reaction tank is adjusted to 3-3.5, ferrous sulfate and hydrogen peroxide are added, and the adding mass ratio of the ferrous sulfate to the hydrogen peroxide is 2-3: 1, the hydraulic retention time is 1-3 h, and the PH of the effluent is regulated to be neutral.
In some preferred embodiments of the combined treatment methods of the present invention, the electrocatalytic oxidation cell has a hydraulic retention time of 20-40 min and a current density of 20mA/cm 2 。
Compared with the prior art, the combined treatment system and the treatment method for the post-landfill leachate membrane concentrated solution have the following advantages:
(1) The combined treatment system for the post-concentration liquid of the landfill leachate membrane has reasonable structural design, can effectively reduce the concentration of organic matters and other pollutants such as salt in the concentrated liquid by combining a Fenton treatment process and a micro-electrolysis process through coagulating sedimentation pretreatment and based on a novel ozone advanced oxidation process, and ensures that the post-treatment of the landfill leachate membrane concentrate realizes standard discharge, and has stable and reliable operation and low investment and operation cost;
(2) According to the combined treatment system for the post-concentrated solution of the landfill leachate membrane, a ferric salt flocculant is added in the coagulating sedimentation, through the coagulating sedimentation effect of the ferric salt, the aim of removing a part of organic pollutants is fulfilled, and meanwhile, a promoting effect is provided for the subsequent ozone advanced catalytic oxidation reaction, and the two stages of processes are connected, so that the organic pollutant removal efficiency of the post-concentrated solution of the landfill leachate membrane is greatly improved, and the standard of the treatment of the organic pollutants in the wastewater by the subsequent processes is ensured;
(3) The combined treatment method of the post-landfill concentrate of the landfill leachate membrane can treat the post-landfill concentrate of which the COD concentration is 3500-5000 mg/L and the ammonia nitrogen and total nitrogen concentration is not more than 150mg/L, ensures that the COD of the final effluent is not more than 100mg/L, is generally maintained at about 50mg/L, and has low investment running cost and no secondary pollution.
Drawings
FIG. 1 is a process flow diagram of a post-landfill leachate membrane concentrate combination treatment system according to example 1 of the present invention.
Detailed Description
Unless defined otherwise, technical terms used in the following examples have the same meaning as commonly understood by one of ordinary skill in the art to which the present invention pertains. The test reagents used in the following examples, unless otherwise specified, are all conventional biochemical reagents; the experimental methods are conventional methods unless otherwise specified.
The present invention will be described in detail with reference to the following examples and drawings.
Example 1
A combined treatment system for a post-concentration solution of a landfill leachate membrane is shown in fig. 1, and comprises a coagulating sedimentation tank, a PH regulating tank, a secondary coagulating sedimentation tank, an ozone advanced catalytic oxidation tank, a Fenton reaction tank, an electrocatalytic oxidation tank and a sludge concentration tank for receiving sludge discharged by the coagulating sedimentation tank, the PH regulating tank, the secondary coagulating sedimentation tank and the Fenton reaction tank which are connected in sequence;
wherein, the coagulant added in the coagulating sedimentation tank is ferric salt coagulant, and the flocculant added is PAM; the PH regulating tank regulates the PH of the effluent to be about 7 by adding sodium hydroxide; the coagulant added into the secondary coagulating sedimentation tank is aluminum salt coagulant, and the flocculant added into the secondary coagulating sedimentation tank is PAM; ozone is added into the ozone advanced catalytic oxidation pond in a jet aeration mode of an electromagnetic EM ozone dissolving device, and heterogeneous catalyst filler is arranged in the ozone advanced catalytic oxidation pond; adjusting the PH value in the Fenton reaction tank to 3-3.5, adding ferrous sulfate and hydrogen peroxide, and controlling the PH value of the effluent to be about 7 by adding sodium hydroxide; electrochemical treatment is carried out in the electrocatalytic oxidation pond by utilizing an electrochemical reactor consisting of a titanium dioxide polar plate group; the COD concentration of the concentrated solution after the garbage percolate film is 3500-5000 mg/L, the concentration of ammonia nitrogen and total nitrogen is not more than 150mg/L, and the COD of the final effluent is not more than 100mg/L.
A combined treatment method for post-concentration liquid of a landfill leachate membrane, which is shown in fig. 1, comprises the following steps:
s1, enabling concentrated solution after a landfill leachate membrane to enter a coagulating sedimentation tank, adding an iron salt coagulant and a PAM flocculant, after sedimentation, sending water into a PH regulating tank, and sending precipitated sludge into a sludge concentration tank; wherein, the adding amount of the ferric salt coagulant is 10-16 g/L, and the ferric salt coagulant is added after being prepared into solution; preparing PAM flocculant into 0.1% solution with the addition amount of 2-6 ml; the hydraulic retention time is 3-8 h;
the COD concentration of the concentrated solution after the garbage percolate film is 3500-5000 mg/L, the concentration of ammonia nitrogen and total nitrogen is not more than 150mg/L, and the COD of the effluent of the coagulating sedimentation tank is about 1500 mg/L;
s2, the water body enters a PH regulating tank, the PH of the water body is regulated to be about 7 by adding sodium hydroxide, after treatment, the sludge is sent into a sludge concentration tank, and the water body is sent into a secondary coagulating sedimentation tank;
s3, the water body enters a secondary coagulating sedimentation tank, an aluminum salt coagulant and a PAM flocculant are added, after treatment, the water body is sent into an ozone advanced catalytic oxidation tank, and sludge is sent into a sludge concentration tank; wherein, the adding amount of the aluminum salt coagulant is 0.5-3 g/L, and the aluminum salt coagulant is added after being prepared into solution; preparing PAM flocculant into 0.1% solution with the addition amount of 2-6 m and the hydraulic retention time of 6-8 h;
the COD of the effluent of the secondary coagulating sedimentation tank is about 1200 mg/L;
s4, the water body enters an ozone advanced catalytic oxidation pond, ozone is added into the electromagnetic EM ozone dissolving device in a jet aeration mode, and the water flow reflux ratio of a jet pump is 1:3; the hydraulic retention time is 1.5-2 h;
the COD of the effluent of the ozone advanced catalytic oxidation pond is about 220 mg/L;
s5, the water body enters a Fenton reaction tank, the pH value of the water body is adjusted to 3-3.5, ferrous sulfate and hydrogen peroxide are added, and the adding mass ratio of the ferrous sulfate to the hydrogen peroxide is 2-3: 1, the hydraulic retention time is 1-3 h; adding sodium hydroxide into the effluent, and adjusting the PH of the effluent to about 7; after treatment, the sludge is sent into a sludge concentration tank, and the water body is sent into an electrocatalytic oxidation tank;
the COD of the effluent of the Fenton reaction tank is about 100 mg/L;
s6, enabling the water body to enter an electrocatalytic oxidation tank, wherein the retention time is 20-40 min, and the current density is 20mA/cm 2 ；
The COD of the effluent of the electrocatalytic oxidation pond is about 55mg/L, which accords with the emission standard;
s7, dehydrating the sludge in the sludge concentration tank, and then delivering the dehydrated sludge to a sludge harmless landfill for landfill.
Application example 1
In the application example, the wastewater source is concentrated solution after nanofiltration of a landfill leachate, and the COD of inflow water is about 3300mg/L. Through the treatment process route described in the embodiment 1, the effluent can meet the discharge requirements of reaching standards.
The specific implementation steps are as follows:
step 1, enabling concentrated solution after nanofiltration of landfill leachate to enter a coagulating sedimentation tank, wherein the coagulating sedimentation tank is divided into a coagulating area, a flocculating area and a sedimentation area, the coagulating area is a coagulant adding area, a stirrer is arranged, the residence time is 10min, the flocculating area is a flocculant adding area, the stirrer is arranged, the residence time is 10min, the sedimentation area is a common tank body, a water outlet is arranged, after hydraulic retention and sedimentation, water is sent into a PH regulating tank, and precipitated sludge is sent into a sludge concentration tank;
wherein the coagulant is polymeric ferric sulfate, the adding amount is 12g/L, and the polymeric ferric sulfate is added after being prepared into a polymeric ferric sulfate solution with the mass concentration of 30 percent; the flocculant is Polyacrylamide (PAM), the mass concentration of the PAM flocculant is 0.1%, and the adding amount is 4 ml/L;
step 2, the water body enters a PH regulating tank, sodium hydroxide solution is added, and the PH of the water outlet is regulated to 7; after treatment, the sludge is sent into a sludge concentration tank, and the water body is sent into a secondary coagulating sedimentation tank;
step 3, the water body enters a secondary coagulating sedimentation tank, and an aluminum salt coagulant and a PAM flocculant are added for secondary coagulating sedimentation; preparing PAC coagulant into PAC coagulant solution with the mass concentration of 30%, and then adding the PAC coagulant solution with the adding amount of 6 ml/L; the mass concentration of the PAM flocculant is 0.1%, and the adding amount is 2ml/L; hydraulic retention time is 8h; the water body enters an ozone advanced catalytic oxidation tank, and the sludge enters a sludge concentration tank;
step 4, the water body enters an ozone advanced catalytic oxidation pond, the ozone adding amount is controlled to be 1.5g/L, the water flow reflux ratio of a jet pump is 1:3, the total residence time is 2h, the electromagnetic EM is externally connected with current 180A, the heterogeneous catalyst filler is aluminum-based loaded manganese oxide and alpha-ferric oxide, and the thickness of the heterogeneous catalyst filler is 0.8m;
step 5, the water body enters a Fenton reaction tank, the pH value is regulated to 3.5 by adopting sulfuric acid, the adding amount of ferrous sulfate is 16mg/L, the mass concentration of hydrogen peroxide is 30%, the adding amount is 8ml/L, after the residence time is controlled for 1h, sodium hydroxide is added into the effluent to regulate the pH value of the effluent to 7, after the effluent is kept stand for 30min by a sedimentation tank, the sludge is sent into a sludge concentration tank, and the water body is sent into an electrocatalytic oxidation tank;
step 6, water enters an electrocatalytic oxidation pond, the total residence time of the pond body is 30min, 11 groups of titanium polar plates are adopted as electrocatalytic polar plates, the area of each group of polar plates is 66cm x 100cm, the external current is 300A, and the current density is 20mA/cm 2 The method comprises the steps of carrying out a first treatment on the surface of the Obtaining water body which can reach the discharge standard;
and 7, dehydrating the sludge in the sludge concentration tank, and then delivering the dehydrated sludge to a sludge harmless landfill for landfill.
The water quality after the treatment at each stage in this application example is shown in table 1:
TABLE 1 Water quality data
| Project | Inflow of water | Coagulating sedimentation | PH regulating tank | Secondary coagulating sedimentation | Advanced catalytic oxidation of ozone | Fenton | Electrocatalytic oxidation | Treatment rate | Running cost |
| COD（mg/L） | 3300 | 1625 | 1600 | 1200 | 220 | 99 | 55 | 100% | 150 yuan/ton |
Comparative example 1
In the comparative example, the COD of the influent water is about 3750mg/L.
And (3) treating the concentrated solution after nanofiltration of the landfill leachate, wherein the steps are as follows:
step 1, pre-treating concentrated solution after nanofiltration of landfill leachate, wherein a pretreatment system comprises an adjusting tank and a dissolved air flotation tank, the pH value of the concentrated solution after membrane treatment is adjusted to 7 by the adjusting tank, PAC coagulant solution with the mass concentration of 30% is added after the concentrated solution enters the dissolved air flotation tank, PAM flocculant solution with the addition of 6mL/L and the mass concentration of 0.1% is added, and suspended matters, oils and partial organic pollutants are removed by the addition of 6 mL/L;
adding 2ml/L of scale inhibitor into the effluent of the floatation tank;
and 2, enabling effluent of the air floatation tank to enter an MVR evaporator, forming supernatant through multistage MVR evaporation, discharging, enabling evaporated materials to enter a centrifugal salt discharging system, separating to obtain crystalline salt, and enabling mother liquor after centrifugation to flow back to a pretreatment section.
The water quality after each stage of treatment in this comparative example is shown in table 2:
TABLE 2 Water quality data
| Project | Inflow of water | Pretreatment of | MVR evaporation | Treatment rate | Running cost |
| COD（mg/L） | 3750 | 3328 | ＜100 | 90% | 220 yuan/ton |
Comparative example 2
In the comparative example, the wastewater source is concentrated solution after nanofiltration of some landfill leachate, and COD of inflow water is about 3300mg/L.
And (3) performing pre-oxidation, biochemical treatment and advanced oxidation treatment on the concentrated solution after nanofiltration of the landfill leachate, wherein the steps are as follows:
step 1, after nanofiltration of some landfill leachate, the concentrated solution is counted into Fenton oxidation treatment through an adjusting tank, the PH is adjusted to 4 by sulfuric acid, ferrous sulfate and hydrogen peroxide are added, the total residence time is 1h, then sodium hydroxide is added into effluent to adjust the PH to 7, and the supernatant fluid enters A after coagulating sedimentation 2 O is subjected to biochemical treatment;
step 2, A 2 In the O treatment process, adding a carbon source into an anaerobic section, keeping the anaerobic section for 8 hours, and controlling the dissolved oxygen to be 0-0.3 mg/L;the retention time of the aerobic section is 8 hours, the aerobic nitrifying liquid flows back to the anaerobic section, the reflux ratio is 1:3, and the dissolved oxygen is controlled to be about 2.5 mg/L;
step 3, the effluent of the biochemical treatment section enters an MBR reactor, the MBR is used for replacing a secondary sedimentation tank in the step, and meanwhile, part of organic matters and particulate matters are removed by using membrane-hanging microorganisms, and the residence time is 6h;
and 4, introducing MBR effluent into an ozone advanced oxidation tank to remove organic pollutants which cannot be degraded by biochemistry, and adding ozone in the form of an aeration disc for 1h.
The water quality after each stage of treatment in this comparative example is shown in Table 3:
TABLE 3 Water quality data
| Project | Inflow of water | Fenton | A 2 O | MBR | Advanced oxidation of ozone | Treatment rate | Running cost |
| COD（mg/L） | 3300 | 1960 | 890 | 820 | 440 | 100% | 110 yuan/ton |
In conclusion, the method comprises the steps of,
from the data in tables 1, 2 and 3, it can be seen that: the COD of the water body finally obtained in the table 1 is less than 100mg/L, the pollutant removing effect is good, the discharge requirement is met, no secondary sewage is generated, the inflow water can be completely treated, and the treatment rate of 100% of the inflow water is realized; compared with the table 1 and the table 2, the COD of the water body finally obtained in the table 2 is less than 100mg/L, but the treatment process has high operation cost, and the inflow water cannot be completely treated, so that secondary sewage is generated, and the treatment rate of the wastewater is low and is only 90%; table 1 shows that the running cost of Table 3 is lower than that of Table 3, no secondary sewage is generated, and the treatment rate of wastewater reaches 100%, but the COD of the final effluent is 440 mg/L, the pollutant removal effect is poor, and the effluent does not meet the emission standard.
Comparative example 4
In order to verify the influence of the addition of the ferric salt flocculant on the pollutant removal rate, in the comparative example, on the basis of application example 1, the difference is that the ferric salt coagulant is not added into the coagulating sedimentation tank, the same amount of aluminum salt coagulant is added instead, and other steps are the same as application example 1, and are not repeated here.
The water quality after each stage of treatment in this comparative example is shown in Table 4:
TABLE 4 Water quality data
| Project | Inflow of water | PAC coagulation sedimentation | PH regulating tank | Secondary coagulating sedimentation | Advanced catalytic oxidation of ozone | Fenton | Electrocatalytic oxidation | Treatment rate | Running cost |
| COD（mg/L） | 3300 | 2630 | 2600 | 2552 | 1544 | 965 | 555 | 100% | 140 yuan/ton |
As can be seen from Table 4, when the coagulant of aluminum salt is added in the coagulating sedimentation, the pollutant removal effect measured by the effluent of the coagulating sedimentation tank is poor, the subsequent advanced catalytic oxidation of ozone does not play a synergistic effect, the pollutant content of the effluent of the advanced catalytic oxidation of ozone is higher, and the pollutant content of the final effluent is influenced. It is known that the addition of the ferric salt coagulant can produce synergistic effect with ozone in addition to the coagulation effect of the ferric salt coagulant, and the removal rate of pollutants is further improved.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the invention.
Claims (9)
1. A landfill leachate membrane post-concentrate combination treatment system is characterized in that: the device comprises a coagulating sedimentation tank, a PH regulating tank, a secondary coagulating sedimentation tank, an ozone advanced catalytic oxidation tank, a Fenton reaction tank, an electrocatalytic oxidation tank and a sludge concentration tank, wherein the coagulating sedimentation tank, the PH regulating tank, the secondary coagulating sedimentation tank, the ozone advanced catalytic oxidation tank, the Fenton reaction tank and the electrocatalytic oxidation tank are sequentially connected; the coagulant added into the coagulating sedimentation tank is ferric salt coagulant; the coagulant added into the secondary coagulating sedimentation tank is a non-ferric salt coagulant.
2. The post-landfill leachate membrane concentrate combination treatment system of claim 1, wherein: the flocculating agent added into the coagulating sedimentation tank is PAM; the coagulant added into the secondary coagulating sedimentation tank is aluminum salt coagulant, and the flocculant added into the secondary coagulating sedimentation tank is PAM.
3. The post-landfill leachate membrane concentrate combination treatment system according to claim 1 or 2, wherein: the COD concentration of the post-concentration solution of the landfill leachate membrane is 3500-5000 mg/L, and the concentration of ammonia nitrogen and total nitrogen is not more than 150mg/L.
4. A post-landfill leachate membrane concentrate combination treatment system according to claim 3, wherein: the adding amount of the coagulant in the coagulating sedimentation tank is 10-16 g/L; the PH of the effluent of the PH regulating tank is neutral; the adding amount of the coagulant in the secondary coagulating sedimentation tank is 0.5-3 g/L; the ozone dissolving device in the ozone advanced catalytic oxidation tank is an electromagnetic EM ozone dissolving device; PH is adjusted to 3-3.5 in the Fenton reaction tank, and the adding mass ratio of ferrous sulfate to hydrogen peroxide is 2-3: 1, the PH of the effluent is neutral; the COD of the effluent of the electrocatalytic oxidation pond is not higher than 100mg/L.
5. A combined treatment method for post-concentration liquid of a landfill leachate membrane, which is characterized by comprising the following steps of:
the concentrated solution after the garbage leachate membrane is treated by a coagulating sedimentation tank, a PH regulating tank, a secondary coagulating sedimentation tank, an ozone advanced catalytic oxidation tank, a Fenton reaction tank and an electrocatalytic oxidation tank in sequence to obtain a water body which can reach the discharge standard; the sludge discharged by the coagulating sedimentation tank, the PH regulating tank, the secondary coagulating sedimentation tank and the Fenton reaction tank enters a sludge concentration tank, is dehydrated and then is sent to a sludge harmless landfill;
wherein the COD concentration of the concentrated solution after the landfill leachate membrane is 3500-5000 mg/L, and the concentration of ammonia nitrogen and total nitrogen is not more than 150mg/L; adding an iron salt coagulant into the coagulating sedimentation tank, and adding a non-iron salt coagulant into the secondary coagulating sedimentation tank; and the COD of the final effluent is not higher than 100mg/L.
6. The post-landfill leachate membrane concentrate combination treatment method according to claim 5, wherein: the adding amount of the iron salt coagulant in the coagulating sedimentation tank is 10-16 g/L, and the hydraulic retention time is 3-8 h;
the PH of the water body is regulated in the PH regulating tank, so that the PH of the effluent is neutral;
the adding amount of the non-ferric salt coagulant in the secondary coagulating sedimentation tank is 0.5-3 g/L, and the hydraulic retention time is 6-8 h.
7. The post-landfill leachate membrane concentrate combination treatment method according to claim 5, wherein: ozone is added into the ozone advanced catalytic oxidation tank in a jet aeration mode of an electromagnetic EM ozone dissolving device, and the water flow reflux ratio of a jet pump is 1:3; the hydraulic retention time is 1.5-2 h; and heterogeneous catalyst filler is arranged in the ozone advanced catalytic oxidation pond.
8. The post-landfill leachate membrane concentrate combination treatment method according to claim 5, wherein: in the Fenton reaction tank, the PH is adjusted to 3-3.5, ferrous sulfate and hydrogen peroxide are added, and the adding mass ratio of the ferrous sulfate to the hydrogen peroxide is 2-3: 1, the hydraulic retention time is 1-3 h, and the PH of the effluent is regulated to be neutral.
9. The post-landfill leachate membrane concentrate combination treatment method according to claim 5, wherein: the hydraulic retention time in the electrocatalytic oxidation pond is 20-40 min, and the current density is 20mA/cm 2 。
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