CN210237367U - Arid cold area landfill leachate processing apparatus - Google Patents
Arid cold area landfill leachate processing apparatus Download PDFInfo
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- CN210237367U CN210237367U CN201920973939.4U CN201920973939U CN210237367U CN 210237367 U CN210237367 U CN 210237367U CN 201920973939 U CN201920973939 U CN 201920973939U CN 210237367 U CN210237367 U CN 210237367U
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Abstract
The utility model relates to a sewage treatment field especially relates to a arid cold region landfill leachate processing apparatus. The treatment device comprises a PH adjusting tank (1), a flocculation reaction tank (2), a sedimentation tank (3), a sand filter (5), an ultrafiltration system (8), a primary DT-RO (13), a secondary DT-RO (17), an evaporation system (19) and a sludge dewatering system (20); DT-RO is a disc tube type reverse osmosis system. 1) The utility model does not use a biochemical treatment method and can not be influenced by temperature and water quality fluctuation. 2) The load of the membrane system is reduced. 3) And is beneficial to the stable operation of the system. Saving manpower and easy management.
Description
Technical Field
The invention relates to the field of sewage treatment, in particular to a garbage leachate treatment device in a drought and cold area.
Background
The landfill leachate in the arid and cold areas is greatly different from the landfill leachate indexes of other areas due to the reasons that the rainfall capacity is smaller than the evaporation capacity, the temperature is low and the like, and mainly reflects high contents of COD, ammonia nitrogen, TDS, metals and the like, imbalance of proportion of microbial nutrient elements and the like. Humic acid in the form ofThe humic acid is mainly macromolecular humic acid and has strong stability, and functional groups at the edges of humic acid molecules have the capacity of adsorbing inorganic substances and inorganic compounds. Humic acid is soluble in water under alkaline conditions, but can absorb divalent cations (Ca) under acidic conditions2+，Mg2+) A precipitate is generated.
The widely applied landfill leachate treatment technology in the industry generally comprises two technologies, one is a biochemical and two-stage DT-RO treatment technology, the process has high degree of automatic control and low technical risk, but the leachate in arid and cold regions has poor biodegradability, so the treatment difficulty is high, and the actual application effect is poor. The other is an evaporation and EDI ion exchange treatment process, which has the disadvantages of complex practical application, high energy consumption, high maintenance cost, high cleaning frequency of a later-stage evaporation tank and high medicament cost.
Disclosure of Invention
The purpose of the invention is as follows: in order to provide a better-effect device and a better-effect method for treating landfill leachate in the drought and cold regions, specific purposes are shown in a plurality of substantial technical effects of a specific implementation part.
In order to achieve the purpose, the invention adopts the following technical scheme:
the first scheme is as follows:
a landfill leachate treatment device in arid and cold regions is characterized by comprising a PH adjusting tank 1, wherein the PH adjusting tank 1 is connected with a flocculation reaction tank 2 through a pipeline, the flocculation reaction tank 2 is connected with a sedimentation tank 3 through a pipeline, the sedimentation tank 3 extends out of the pipeline and is connected with a PH readjustment tank 4, the PH readjustment tank 4 is connected with a sand filter tank 5 through a pipeline, the sand filter tank 5 is connected with a first buffer water tank 6 through a pipeline, the first buffer water tank 6 is connected with a first security filter 7, the first security filter 7 is connected with an ultrafiltration system 8 through a pipeline, and the ultrafiltration system 8 is connected with a second buffer water tank 9 through a pipeline; the second buffer water tank 9 is connected with an inlet of the first heat exchanger 10 through a pipeline, an outlet of the first heat exchanger 10 is connected with an inlet of the second cartridge filter 11 through a pipeline, an outlet of the second cartridge filter 11 is connected with a water inlet end of the first-stage DT-RO13 through a first plunger pump 12, a water production end of the first-stage DT-RO13 is connected with the third buffer water tank 14 through a pipeline, and a concentrated water end of the first-stage DT-RO13 is connected with a concentrated water tank 18; the third buffer water tank 14 is connected with a second heat exchanger 15, the second heat exchanger 15 is connected with the inlet end of a second plunger pump 16, and the water outlet end of the second plunger pump 16 is connected with the water inlet end of the second-stage DT-RO 17; the water production end of the second-stage DT-RO17 is connected with the water production tank 21 through a pipeline, and the concentrated water end is connected with the second buffer water tank 9; the concentrated water tank is connected with an evaporation system 19 through a lift pump, and a condensate outlet of the evaporation system 19 is connected with a pH adjusting tank 1; the sedimentation tank 3 is connected with a sludge tank 22 through a pipeline, and the sludge tank 22 is connected with a filter press 20 through a pipeline; DT-RO is a disc tube type reverse osmosis system.
Scheme II:
a method for treating landfill leachate in arid and cold regions is characterized by comprising the following steps,
1) collecting the landfill leachate to a pH adjusting tank, adding sulfuric acid, adjusting the pH to 3-4, and absorbing divalent cation Ca by humic acid2+、Mg2+Generating precipitate, and simultaneously generating carbon dioxide by carbonate to escape;
2) adding a coagulant and a flocculant into the flocculation reaction tank to promote the separation of suspended particles and humic acid sediment in the leachate from water;
3) discharging the sludge generated in the step 2) to a sludge concentration tank, pressurizing by a pump, lifting to a sludge dewatering device for sludge-water separation, treating sludge cakes as agricultural fertilizers or transporting the sludge cakes outside, and returning the filter pressing liquid to an adjusting tank for circular treatment;
4) feeding the flocculated and precipitated effluent into a pH adjusting tank, adding a sodium hydroxide solution, adjusting the pH to 6-6.5, lifting the effluent into a sand filter through a pump, removing suspended solid impurities, and preventing the impurities from entering a subsequent ultrafiltration system; the produced water of the sand filter enters a first buffer water tank; the sand filtration system performs back flushing by using water in the first buffer water tank, and back flushing wastewater is discharged to the sludge concentration tank;
5) the water in the first buffer water tank is lifted by a pump to enter an ultrafiltration system, and residual fine particles and suspended matter impurities in the pretreated water are removed by utilizing the physical interception function of an ultrafiltration membrane, so that a subsequent membrane element is protected; the effluent of the ultrafiltration enters a second buffer water tank, and concentrated water flows back to the regulating tank; concentrated water generated by ultrafiltration flushing flows back to the regulating tank for circular treatment;
6) the ultrafiltration effluent in the second buffer water tank is pressurized by a high-pressure pump and enters a first-level disc tube type reverse osmosis system, most soluble salts, organic matters and hardness in the water are intercepted and removed by a membrane element, the permeate of the first-level disc tube type reverse osmosis system enters a third buffer water tank, and the concentrated water enters a concentrated water tank for storage. The concentrated water is lifted by a pump and enters an evaporation system for evaporation, drying and crystallization, the evaporation condensate returns to an adjusting tank for circular treatment, and the crystallized salt is transported outside for disposal or recycling;
7) the water produced by the first-stage disc-tube type reverse osmosis system in the third buffer water tank is pressurized by a high-pressure pump and enters a second-stage disc-tube type reverse osmosis system for further treatment, the water produced by the second-stage disc-tube type reverse osmosis system enters a water producing pool to be reused as the flushing water of the reverse osmosis system, and the rest of the water is discharged after reaching the standard; and the concentrated water enters a second buffer water tank and returns to the first-stage disc tube type reverse osmosis system for circular treatment.
The further technical scheme of the invention is that in the step 1), a stirring device is arranged in the regulating tank, and the stirring device is a mechanical stirring device or an air stirring device.
The further technical scheme of the invention is that the flocculation reaction tank in the step 2) is divided into a reaction area and a precipitation area, and the reaction area is provided with a mechanical stirring device; the used coagulant is inorganic salt coagulant or polymer coagulant; the flocculant used was polyacrylamide.
The further technical scheme of the invention is that the booster pump mentioned in the step 3) is a G-shaped screw pump, and the sludge dewatering device is one of a plate-and-frame filter press or a stacked-screw type sludge dewatering machine.
The further technical scheme of the invention is that the sand filter in the step 4) adopts a civil engineering pool body or integrated equipment.
The further technical scheme of the invention is that the ultrafiltration used in the step 5) is tubular ultrafiltration, each system is provided with a raw water pump and a circulating pump, and the water yield is at least 90%.
The further technical scheme of the invention is that the high-pressure pump for pressurizing the disc-tube type reverse osmosis system in the step 6) and the step 7) is plunger pumps, and a shock absorber is arranged behind each plunger pump and is used for absorbing pressure pulses generated by the high-pressure pump and providing stable pressure for the membrane column.
The further technical scheme of the invention is that the evaporation mode of the evaporation system used in the step 7) is one of MVR and MED evaporation modes.
Compared with the prior art, the invention adopting the technical scheme has the following beneficial effects:
1) the invention does not use a biochemical treatment method and can not be influenced by temperature and water quality fluctuation.
2) The pretreatment adopts a mode of adding acid to adjust the pH value of the inlet water to be acidic, the humic acid is combined with calcium ions to generate precipitation, a large amount of precipitation is removed, simultaneously the hardness is removed, the load of a membrane system is reduced, and the cleaning period of the membrane system is prolonged. The humic acid which takes humic acid as the main component is obtained by precipitation, and can be used as agricultural fertilizer for recycling after dehydration.
3) Under the acidic condition, the method can effectively remove the carbonate, reduce the scale ions in the evaporation main reactor and prolong the scale formation time of the heat exchange tube. Because the scaling anions are reduced, the concentration of the 2-valent cations in the discharged concentrated solution is obviously increased, and the stable operation of the system is facilitated.
4) The invention has the characteristics of small equipment volume, small occupied area, no secondary pollution, investment cost saving, high automation degree, manpower saving and easy management.
Drawings
To further illustrate the present invention, further description is provided below with reference to the accompanying drawings:
FIG. 1 is a schematic view of the inventive connection structure;
FIG. 2 is a schematic view of the inventive process flow;
FIG. 3 shows the main water inlet and outlet indicators and water amount of the project of the first embodiment;
wherein: 1, a PH adjusting tank; 2. a flocculation reaction tank; 3. a sedimentation tank; 4, returning the PH to the pool; 5. a sand filter; 6. a first buffer water tank; 7. a first security filter; 8. an ultrafiltration system; 9. a second buffer water tank; 10. a first heat exchanger; 11. a second security filter; 12. a plunger pump I; 13. primary DT-RO; 14. a third buffer water tank; 15. a second heat exchanger; 16. a plunger pump II; 17. secondary DT-RO; 18. a dense water tank; 19. an evaporation system; 20. a filter press; 21. a water producing pool; 22. a sludge tank.
Detailed Description
The present invention will be further illustrated with reference to the accompanying drawings and specific embodiments, which are to be understood as merely illustrative of the invention and not as limiting the scope of the invention. In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", "top", "bottom", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. Furthermore, unless expressly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, as they may be fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art. The connection in this context is mostly via pipes.
The patent provides a plurality of parallel schemes, and different expressions belong to an improved scheme based on a basic scheme or a parallel scheme. Each solution has its own unique features.
The first embodiment is as follows:
the average COD value of the leachate treatment project of a certain domestic garbage landfill in Xinjiang is above 7000Mg/L, the TDS value is above 30000Mg/L, and the hardness is mainly Mg2+Mainly of Ca2+Low total hardness greater than 1500mg/L and daily treatment capacity of 100m3And/d, treating the mixture by the following steps:
1) collecting the garbage percolate to a pH adjusting tank, arranging a pH online monitoring system in the adjusting tank, interlocking with an acid adding pump, adding sulfuric acid, controlling the pH in the adjusting tank to be 3-4, and fully stirring the percolate by using an air stirring device;
2) the flocculation reaction tank is divided intoA coagulant and a flocculant are added into the reaction zone, the mixture is fully stirred and precipitated, and the generated precipitated sludge enters a sludge concentration tank; the flocculation reaction time is 15-30 minutes, and the surface load of a settling zone is preferably 1.5m3/(m2H); the main component of the precipitate is divalent cation (Ca) absorbed2+，Mg2+) Precipitating the humic acid;
3) the precipitated effluent enters a pH adjusting tank, the pH is adjusted to about 6.5, the effluent enters a sand filtration tank after being lifted, suspended matters with the size of more than 100 mu m are removed, the sand filtration tank is back flushed by air water, a back flushing water source adopts a sand filtration system to produce water, and back flushing wastewater enters an adjusting tank for circular treatment.
4) The sand filtration tank produced water enters the buffer water tank 1, enters the tubular ultrafiltration system after being lifted, and removes the residual impurities such as fine particles, suspended matters and the like in the pretreated water by utilizing the physical interception function of the UF membrane, thereby protecting the subsequent membrane elements. The system is provided with 2 8-inch tubular ultrafiltration membranes, 1 raw water pump and 1 circulating pump. The flow rate of the filtered water is obviously reduced and is lower than a preset value (about 20% -30% lower than normal flux), and the membrane is chemically cleaned, wherein the chemical cleaning period is generally 2-8 weeks.
The ultrafiltration effluent enters a buffer water tank 2, and the concentrated water flows back to the regulating tank. The wastewater generated by the ultrafiltration flushing flows back to the regulating tank for circular treatment;
5) and (3) pressurizing the percolate in the buffer tank 2 by using a booster pump, pumping the percolate into a primary DT-RO system by using a plunger pump after passing through a security filter, and adding a scale inhibitor into the system by using a metering pump, wherein the adding amount is about 3-5 ppm. And (3) the primary DT-RO concentrated water enters an evaporation system for evaporation and crystallization, the evaporation condensate returns to the regulating reservoir for cyclic treatment, and the crystallized salt is transported outside for disposal or recycling. The primary DT-RO produced water enters a buffer water tank 3;
6) and the percolate in the buffer tank 3 enters a plunger pump through a booster pump, is pumped into a secondary DT-RO system by the plunger pump, the concentrated water returns to the buffer tank 2, the produced water enters a water producing pool and is used as a membrane system cleaning water source, and the excess water is discharged.
TABLE 1 Main indexes of water inlet and outlet and water quantity
| Categories | Amount of water (m)3/d) | Whole salt (mg/L) | COD(mg/L) | Total nitrogen (mg/L) |
| |
100 | 30000 | 7000 | 2500 |
| |
40 | 75000 | 17500 | 6400 |
| |
60 | 130 | 30 | 10 |
In general, the implementation of this scheme is as follows:
1) collecting the landfill leachate to a pH adjusting tank, adding sulfuric acid, adjusting the pH to 3-4, and absorbing divalent cations (Ca) by humic acid2+，Mg2+) Precipitation occurs while carbonate forms carbon dioxide to escape.
2) Adding a coagulant and a flocculant into the flocculation reaction tank to promote the separation of suspended particles and humic acid sediment in the leachate from water;
3) discharging the sludge generated in the step 2) to a sludge concentration tank, pressurizing by a pump, lifting to a sludge dewatering device for sludge-water separation, treating sludge cakes as agricultural fertilizers or transporting the sludge cakes outside, and returning the filter pressing liquid to an adjusting tank for circular treatment;
4) and (3) allowing the flocculated and precipitated effluent to enter a pH adjusting tank, adding a sodium hydroxide solution, adjusting the pH to 6-6.5, lifting the effluent into a sand filter through a pump, removing suspended solid impurities, and preventing the impurities from entering a subsequent ultrafiltration system. The produced water of the sand filter enters a buffer water tank 1; the sand filtration system utilizes the water in the buffer water tank 1 to carry out back flushing, and the back flushing wastewater is discharged to a sludge concentration tank;
5) the water in the buffer water tank 1 is lifted by a pump to enter an ultrafiltration system, and impurities such as residual fine particles, suspended matters and the like in the pretreated water are removed by utilizing the physical interception function of an ultrafiltration membrane, so that the subsequent membrane element is protected. The ultrafiltration effluent enters a buffer water tank 2, and the concentrated water flows back to the regulating tank. Concentrated water generated by ultrafiltration flushing flows back to the regulating tank for circular treatment;
6) the ultrafiltration effluent in the buffer water tank 2 is pressurized by a high-pressure pump, enters a primary disc tube type reverse osmosis (DT-RO) system, most soluble salts, organic matters, hardness and the like in the water are intercepted and removed by a membrane element, the permeate of the primary DT-RO system enters the buffer water tank 3, the concentrated water enters a concentrated water tank for storage, is lifted by a pump and enters an evaporation system for evaporation, drying and crystallization, the evaporation condensate returns to an adjusting tank for cyclic treatment, and the crystallized salt is transported outside for disposal or recycling.
7) The primary DT-RO produced water in the buffer water tank 3 is pressurized by a high-pressure pump and enters a secondary DT-RO for further treatment, the secondary DT-RO produced water enters a water producing pool to be reused as the washing water of a reverse osmosis system, and the rest is discharged after reaching the standard; the concentrated water enters the buffer water tank 2 and returns to the primary DT-RO system for circular treatment.
Specifically, in the step 1), a stirring device is arranged in the regulating tank, and the stirring device can be mechanical stirring or air stirring;
the flocculation reaction tank in the step 2) is divided into a reaction area and a precipitation area, and the reaction area is provided with a mechanical stirring device. The coagulant can be inorganic salt coagulant or polymer coagulant; the flocculant used is polyacrylamide;
the booster pump mentioned in the step 3) is a G-shaped screw pump, and the sludge dewatering device can be one of a plate-and-frame filter press or a stacked-screw type sludge dewatering machine;
the sand filter in the step 4) can adopt a civil engineering pond body or integrated equipment.
The ultrafiltration used in the step 5) is tubular ultrafiltration, each set of system is provided with a raw water pump and a circulating pump, and the water yield is at least 90 percent;
step 6) the high-pressure pump for pressurizing the DT-RO system in the step 7) is a plunger pump, and a shock absorber is arranged behind each plunger pump and used for absorbing pressure pulses generated by the high-pressure pump and providing stable pressure for the membrane column;
the DT-RO system in the step 7) can select primary or secondary treatment according to the actual effluent requirement;
and 7) selecting evaporation modes such as MVR, MED and the like according to actual needs by using the evaporation system used in the step 7).
Creatively, the above effects exist independently, and the combination of the above results can be completed by a set of structure.
1) The invention does not use a biochemical treatment method and can not be influenced by temperature and water quality fluctuation.
| Suitable temperature (. degree.C.) | BOD5/COD | C:N:P | |
| |
15～35 | ＞0.3 | 100:5:1 |
| The invention | ≤45 | Without limitation | Without limitation |
2) The pretreatment adopts a mode of adding acid to adjust the pH value of the inlet water to be acidic, the humic acid is combined with calcium ions to generate precipitation, a large amount of precipitation is removed, simultaneously the hardness is removed, the load of a membrane system is reduced, and the cleaning period of the membrane system is prolonged. The humic acid which takes humic acid as the main component is obtained by precipitation, and can be used as agricultural fertilizer for recycling after dehydration.
The reaction equation is as follows:
R+Ca2+→RCa↓
R+Mg2+→RMg↓
3) under the acidic condition, the method can effectively remove the carbonate, reduce the scale ions in the evaporation main reactor and prolong the scale formation time of the heat exchange tube. Because the scaling anions are reduced, the concentration of the 2-valent cations in the discharged concentrated solution is obviously increased, and the stable operation of the system is facilitated.
The reaction equation is as follows:
2H++CO3 2-→H2O+CO2↑
4) the invention has the characteristics of small equipment volume, small occupied area, no secondary pollution, investment cost saving, high automation degree, manpower saving and easy management.
Measured as 100 tons/day landfill leachate:
the technical effect that above structure was realized realizes clearly, if do not consider additional technical scheme, this patent name can also be a novel environmental protection structure and purification method. Some details are not shown in the figures.
It should be noted that the plurality of schemes provided in this patent include their own basic schemes, which are independent of each other and are not restricted to each other, but they may be combined with each other without conflict, so as to achieve a plurality of effects.
The foregoing shows and describes the general principles, essential features, and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are intended to illustrate the principles of the invention, but that various changes and modifications may be made without departing from the spirit and scope of the invention, and the invention is to be limited to the embodiments described above.
Claims (1)
1. The garbage leachate treatment device in the arid and cold regions is characterized by comprising a PH adjusting tank (1), wherein the PH adjusting tank (1) is connected with a flocculation reaction tank (2) through a pipeline, the flocculation reaction tank (2) is connected with a sedimentation tank (3) through a pipeline, the sedimentation tank (3) extends out of the pipeline and is connected with a PH callback tank (4), the PH callback tank (4) is connected with a sand filter tank (5) through a pipeline, the sand filter tank (5) is connected with a first buffer water tank (6) through a pipeline, the first buffer water tank (6) is connected with a first security filter (7), the first security filter (7) is connected with an ultrafiltration system (8) through a pipeline, and the ultrafiltration system (8) is connected with a second buffer water tank (9) through a pipeline; the second buffer water tank (9) is connected with an inlet of the first heat exchanger (10) through a pipeline, an outlet of the first heat exchanger (10) is connected with an inlet of the second security filter (11) through a pipeline, an outlet of the second security filter (11) is connected with a water inlet end of the first-stage DT-RO (13) through a first plunger pump (12), a water producing end of the first-stage DT-RO (13) is connected with a third buffer water tank (14) through a pipeline, and a concentrated water end of the first-stage DT-RO (13) is connected with a concentrated water tank (18); the third buffer water tank (14) is connected with the second heat exchanger (15), the second heat exchanger (15) is connected with the inlet end of the second plunger pump (16), and the water outlet end of the second plunger pump (16) is connected with the water inlet end of the second DT-RO (17); the water production end of the second-stage DT-RO (17) is connected with a water production pool (21) through a pipeline, and the concentrated water end is connected with a second buffer water tank (9); the concentrated water tank is connected with an evaporation system (19) through a lift pump, and a condensate outlet of the evaporation system (19) is connected with the pH adjusting tank (1); the sedimentation tank (3) is connected with a sludge tank (22) through a pipeline, and the sludge tank (22) is connected with a filter press (20) through a pipeline; DT-RO is a disc tube type reverse osmosis system.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110240342A (en) * | 2019-06-26 | 2019-09-17 | 山东百川集大环境工程有限公司 | A kind of arid and cold region garbage leachate treatment device and method |
| WO2022057052A1 (en) * | 2020-09-17 | 2022-03-24 | 广东闻扬环境科技有限公司 | Treatment system and treatment method for landfill leachate wastewater |
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2019
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110240342A (en) * | 2019-06-26 | 2019-09-17 | 山东百川集大环境工程有限公司 | A kind of arid and cold region garbage leachate treatment device and method |
| CN110240342B (en) * | 2019-06-26 | 2024-04-09 | 山东百川集大环境工程有限公司 | Device and method for treating landfill leachate in arid and cold regions |
| WO2022057052A1 (en) * | 2020-09-17 | 2022-03-24 | 广东闻扬环境科技有限公司 | Treatment system and treatment method for landfill leachate wastewater |
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