CN111675367A - DTRO landfill leachate concentrated solution near zero emission treatment system and implementation method thereof - Google Patents
DTRO landfill leachate concentrated solution near zero emission treatment system and implementation method thereof Download PDFInfo
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 96
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- 239000002244 precipitate Substances 0.000 claims abstract description 16
- 238000003825 pressing Methods 0.000 claims abstract description 16
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- 239000012528 membrane Substances 0.000 claims description 9
- 238000011084 recovery Methods 0.000 claims description 8
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 claims description 7
- 229910001425 magnesium ion Inorganic materials 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 7
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 5
- 229910052791 calcium Inorganic materials 0.000 claims description 5
- 239000011575 calcium Substances 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 5
- 238000004062 sedimentation Methods 0.000 claims description 5
- 239000004568 cement Substances 0.000 claims description 4
- 239000002738 chelating agent Substances 0.000 claims description 4
- 239000012141 concentrate Substances 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- 239000010881 fly ash Substances 0.000 claims description 4
- 239000002920 hazardous waste Substances 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 4
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 3
- 230000000903 blocking effect Effects 0.000 claims description 3
- 229910001424 calcium ion Inorganic materials 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 2
- 239000013049 sediment Substances 0.000 claims description 2
- 239000012466 permeate Substances 0.000 claims 1
- 150000003839 salts Chemical class 0.000 abstract description 4
- 239000002910 solid waste Substances 0.000 abstract description 2
- 230000008569 process Effects 0.000 description 8
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 5
- 208000028659 discharge Diseases 0.000 description 5
- 230000033228 biological regulation Effects 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 235000011132 calcium sulphate Nutrition 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
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- 230000006911 nucleation Effects 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- POJAQDYLPYBBPG-UHFFFAOYSA-N 2-(2,4,7-trinitrofluoren-9-ylidene)propanedinitrile Chemical compound [O-][N+](=O)C1=CC([N+]([O-])=O)=C2C3=CC=C([N+](=O)[O-])C=C3C(=C(C#N)C#N)C2=C1 POJAQDYLPYBBPG-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
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- 230000009286 beneficial effect Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 235000010216 calcium carbonate Nutrition 0.000 description 1
- 239000001175 calcium sulphate Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 238000010903 primary nucleation Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
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- 239000002689 soil Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- Engineering & Computer Science (AREA)
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- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to a DTRO landfill leachate concentrated solution near zero emission treatment system and an implementation method thereof, wherein a treatment object is a concentrated solution generated by DTRO treatment of landfill leachate. The device comprises a first-stage reverse osmosis mechanism, a drainage reverse osmosis mechanism, a second-stage reverse osmosis mechanism, a crystal seed crystallization device, a nanofiltration mechanism, a hydraulic cyclone separation mechanism, a filter pressing mechanism and a dehydration mechanism, wherein a clear water outlet of the first-stage reverse osmosis mechanism is connected with the drainage reverse osmosis mechanism, a concentrated water outlet of the first-stage reverse osmosis mechanism is connected with the second-stage reverse osmosis mechanism, a concentrated water outlet of the second-stage reverse osmosis mechanism is connected with the crystal seed crystallization device, a clear water outlet of the crystal seed crystallization device is connected with the nanofiltration mechanism, a bottom precipitate outlet of the crystal seed crystallization device is connected with the dehydration mechanism, a concentrated water outlet of. The concentration multiple of the system is 50 times, and the water yield reaches 98%. Finally, 2% of residues of the concentrated solution are solidified and then are subjected to landfill treatment, crystallized solid wastes are used as industrial salt dangers, and 98% of clean drainage is carried out.
Description
Technical Field
The invention relates to a treatment system of landfill leachate concentrated solution.
Background
The landfill leachate has the characteristics of large variation of water quality and water quantity, high concentration of organic matters, high content of heavy metal ions, high ammonia nitrogen content, imbalance proportion of water quality nutrient elements, high salt content and the like, so the treatment difficulty of the landfill leachate is high.
The disc tube type reverse osmosis membrane (DTRO) system has the characteristics of wide channel, short flow and turbulence. Because of low requirement on the quality of the inlet water and good treatment effect, the method is widely applied to the treatment of the landfill leachate. The disc tube type reverse osmosis membrane process has good stability, safety and adaptability. Due to the characteristics, the process does not depend on complex pretreatment, and can directly treat the percolate. The DTRO reverse osmosis system can ensure that the outlet water reaches the standard, and the disc-tube reverse osmosis has good adaptability to the percolate of each stage of the landfill.
The disc tube reverse osmosis membrane (DTRO) process has been widely used as an efficient leachate treatment technology. However, DTRO, as a separation technique, produces around 30% concentrate. The DTRO concentrated solution mainly comprises refractory organic matters, ammonia nitrogen, heavy metals and high-valence salts, and is brownish black in color. The concentrated solution has serious threat to surface water, underground water, soil environment and the like and can not be directly discharged into the environment. The following two methods are mainly used for the treatment. The first main stream treatment process of the landfill leachate concentrated solution in the waste incineration power plant is spraying back to a hearth for incineration, however, only part of the concentrated solution can be treated by adopting the method, the spraying back to the hearth for incineration can cause serious fire grate corrosion, ash blockage of a dust remover, dirt blockage of a conical opening and the like, so that equipment needs to be shut down frequently, and the furnace temperature can be reduced by adopting the treatment method, which is very unfavorable for normal operation of the equipment. Secondly, the main stream treatment process of landfill leachate concentrated solution in landfill plants is to recharge the concentrated solution to a landfill body, which causes the salinity of leachate to increase, and the load of a treatment system to increase and even collapse.
Therefore, it is necessary to develop a discharge treatment system for the continuous treatment of the landfill leachate concentrated solution to solve the problem of discharging the landfill leachate concentrated solution.
Disclosure of Invention
The invention provides an efficient treatment system aiming at the characteristics of the DTRO landfill leachate concentrated solution, namely the concentrated solution generated by DTRO treatment of landfill leachate, and realizes near zero emission of the DTRO landfill leachate concentrated solution.
The technical scheme adopted by the invention for solving the problems is as follows: the utility model provides a nearly zero release processing system of DTRO landfill leachate dense liquid, includes one-level reverse osmosis mechanism, drainage reverse osmosis mechanism, second grade reverse osmosis mechanism, seed crystal crystallization device, receives filter mechanism, hydraulic cyclone separation mechanism, filter pressing mechanism, dewatering mechanism, the clear water exit linkage of one-level reverse osmosis mechanism drainage reverse osmosis mechanism, dense water exit linkage second grade reverse osmosis mechanism, the clear water export of drainage reverse osmosis mechanism is as outlet, dense water exit linkage and reverse osmosis mechanism's the incoming water, the clear water exit linkage of second grade reverse osmosis mechanism drainage reverse osmosis mechanism, dense water exit linkage seed crystal crystallization device, the clear water exit linkage of seed crystal crystallization device receive filter mechanism, bottom precipitate exit linkage dewatering mechanism, the clear water exit linkage of receiving filter mechanism second grade reverse osmosis mechanism, dewatering mechanism, The concentrated water outlet is connected with the hydraulic cyclone separation mechanism, the clear water outlet of the hydraulic cyclone separation mechanism is connected with the crystal seed crystallization device and the concentrated water outlet, and the filter pressing liquid outlet of the filter pressing mechanism is connected with the crystal seed crystallization device.
Furthermore, the working pressure of the first-stage reverse osmosis mechanism is greater than that of the drainage reverse osmosis mechanism, and the working pressure of the second-stage reverse osmosis mechanism is greater than that of the first-stage reverse osmosis mechanism. Alternatively, the primary reverse osmosis mechanism is selected from 75-90bar DTRO reverse osmosis membranes, the drain reverse osmosis mechanism is selected from 30-50bar DTRO reverse osmosis membranes, and the secondary reverse osmosis mechanism is selected from 120bar DTRO reverse osmosis membranes.
Preferably, the dewatering structure is selected from a drying and solidifying device or an evaporation seed crystal crystallizing device.
Preferably, the seed crystal crystallization device comprises a seed crystal dosing device, a seed crystal crystallization reactor, a stirrer, a sedimentation tank and a clear liquid discharge pipe. And adding calcium sulfate crystal seeds into the water by a crystal seed adding device. The water and the seed crystal are reacted and crystallized in the seed crystal reactor. The stirrer stirs the crystallization liquid to promote the collision of crystal nuclei, and crystals grow and separate out uniformly. The sedimentation tank is used for solid-liquid separation to obtain a solid phase at the lower layer and a clear liquid at the upper layer.
The implementation method of the processing system comprises the following steps:
s1, collecting the DTRO landfill leachate concentrated solution by using a primary reverse osmosis mechanism, and separating the concentrated solution into 65-75% of clear solution and 25-35% of concentrated solution.
S2, collecting the clear liquid obtained in the step S1 by using a drainage reverse osmosis mechanism, further purifying and separating the clear liquid, enabling the produced water to reach the discharge standard, and enabling the concentrated water to flow back to the first-stage reverse osmosis mechanism to adjust the concentrated liquid of the DTRO landfill leachate, so that the clear water is utilized.
S3, collecting the concentrated solution from S1 by a secondary reverse osmosis mechanism, further concentrating and separating, wherein the secondary reverse osmosis mechanism adopts a batch treatment mode for filtering, the concentration is stopped until the conductance of the concentrated solution reaches over 160000 muS/cm, the recovery rate of the secondary reverse osmosis mechanism is designed to be 50%, and the produced water is conveyed to a drainage reverse osmosis mechanism.
S4 the concentrated solution of step S3 is collected by a seed crystal crystallizing device, because the components of the concentrated solution are complex and the tendency of scaling and fouling is very high. By introducing CaSO4 crystal seed crystallization, calcium ions, sulfate ions in raw water and a large amount of sulfate ions brought in the process of adjusting the pH of the raw solution are mainly separated from the concentrated solution by the crystal seed crystallization, so that the scaling tendency of the concentrated solution is reduced. The seed crystal crystallization is an important crystallization process, the existence of the seed crystal has great influence on the nucleation growth process, and the operation of adding the crystal can lead the precipitation to be carried out under lower supersaturation degree, thus being beneficial to the crystal growth. In order to obtain good precipitation, narrow crystal size distribution and improve the quality of the crystal product, the introduction of seed crystal to induce nucleation or the inhibition of primary nucleation at the early stage of precipitation crystallization is often one of the effective means. In addition, by increasing the pH value of the concentrated solution, a large amount of magnesium ions and a part of organic matters can be removed, and clear liquid and precipitates are obtained.
S5 collecting the clear liquid of step S4 by a nanofiltration mechanism, wherein the nanofiltration mechanism has selective permeability to ions and good removal effect on divalent ions such as calcium, magnesium and sulfate ions. The clear liquid mainly contains monovalent ions, and the scaling tendency of the clear liquid is greatly reduced. Monovalent ions are separated into clear water, divalent ions are left in the concentrated water, the clear water flows back to the second-stage reverse osmosis mechanism to be mixed with the concentrated water of the first-stage reverse osmosis mechanism, the scaling and pollution blocking tendency of the incoming water is reduced, the regulation is mainly to improve the recovery rate of the second-stage reverse osmosis mechanism, and otherwise, the regulation is difficult to realize.
S6, collecting the concentrated water obtained in the step S5 by using a hydraulic cyclone separation mechanism, wherein calcium, magnesium ions and sulfate ions in the concentrated water of the nanofiltration mechanism rise again and tend to be saturated, crystal particles in the concentrated water are separated from the concentrated water through the hydraulic cyclone effect, and clear liquid obtained through separation flows back to the seed crystal crystallization device. The hydrocyclone is a device for separating crystallized particles according to different centrifugal forces applied to the particles with different particle sizes during the rotary motion. After the crystal seeds are crystallized, clear liquid discharged from the sedimentation tank is filtered and concentrated by a nanofiltration mechanism, and calcium, magnesium ions and sulfate ions in the concentrated solution are raised again. By means of the hydrocyclone, the crystal particles in the concentrate, including calcium sulphate, magnesium sulphate and calcium carbonate, are separated due to the centrifugal forces to which they are subjected.
S7, collecting the precipitate separated by the hydraulic cyclone separating mechanism in the step S6 by using a filter pressing mechanism, realizing solid-liquid separation, disposing the produced mud cake as hazardous waste, and refluxing the separated clear liquid to a crystal seed crystallizing device.
S8, collecting the precipitate from the S4 crystal seed crystallizing device by a dewatering mechanism, dewatering the precipitate, concentrating the final 2% residue, solidifying the residue with cement or fly ash and chelating agent, and filling the solidified residue into a landfill.
Compared with the prior art, the invention has the advantages that:
the invention realizes the treatment of the landfill leachate concentrated solution and achieves the aim of near zero emission. The invention aims to treat concentrated liquor generated by treating landfill leachate by DTRO. By combining the primary DTRO, the DTNF, the secondary DTRO, the drained DTRO, the seed crystal reaction precipitation, the hydraulic cyclone separation equipment, the filter pressing mechanism and the dewatering mechanism (evaporation crystallization device), the water yield of about 98 percent is achieved by setting multiple separation processes such as water production circulation, crystallization circulation and the like, and the water yield is the percentage of the drained water in the raw water. The final 2% of the evaporative crystallised residue can be landfilled in landfills by curing with cement or fly ash and a chelating agent.
Compared with a primary reverse osmosis mechanism, the treatment system can improve the recovery rate of the original DTRO system from 70% to 98%, namely the concentration multiple of the system is improved from 3.3 to 50 times, so that the discharge amount of concentrated solution is greatly reduced, the drainage standard is improved, and the harm to the environment is reduced.
Drawings
FIG. 1 is a schematic view of a processing system according to an embodiment of the present invention;
in the figure, a first-stage reverse osmosis mechanism 1, a drainage reverse osmosis mechanism 2, a second-stage reverse osmosis mechanism 3, a nanofiltration mechanism 4, a seed crystal crystallization device 5, a hydraulic cyclone separation mechanism 6, a plate-frame filter pressing mechanism 7 and a dehydration mechanism 8 are arranged, and lines in the figure represent connecting pipelines.
Detailed Description
The present invention will be described in further detail below with reference to the embodiments of the drawings, which are illustrative and intended to be illustrative of the present invention and are not to be construed as limiting the present invention.
The DTRO landfill leachate concentrated solution near-zero emission treatment system of the embodiment comprises a primary reverse osmosis mechanism 1, a drainage reverse osmosis mechanism 2, a secondary reverse osmosis mechanism 3, a crystal seed crystallization device 5, a nanofiltration mechanism 4, a hydraulic cyclone separation mechanism 6, a plate frame filter pressing mechanism 7 and a dehydration mechanism 8.
90bar DTRO is selected to first order reverse osmosis mechanism 1, 50bar DTRO is selected to drainage reverse osmosis mechanism 2, 120bar DTRO is selected to second grade reverse osmosis mechanism 3, 40bar STNF is selected to nanofiltration mechanism 4, seed crystal crystallization device 5 includes seed crystal charge device, seed crystal crystallization reactor, agitator, sedimentation tank and clear liquid discharge pipe, 8 selection evaporation crystallization devices of dewatering mechanism.
The first-stage reverse osmosis mechanism 1 is butted with DTRO landfill leachate concentrated solution, the drainage reverse osmosis mechanism 2 is connected with a clear water outlet of the first-stage reverse osmosis mechanism 1, the second-stage reverse osmosis mechanism 3 is connected with a concentrated water outlet of the first-stage reverse osmosis mechanism 1, a clear water outlet of the drainage reverse osmosis mechanism 2 is directly connected with a drainage pipe to realize clear water drainage, the concentrated water outlet is connected with incoming water of the first-stage reverse osmosis mechanism 1, the clear water outlet of the second-stage reverse osmosis mechanism 3 is connected with the drainage reverse osmosis mechanism 2, the concentrated water outlet is connected with the seed crystal crystallizing device 5, the clear water outlet of the seed crystal crystallizing device 5 is connected with the nanofiltration mechanism 4, the bottom sediment outlet is connected with the dehydration mechanism 8, the clear water outlet of the nanofiltration mechanism 4 is connected with incoming water of the second-stage reverse osmosis mechanism 3, the concentrated water outlet is connected with, the filter pressing liquid outlet of the filter pressing mechanism 7 is connected with the crystal seed crystallizing device 5, and the filter cake is treated as hazardous waste.
The implementation method of the treatment system for near zero emission of the landfill leachate concentrated solution comprises the following steps:
s1 the concentrated DTRO landfill leachate is collected by a primary reverse osmosis mechanism and separated into 70% clear solution and 30% concentrated solution.
S2, collecting the clear liquid obtained in the step S1 by using a drainage reverse osmosis mechanism, further purifying and separating to ensure that the produced water reaches the discharge standard, and returning the concentrated water to the primary reverse osmosis mechanism to adjust the concentrated liquid of the DTRO landfill leachate, thereby realizing the utilization of the clear water.
S3, collecting the concentrated solution from S1 by a secondary reverse osmosis mechanism, further concentrating and separating, wherein the secondary reverse osmosis mechanism adopts a batch treatment mode for filtering, the concentration is stopped until the conductance of the concentrated solution reaches over 160000 muS/cm, the recovery rate of the secondary reverse osmosis mechanism is designed to be 50%, and the produced water is conveyed to a drainage reverse osmosis mechanism.
S4 collecting the concentrated solution from S3 by using a seed crystal crystallizing device, and introducing CaSO into the concentrated solution4Crystal seed crystallization, wherein sulfate ions in the concentrated solution are separated from the concentrated solution by using calcium ions in a crystal seed crystallization mode, so that the scaling tendency is reduced; in addition, the pH value of the concentrated solution is adjusted to 8-12, magnesium ions are removed, and partial organic matters are decomposed to obtain clear liquid and precipitate.
S5, collecting the clear liquid in the step S4 by using a nanofiltration mechanism, separating monovalent ions into clear water by the nanofiltration mechanism according to the selective permeability of the ions, keeping divalent ions in the concentrated water, and returning the clear water to the secondary reverse osmosis mechanism to be mixed with the concentrated water of the primary reverse osmosis mechanism to reduce the scaling and pollution blocking tendency of the incoming water and mainly improve the recovery rate of the secondary reverse osmosis mechanism by regulation, otherwise, the realization is difficult.
S6, collecting the concentrated water obtained in the step S5 by using a hydraulic cyclone separation mechanism, wherein calcium, magnesium ions and sulfate ions in the concentrated water of the nanofiltration mechanism rise again and tend to be saturated, crystal particles in the concentrated water are separated from the concentrated water through the hydraulic cyclone effect, and clear liquid obtained through separation flows back to the seed crystal crystallization device.
S7, collecting the precipitate separated by the hydraulic cyclone separating mechanism in the step S6 by using a filter pressing mechanism, realizing solid-liquid separation, disposing the produced mud cake as hazardous waste, and refluxing the separated clear liquid to a crystal seed crystallizing device.
S8, collecting the precipitate from the S4 crystal seed crystallizing device by a dewatering mechanism, dewatering the precipitate, concentrating the precipitate to 2% of residue, solidifying the residue with cement or fly ash and chelating agent, and filling the residue into a refuse landfill, wherein the concentration multiple of the system reaches 50 times.
The concentration multiple of the system is improved from 3.3 to 50 times, the water yield reaches 98 percent, the discharge amount of concentrated solution is greatly reduced, and the harm to the environment is also reduced. Finally, 2% of residues of the concentrated solution are solidified and then are subjected to landfill treatment, crystallized solid wastes are used as industrial salt dangers, and 98% of clear solution is used as clean drainage.
Although preferred embodiments of the present invention have been described in detail hereinabove, it should be clearly understood that modifications and variations of the present invention are possible to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (9)
1. The utility model provides a nearly zero release processing system of DTRO landfill leachate dense solution which characterized in that: comprises a first-stage reverse osmosis mechanism, a drainage reverse osmosis mechanism, a second-stage reverse osmosis mechanism, a seed crystal crystallization device, a nanofiltration mechanism, a hydraulic cyclone separation mechanism, a filter pressing mechanism and a dehydration mechanism,
the clear water outlet of the first-stage reverse osmosis mechanism is connected with the drainage reverse osmosis mechanism, the concentrated water outlet is connected with the second-stage reverse osmosis mechanism, a clear water outlet of the drainage reverse osmosis mechanism is used as a water outlet, a concentrated water outlet is connected with the water coming from the reverse osmosis mechanism, the clear water outlet of the secondary reverse osmosis mechanism is connected with the drainage reverse osmosis mechanism, the concentrated water outlet is connected with the crystal seed crystallization device, the clear water outlet of the crystal seed crystallization device is connected with the nanofiltration mechanism, the bottom sediment outlet is connected with the dehydration mechanism, the clear water outlet of the nanofiltration mechanism is connected with the secondary reverse osmosis mechanism, the concentrated water outlet is connected with the hydraulic cyclone separation mechanism, the clear water outlet of the hydraulic cyclone separation mechanism is connected with the crystal seed crystallization device, the concentrated water outlet is connected with the filter pressing mechanism, and the filter pressing liquid outlet of the filter pressing mechanism is connected with the crystal seed crystallization device.
2. The DTRO landfill leachate concentrated solution near-zero emission treatment system of claim 1, wherein: the working pressure of the first-stage reverse osmosis mechanism is greater than that of the drainage reverse osmosis mechanism, and the working pressure of the second-stage reverse osmosis mechanism is greater than that of the first-stage reverse osmosis mechanism.
3. The DTRO landfill leachate concentrated solution near-zero emission treatment system of claim 2, wherein: the primary reverse osmosis mechanism is selected from 75-90bar DTRO reverse osmosis membranes, the drainage reverse osmosis mechanism is selected from 30-50bar DTRO reverse osmosis membranes, and the secondary reverse osmosis mechanism is selected from 120bar DTRO reverse osmosis membranes.
4. The DTRO landfill leachate concentrated solution near-zero emission treatment system of claim 1, wherein: the dehydration structure is selected from a drying and solidifying device or an evaporation seed crystal crystallizing device.
5. The DTRO landfill leachate concentrated solution near-zero emission treatment system of claim 1, wherein: the seed crystal crystallization device comprises a seed crystal dosing device, a seed crystal crystallization reactor, a stirrer, a sedimentation tank and a clear liquid discharge pipe.
6. A method for implementing the DTRO landfill leachate concentrated solution near-zero emission treatment system according to any of claims 1-5, wherein the DTRO landfill leachate concentrated solution near-zero emission treatment system comprises:
s1, collecting the DTRO landfill leachate concentrated solution by using a primary reverse osmosis mechanism, and separating the concentrated solution into 65-75% of clear solution and 25-35% of concentrated solution;
s2, collecting the clear liquid obtained in the step S1 by using a drainage reverse osmosis mechanism, further purifying and separating the clear liquid, returning the produced water to a first-stage reverse osmosis mechanism to adjust the DTRO landfill leachate concentrated liquid, and thus realizing the utilization of the clear water;
s3, collecting the concentrated solution obtained in the step S1 by using a secondary reverse osmosis mechanism, further concentrating and separating, wherein the secondary reverse osmosis mechanism adopts a batch treatment mode for filtration, the concentration is stopped until the conductance of the concentrated solution reaches more than 160000 muS/cm, the recovery rate of the secondary reverse osmosis mechanism is designed to be 50%, and the produced water is conveyed to a drainage reverse osmosis mechanism;
s4 collecting the concentrated solution from S3 by using a seed crystal crystallizing device, and introducing CaSO into the concentrated solution4Crystal seed crystallization, wherein sulfate ions in the concentrated solution are separated from the concentrated solution by using calcium ions in a crystal seed crystallization mode, so that the scaling tendency is reduced; in addition, the pH of the concentrated solution is adjusted to remove magnesium ions and decompose partial organic matters to obtain clear liquid and precipitates;
s5, collecting the clear liquid obtained in the step S4 by using a nanofiltration mechanism, separating monovalent ions into clear water by using the nanofiltration mechanism to selectively permeate ions, keeping divalent ions in the concentrated water, and refluxing the clear water to the secondary reverse osmosis mechanism to be mixed with the concentrated water of the primary reverse osmosis mechanism to reduce the scaling and pollution blocking tendency of the incoming water and mainly improve the recovery rate of the secondary reverse osmosis mechanism by adjusting, otherwise, the recovery rate is difficult to realize;
s6, collecting the concentrated water obtained in the step S5 by using a hydraulic cyclone separation mechanism, wherein calcium, magnesium ions and sulfate ions in the concentrated water of the nanofiltration mechanism rise again and tend to be saturated, crystal particles in the concentrated water are separated from the concentrated water through the hydraulic cyclone effect, and clear liquid obtained by separation flows back to the seed crystal crystallization device;
s7, collecting the precipitate separated by the hydraulic cyclone separating mechanism in the step S6 by using a filter pressing mechanism to realize solid-liquid separation, disposing the produced mud cake as hazardous waste, and refluxing the separated clear liquid to a crystal seed crystallizing device;
s8, collecting the precipitate from the S4 crystal seed crystallizing device by a dewatering mechanism, dewatering the precipitate, solidifying the concentrated residue with cement or fly ash and chelating agent, and burying the solidified residue in a landfill.
7. The implementation method according to claim 6, characterized in that: step S4 is to adjust the pH of the concentrated solution to 8-12.
8. The implementation method according to claim 6, characterized in that: in step S6, the residue obtained by concentrating the precipitate to 2% is solidified, i.e. the concentration factor of the system reaches 50 times.
9. The implementation method according to claim 6, characterized in that: in step S1, the primary reverse osmosis mechanism separates the concentrate into 70% clear solution and 30% concentrate.
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| CN112079489A (en) * | 2020-10-09 | 2020-12-15 | 南京九胜揽天科技有限公司 | Reverse osmosis treatment process and device for landfill leachate |
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