CN110655273A - Old refuse landfill leachate treatment system and method - Google Patents
Old refuse landfill leachate treatment system and method Download PDFInfo
- Publication number
- CN110655273A CN110655273A CN201910893718.0A CN201910893718A CN110655273A CN 110655273 A CN110655273 A CN 110655273A CN 201910893718 A CN201910893718 A CN 201910893718A CN 110655273 A CN110655273 A CN 110655273A
- Authority
- CN
- China
- Prior art keywords
- treatment system
- hpro
- stage
- treatment
- permeate
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000011282 treatment Methods 0.000 title claims abstract description 207
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000000149 chemical water pollutant Substances 0.000 title claims description 12
- ONIBWKKTOPOVIA-UHFFFAOYSA-N Proline Chemical compound OC(=O)C1CCCN1 ONIBWKKTOPOVIA-UHFFFAOYSA-N 0.000 claims abstract description 76
- 239000012466 permeate Substances 0.000 claims abstract description 67
- 239000007788 liquid Substances 0.000 claims abstract description 59
- 238000001704 evaporation Methods 0.000 claims abstract description 52
- 230000008020 evaporation Effects 0.000 claims abstract description 49
- 239000012528 membrane Substances 0.000 claims abstract description 39
- 238000007711 solidification Methods 0.000 claims abstract description 27
- 230000008023 solidification Effects 0.000 claims abstract description 27
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 22
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 22
- 230000001105 regulatory effect Effects 0.000 claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 61
- 239000000243 solution Substances 0.000 claims description 45
- 238000012545 processing Methods 0.000 claims description 29
- 239000012452 mother liquor Substances 0.000 claims description 20
- 239000012530 fluid Substances 0.000 claims description 19
- 239000003795 chemical substances by application Substances 0.000 claims description 17
- 239000010813 municipal solid waste Substances 0.000 claims description 17
- 238000002156 mixing Methods 0.000 claims description 15
- 239000012141 concentrate Substances 0.000 claims description 14
- 238000005273 aeration Methods 0.000 claims description 13
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 10
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 10
- 239000004568 cement Substances 0.000 claims description 10
- 239000004571 lime Substances 0.000 claims description 10
- 230000000149 penetrating effect Effects 0.000 claims description 10
- 238000011001 backwashing Methods 0.000 claims description 9
- 150000003568 thioethers Chemical class 0.000 claims description 9
- 239000010802 sludge Substances 0.000 claims description 8
- 239000010413 mother solution Substances 0.000 claims description 7
- 239000000047 product Substances 0.000 claims description 7
- 238000007872 degassing Methods 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 2
- 238000005457 optimization Methods 0.000 claims description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 20
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 abstract description 13
- 238000001179 sorption measurement Methods 0.000 abstract description 9
- 239000011347 resin Substances 0.000 abstract description 7
- 229920005989 resin Polymers 0.000 abstract description 7
- 230000007797 corrosion Effects 0.000 abstract description 5
- 238000005260 corrosion Methods 0.000 abstract description 5
- 238000004065 wastewater treatment Methods 0.000 abstract description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 20
- 229910052757 nitrogen Inorganic materials 0.000 description 10
- 230000002829 reductive effect Effects 0.000 description 9
- 230000000694 effects Effects 0.000 description 7
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 239000002253 acid Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 3
- BUGBHKTXTAQXES-UHFFFAOYSA-N Selenium Chemical compound [Se] BUGBHKTXTAQXES-UHFFFAOYSA-N 0.000 description 3
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 3
- 229910052785 arsenic Inorganic materials 0.000 description 3
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 229910052788 barium Inorganic materials 0.000 description 3
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 3
- 229910052790 beryllium Inorganic materials 0.000 description 3
- ATBAMAFKBVZNFJ-UHFFFAOYSA-N beryllium atom Chemical compound [Be] ATBAMAFKBVZNFJ-UHFFFAOYSA-N 0.000 description 3
- 229910052804 chromium Inorganic materials 0.000 description 3
- 239000011651 chromium Substances 0.000 description 3
- JOPOVCBBYLSVDA-UHFFFAOYSA-N chromium(6+) Chemical compound [Cr+6] JOPOVCBBYLSVDA-UHFFFAOYSA-N 0.000 description 3
- 229910052802 copper Inorganic materials 0.000 description 3
- 239000010949 copper Substances 0.000 description 3
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 3
- 229910052753 mercury Inorganic materials 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000000465 moulding Methods 0.000 description 3
- 229910052759 nickel Inorganic materials 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 238000001223 reverse osmosis Methods 0.000 description 3
- 229910052711 selenium Inorganic materials 0.000 description 3
- 239000011669 selenium Substances 0.000 description 3
- 229910052709 silver Inorganic materials 0.000 description 3
- 239000004332 silver Substances 0.000 description 3
- 239000011701 zinc Substances 0.000 description 3
- 229910052725 zinc Inorganic materials 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 239000012459 cleaning agent Substances 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 230000000670 limiting effect Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 239000002033 PVDF binder Substances 0.000 description 1
- 239000002518 antifoaming agent Substances 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003729 cation exchange resin Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000012510 hollow fiber Substances 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- 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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
-
- 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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The invention belongs to the field of wastewater treatment, and relates to a percolate treatment system for an old refuse landfill.A regulating tank is communicated with a liquid inlet of an MBR treatment system, and a permeate outlet of the MBR treatment system is communicated with a two-stage DTRO treatment system; the concentrated solution outlet of the two-stage DTRO treatment system is communicated with the liquid inlet of the HPRO treatment system; a permeate outlet and a concentrated solution outlet of the HPRO treatment system are respectively communicated with the permeate treatment system and the evaporation system; the invention also provides a treatment method of the percolate, the percolate is sequentially treated by the MBR treatment system, the two-stage DTRO treatment system and the HPRO treatment system, the obtained concentrated solution is safely buried after being treated by the evaporation system, and the permeate is discharged after reaching the standard after being sequentially treated by the two-stage RO treatment system and the ion exchange resin device. The invention realizes the full-scale treatment of the percolate through multi-stage membrane treatment, evaporation, solidification and resin adsorption, and solves the problems of high sulfide, high ammonia nitrogen, high conductivity, serious corrosion of power equipment and electrical elements and the like of the prior percolate.
Description
Technical Field
The invention belongs to the technical field of wastewater treatment, and particularly relates to a system and a method for treating percolate of an old refuse landfill.
Background
The old refuse landfill has bad water quality, high COD, high ammonia nitrogen, high conductivity and high sulfide due to long-term membrane concentrate recharging, and has poor stability and low permeate rate by adopting the common biochemical and membrane treatment process, and the membrane concentrate is not solved all the time. On the other hand, at present, a plurality of landfill sites and leachate regulating tanks adopt a film covering process, the quality of leachate water sulfides also gradually rise, and the sulfides which are continuously accumulated are harmful to human bodies, seriously corrode power equipment and electrical elements and cause the system to be incapable of normally operating. Therefore, it is necessary to design a leachate treatment system and method for old landfill sites according to the water quality characteristics and the current operating conditions of the old landfill sites.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention aims to provide a system and a method for treating percolate of an old refuse landfill, which can realize the full-quantitative treatment of membrane concentrated solution and sulfide of the old refuse landfill.
In order to achieve the purpose, the technical scheme of the invention is a percolate treatment system of an old refuse landfill, which comprises a regulating tank, an MBR treatment system, a two-stage DTRO treatment system, an HPRO treatment system, an evaporation system and a permeate treatment system; the regulating tank is communicated with a liquid inlet of the MBR treatment system, and a permeate outlet of the MBR treatment system is communicated with a liquid inlet of the two-stage DTRO treatment system; a concentrated solution outlet of the two-stage DTRO treatment system is communicated with a liquid inlet of the HPRO treatment system; and a permeate outlet of the HPRO treatment system is communicated with the permeate treatment system, and a concentrate outlet of the HPRO treatment system is communicated with the evaporation system.
Furthermore, permeate liquid processing system includes two-stage RO processing system, HPRO processing system's permeate liquid export with evaporating system's evaporation effluent export all with two-stage RO processing system's inlet intercommunication, two-stage RO processing system's concentrate export with HPRO processing system's inlet intercommunication.
Furthermore, the permeate liquid treatment system also comprises an ion exchange resin device, and the permeate liquid outlet of the two-stage RO treatment system is communicated with the liquid inlet of the ion exchange resin device.
Further, the evaporation system comprises an evaporator and a solidification device, a concentrated solution outlet of the HPRO treatment system is communicated with a liquid inlet of the evaporator, an evaporation water outlet of the evaporator is communicated with a liquid inlet of the two-stage RO treatment system, and an evaporation mother solution outlet of the evaporator is communicated with the solidification device.
Furthermore, the curing device comprises a mixing stirrer and a curing agent bin, and the curing agent bin and an evaporation mother liquor outlet of the evaporator are connected with the mixing stirrer.
Further, the two-stage DTRO treatment system comprises a one-stage DTRO treatment unit and a two-stage DTRO treatment unit, wherein a permeate liquid outlet of the MBR treatment system is communicated with a liquid inlet of the one-stage DTRO treatment unit, a permeate liquid outlet of the one-stage DTRO treatment unit is communicated with a liquid inlet of the two-stage DTRO treatment unit, and a concentrate liquid outlet of the one-stage DTRO treatment unit is communicated with a concentrate liquid outlet of the two-stage DTRO treatment unit and is communicated with a liquid inlet of the HPRO treatment system.
Further, the MBR treatment system comprises an MBR reaction tank, an aeration device, a sludge discharge device and a backwashing device, wherein the aeration device is communicated with the MBR reaction tank through an aeration pipe, and the sludge discharge device is communicated with the bottom of the MBR reaction tank; and an MBR membrane module is arranged in the MBR reaction tank, and the backwashing device is connected with the MBR membrane module.
The invention also provides a method for treating the percolate of the old refuse landfill, which comprises the following steps:
1) the leachate of the regulating tank enters an MBR treatment system, sulfides are separated out by the MBR treatment system and are discharged, and MBR permeate is obtained;
2) the MBR penetrating fluid enters a two-stage DTRO treatment system for treatment to obtain DTRO penetrating fluid and DTRO concentrated fluid, and the DTRO penetrating fluid is treated by a degassing tower and then discharged after reaching the standard;
3) the DTRO concentrated solution enters an HPRO treatment system for treatment to obtain HPRO permeate solution and HPRO concentrated solution, the HPRO concentrated solution enters an evaporator of an evaporation system for further concentration to obtain evaporated water and evaporated mother liquor, the evaporated mother liquor enters a solidification device of the evaporation system for solidification, and the obtained solidified product is safely buried;
4) the HPRO permeate and the evaporated effluent enter a two-stage RO treatment system for further optimization to obtain RO permeate and RO concentrated solution, and the RO concentrated solution returns to the HPRO treatment system for treatment again;
5) and treating the RO permeate by adopting an ion exchange resin device, and then discharging the treated RO permeate after reaching the standard.
Further, in the step 3), before the DTRO concentrated solution enters the HPRO treatment system, the pH value of the DTRO concentrated solution is adjusted to 4-6, and then the DTRO concentrated solution enters the HPRO treatment system for HPRO treatment.
Further, in the step 3), evaporating the mother liquor, feeding the mother liquor into a mixing stirrer of a curing device, and adding a curing agent for curing; the curing agent comprises cement and lime, and the adding ratio of the cement to the lime is 0.1-0.5: 1.
compared with the prior art, the invention has the following beneficial effects:
(1) the system and the method for treating the percolate of the old refuse landfill can solve the problems of high percolate sulfide, poor system stability, serious corrosion of power equipment and electrical elements and the like of the current old landfill, the water yield of the system is up to 90-96 percent, and the system is a full-scale treatment process;
(2) the system and the method for treating the percolate of the old refuse landfill do not comprise a biochemical treatment system, have small floor area and quick start, and are suitable for treating the percolate of the old refuse landfill;
(3) according to the invention, sulfides in the leachate are separated by the MBR treatment system, and then the sulfides remaining in the produced water are removed by the two-stage RO treatment system, so that the harm to human bodies and the corrosion to power equipment and electrical elements are reduced, and the stability of the equipment is improved;
(4) the invention reduces COD and ammonia nitrogen in the produced water through the multi-stage membrane treatment, and adsorbs the ammonia nitrogen and total nitrogen in the produced water through the ion exchange resin device after the multi-stage membrane treatment, thereby ensuring that the effluent reaches the discharge standard.
(5) The evaporation system adopted by the invention has high water yield, large concentration multiple, difficult scaling and stable operation.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic view of a leachate treatment system for an aged landfill site provided in an embodiment of the present invention;
in the figure: 1. a regulating tank, 2, an MBR treatment system, 3, a two-stage DTRO treatment system, 4, an HPRO treatment system, 5, an evaporator, 6, a solidification device, 7, a two-stage RO treatment system, 8, and an ion exchange resin device.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it is to be understood that the terms "center", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", 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, and do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and thus, are not to be construed as limiting the present invention.
The terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature; in the description of the present invention, "a plurality" means two or more unless otherwise specified.
Example 1
As shown in fig. 1, the present embodiment provides a leachate treatment system for an old landfill, which includes a regulating tank 1, an MBR treatment system 2, a two-stage DTRO treatment system 3, an HPRO treatment system 4, an evaporation system, and a permeate treatment system; the regulating tank 1 is communicated with a liquid inlet of the MBR treatment system 2, and a permeate outlet of the MBR treatment system 2 is communicated with a liquid inlet of the two-stage DTRO treatment system 3; the concentrated solution outlet of the two-stage DTRO treatment system 3 is communicated with the liquid inlet of the HPRO treatment system 4; the permeate outlet of the HPRO treatment system 4 is in communication with the permeate treatment system, and the concentrate outlet of the HPRO treatment system 4 is in communication with the evaporation system. The embodiment aims at the membrane concentrated solution recharge, high sulfide, increasingly poor system stability and serious equipment corrosion of the old landfill, improves the full-scale treatment system of the old landfill leachate, can reduce COD, ammonia nitrogen, sulfide and the like in produced water through multi-stage membrane treatment and a permeate liquid treatment system, solves the problems of high sulfide, poor system stability, serious corrosion of power equipment and electrical elements and the like of the old landfill leachate at present, has the water production rate of up to 90-96 percent, does not contain a biochemical treatment system, has small floor area and quick start, and is suitable for the old landfill leachate treatment.
Specifically, the permeate treatment system in this embodiment includes a two-stage RO treatment system 7, the permeate outlet of the HPRO treatment system 4 and the evaporated water outlet of the evaporation system are both communicated with the liquid inlet of the two-stage RO treatment system 7, and the concentrate outlet of the two-stage RO treatment system 7 is communicated with the liquid inlet of the HPRO treatment system 4. The two-stage RO treatment system 7 comprises a first-stage RO treatment unit and a second-stage RO treatment unit, wherein a permeate outlet of the HPRO treatment system and an evaporated water outlet of the evaporation system are both communicated with a liquid inlet of the first-stage RO treatment unit, a concentrated liquid outlet of the first-stage RO treatment unit is communicated with a liquid inlet of the second-stage RO treatment unit, and a permeate outlet of the second-stage RO treatment unit is communicated with a liquid inlet of the ion exchange resin device; and the concentrated solution outlet of the first-stage RO treatment unit and the concentrated solution outlet of the second-stage RO treatment unit are both communicated with the liquid inlet of the HPRO treatment system. The two-stage RO processing system 7 of the present embodiment may be a two-stage MTRO or a two-stage DTRO. Optimally, the permeate liquid treatment system further comprises an ion exchange resin device 8, the permeate liquid outlet of the secondary RO treatment unit is communicated with the liquid inlet of the ion exchange resin device 8, the ion exchange resin device 8 can adsorb ammonia nitrogen and total nitrogen in the effluent water, and the effluent water quality is further ensured to reach the discharge standard. The ion exchange system in the ion exchange resin device 8 selects strong acid cation exchange resin with strong selectivity to ammonia nitrogen, has the advantages of strong adsorption capacity, good selectivity, simple equipment, low cost and the like, can effectively remove the residual ammonia nitrogen intercepted by the front-end membrane, and ensures that the effluent of the system meets the requirements. In addition, the ion exchange resin device 8 can also be provided with a regeneration device and a backwashing device, and the backwashing device regularly backwashes the resin to ensure the adsorption effect; when the adsorption effect is continuously reduced, the adsorption capacity of the resin is restored by the regeneration device.
Specifically, the evaporation system in the embodiment comprises an evaporator 5 and a solidification device 6, wherein a concentrated solution outlet of an HPRO treatment system 4 is communicated with a liquid inlet of the evaporator 5, an evaporation water outlet of the evaporator 5 is communicated with a liquid inlet of a two-stage RO treatment system 7, and an evaporation mother solution outlet of the evaporator 5 is communicated with the solidification device 6, the evaporator of the embodiment can adopt an MVR evaporator, a low-temperature evaporator and the like, furthermore, the solidification device 6 comprises a mixing stirrer and a solidification agent bin, the solidification agent bin and the evaporation mother solution outlet of the evaporator 5 are both connected with the mixing stirrer, the solidification agent and the evaporation mother solution are fully mixed and stirred in the mixing stirrer, the mixing and stirring are generally 5 ~ 30 minutes, the solidification time is shortest, the chemical usage amount is minimum, the leaching rate is minimum, the solidification agent is generally cement and lime, the adding ratio is 0.1-0.1: 1, the solidified product is packaged and then safely filled, and the evaporation system is further provided with an antifoaming agent adding device, an acid adding machine, a packaging machine, a cleaning agent and the like are respectively, and a cleaning agent are configured for periodic backwashing.
Specifically, the two-stage DTRO processing system 3 in this embodiment includes a first-stage DTRO processing unit and a second-stage DTRO processing unit, the permeate outlet of the MBR processing system 2 is communicated with the liquid inlet of the first-stage DTRO processing unit, the permeate outlet of the first-stage DTRO processing unit is communicated with the liquid inlet of the second-stage DTRO processing unit, and the concentrate outlet of the first-stage DTRO processing unit and the concentrate outlet of the second-stage DTRO processing unit are both communicated with the liquid inlet of the HPRO processing system 4. Optimally, a permeate liquid outlet of the secondary DTRO treatment unit is communicated with an inlet of the degassing tower, and permeate liquid treated by the secondary DTRO treatment unit is treated by the degassing tower and then is discharged after reaching the standard. The two-stage DTRO treatment system 3 further comprises a sand-containing filter tank, an acid adjusting device and a security filter, wherein the acid adjusting device adjusts the pH value of the DTRO concentrated solution. The sand filter tank can intercept large particles, the filtering precision is 50 mu m, and colloidal particles and high molecular organic matters can be effectively removed. The precision of the cartridge filter filtration is 10 μm to provide a final protective barrier for the membrane column.
Specifically, the MBR treatment system 2 in the embodiment is an MBR treatment system, and the hydraulic retention time is 0.5-3 hours; the MBR treatment system 2 comprises an MBR reaction tank, an aeration device, a sludge discharge device and a backwashing device, wherein an MBR membrane component is arranged in the MBR reaction tank, and the MBR membrane component adopts a hollow fiber membrane, which can be a PTEF membrane, a PVDF membrane and the like; the aeration device is communicated with the MBR reaction tank through an aeration pipe, and the sludge discharge device is communicated with the bottom of the MBR reaction tank; the aeration device can keep certain dissolved oxygen in the MBR reaction tank, so that sulfides are converted into elemental sulfur, the elemental sulfur is intercepted through the interception effect of the MBR membrane module, the separation of the sulfides is realized, and the intercepted elemental sulfur is discharged out of the system through the sludge discharge device; and the backwashing device is connected with the MBR membrane component, and is started to backwash the MBR membrane component after the membrane flux of the MBR membrane component is reduced, so that the MBR membrane component is recovered to the maximum flux.
As shown in fig. 1, this embodiment further provides a method for treating leachate from an old landfill, which includes the following steps:
1) the leachate of the regulating tank 1 firstly enters an MBR (membrane bioreactor) treatment system 2 through a lift pump, sulfides are converted into elemental sulfur through the MBR treatment system 2, the elemental sulfur is separated out through the interception effect of an MBR membrane component, and the elemental sulfur is discharged out of the MBR treatment system 2 through a sludge discharge device to obtain MBR permeate;
2) the MBR penetrating fluid enters a two-stage DTRO treatment system 3 for treatment to obtain DTRO penetrating fluid and DTRO concentrated fluid, and the DTRO penetrating fluid is treated by a degassing tower and then discharged after reaching the standard;
specifically, the two-stage DTRO treatment system 3 comprises a first-stage DTRO treatment unit and a second-stage DTRO treatment unit, MBR penetrating fluid is firstly treated in the first-stage DTRO treatment unit to obtain first-stage DTRO permeating fluid and first-stage DTRO concentrated fluid, the first-stage DTRO permeating fluid is treated in the second-stage DTRO treatment unit to obtain second-stage DTRO permeating fluid and second-stage DTRO concentrated fluid, and the second-stage DTRO permeating fluid is treated by a degassing tower and then is discharged after reaching the standard; the water yield of the primary DTRO is 70-80%, the operation pressure of the operation pressure is 0-100 bar, the water yield of the secondary DTRO is 80-90%, and the operation pressure of the operation pressure is 0-100 bar;
3) the primary DTRO concentrated solution and the secondary DTRO concentrated solution enter an HPRO treatment system 4 for treatment to obtain HPRO permeate liquid and HPRO concentrated solution, the water yield of the HPRO is 40-60%, and the operating pressure is 0-120 bar; the HPRO concentrated solution enters an evaporator 5 of an evaporation system for further concentration to obtain evaporation effluent water and evaporation mother liquor, the evaporation mother liquor enters a solidification device 6 of the evaporation system for solidification, and the obtained solidified product is safely buried; the water yield of the evaporation system is 70-90%, and the water content of the mother liquor is about 40-60%;
4) the HPRO permeate and the evaporated effluent still contain partial COD, ammonia nitrogen, sulfide and other substances, in order to make the effluent reach the standard, the HPRO permeate and the evaporated effluent are pumped into a two-stage RO treatment system 7 for further optimizing the effluent, the two-stage RO treatment system 7 can intercept macromolecular substances, the COD is reduced to be below 60mg/L, RO permeate and RO concentrate are obtained, and the RO concentrate returns to the HPRO treatment system 4 for treatment again; the water yield of the two-stage RO is 80-90%, and the operating pressure is 0-100 bar;
5) in order to ensure that the effluent further reaches the standard, an ion exchange resin device 8 is adopted to adsorb ammonia nitrogen and total nitrogen in the RO permeate liquid, so that the water is discharged after meeting the requirement. Specifically, according to the field operation condition, if the ammonia nitrogen is high, the ion exchange resin device 8 prepares an ammonia nitrogen adsorption resin tank; if the total nitrogen is high, the ion exchange resin device 8 prepares a total nitrogen adsorption resin tank; in addition, the ion exchange resin device 8 can also be used for simultaneously preparing an ammonia nitrogen adsorption resin tank and a total nitrogen adsorption resin tank.
Optimally, in the step 3), as the alkalinity and hardness of the DTRO concentrated solution are higher, in order to ensure that the HPRO treatment system operates more stably, an acid adding device is arranged in the two-stage DTRO treatment system 3, hydrochloric acid is added before the DTRO concentrated solution enters the HPRO treatment system 4 to adjust the pH value of the DTRO concentrated solution to 4-6, and then the DTRO concentrated solution enters the HPRO treatment system 4 to perform HPRO treatment, so that the water yield is improved, the membrane pollution and the membrane cleaning frequency are reduced, and the ammonia nitrogen concentration of effluent is reduced.
Optimally, in the step 3), the evaporation mother liquor enters a mixing stirrer of the curing device 6, and curing agent is added into the mixing stirrer for curing; the curing agent comprises cement and lime, and the adding ratio of the cement to the lime is 0.1-0.5: 1.
example 2
A domestic garbage landfill site in Hubei province belongs to old garbage landfill sites, and the garbage leachate of the landfill site has the following water quality:
as can be seen from Table 1, the landfill leachate has high COD, high ammonia nitrogen, high conductivity and high sulfide content, and is difficult to reach the standard by adopting the conventional biochemical treatment and membrane treatment process.
The processing system and the method provided by the embodiment 1 of the invention are adopted for processing:
firstly, the landfill leachate of a regulating tank 1 enters an MBR (membrane bioreactor) treatment system 2 through a lift pump, the sulfide of the effluent is reduced to be below 10mg/L through an aeration device and a membrane separation effect, the MBR permeate enters a two-stage DTRO treatment system 3, the water yield of the first stage DTRO is 80%, the operating pressure is 50bar, the water yield of the second stage DTRO is 90%, and the operating pressure is 30 bar; then, the DTRO concentrated solution enters an HPRO treatment system 4, the HPRO permeate enters a two-stage MTRO treatment system, the water yield of the HPRO is 50%, and the operating pressure is 100 bar; the HPRO concentrated solution enters a low-temperature evaporation system for further concentration, the evaporated water enters a two-stage MTRO treatment system, the evaporated mother liquor enters solidification equipment, the water yield of the evaporation system is 90%, and the water content of the mother liquor is about 50%; the HPRO permeate and the evaporated effluent enter two-stage MTRO reverse osmosis treatment, the water production rate of the MTRO is 88 percent, the operating pressure is 20bar, and in order to ensure that the effluent further reaches the standard, the HPRO produced water is treated by ion exchange resin, the COD (chemical oxygen demand) of the effluent reaches 8.8mg/L, the ammonia nitrogen reaches 1.24mg/L, the total nitrogen reaches 12.4mg/L, which is far lower than the second requirement of the pollution control standard (GB 16889-2008) of a domestic garbage landfill; the low-temperature evaporation mother liquor enters curing equipment for curing, cement and lime are adopted as curing agents, and the adding ratio is 0.4: 1, after mixing and stirring for 20 minutes generally, conveying the mixture to a mold through a conveyor for solidification and molding; the water content of the cured product is 27 percent, the total copper is 0.01mg/L, the total zinc is 0.005mg/L, the total lead is 0.05mg/L, the total chromium is 0.05mg/L, the hexavalent chromium is 0.004mg/L, the mercury is 0.02ug/L, the beryllium is 0.1ug/L, the barium is not detected, the total nickel is 0.04mg/L, the silver is 0.01mg/L, the total arsenic is 0.1ug/L, the selenium is 0.2ug/L, and the water content is far lower than the requirement of the pollution control standard of a domestic garbage landfill (GB 16889-2008) table.
Example 3
A certain household garbage landfill in Henan province belongs to old garbage landfill, and the garbage leachate of the landfill has the following water quality:
as can be seen from Table 2, the landfill leachate has high COD, high ammonia nitrogen, high sulfide and high conductivity, and is difficult to reach the standard by adopting the conventional biochemical treatment and membrane treatment process.
The processing system and the method provided by the embodiment 1 of the invention are adopted for processing:
firstly, the landfill leachate of a regulating tank 1 enters an MBR (membrane bioreactor) treatment system 2 through a lift pump, the sulfide of the effluent is reduced to be below 5mg/L through an aeration device and a membrane separation effect, the MBR permeate enters a two-stage DTRO treatment system 3, the water yield of the first stage DTRO is 75%, the operating pressure is 45bar, the water yield of the second stage DTRO is 85%, and the operating pressure is 30 bar; then, the DTRO concentrated solution enters an HPRO treatment system 4, the HPRO permeate enters a two-stage MTRO treatment system, the water yield of the HPRO is 45%, and the operating pressure is 100 bar; the HPRO concentrated solution enters a low-temperature evaporation system for further concentration, the evaporated water enters a two-stage MTRO treatment system, the evaporated mother liquor enters solidification equipment, the water yield of the evaporation system is 85 percent, and the water content of the mother liquor is about 50 percent; the HPRO permeate and the evaporated effluent enter two-stage DTRO reverse osmosis treatment, the water yield of the MTRO is 90%, the operating pressure is 30bar, in order to ensure that the effluent further reaches the standard, the water produced by the MTRO is treated by ion exchange resin, the COD (chemical oxygen demand) of the effluent reaches 5.19mg/L, the ammonia nitrogen reaches 3.34mg/L, the total nitrogen reaches 12.4mg/L, and the total nitrogen is far lower than the second requirement of the pollution control standard of a domestic garbage landfill (GB 16889-2008); the low-temperature evaporation mother liquor enters curing equipment for curing, cement and lime are adopted as curing agents, and the adding ratio is 0.3: 1, after mixing and stirring for 15 minutes generally, conveying the mixture to a mold through a conveyor for solidification and molding; the water content of the cured product is 29 percent, the total copper is 0.04mg/L, the total zinc is 0.002mg/L, the total lead is 0.05mg/L, the total chromium is 0.07mg/L, the hexavalent chromium is 0.006mg/L, the mercury is 0.01ug/L, the beryllium is 0.1ug/L, the barium is not detected, the total nickel is 0.02mg/L, the silver is 0.02mg/L, the total arsenic is 0.2ug/L, the selenium is 0.1ug/L, and the water content is far lower than the requirement of the pollution control standard of the domestic garbage landfill (GB 16889-2008) table.
Example 4
A household garbage landfill in inner Mongolia province belongs to old garbage landfill, and the garbage leachate of the garbage landfill has the following water quality:
as can be seen from Table 3, the landfill leachate has high COD, high ammonia nitrogen and high conductivity, and is difficult to reach the standard by adopting the conventional biochemical treatment and membrane treatment process.
The processing system and the method provided by the embodiment 1 of the invention are adopted for processing:
firstly, the landfill leachate of a regulating tank 1 enters an MBR (membrane bioreactor) treatment system 2 through a lift pump, the sulfide of the effluent is reduced to be below 5mg/L through an aeration device and a membrane separation effect, the MBR permeate enters a two-stage DTRO treatment system 3, the water yield of the first-stage DTRO is 70%, the operating pressure is 50bar, the water yield of the second-stage DTRO is 89%, and the operating pressure is 35 bar; then, the DTRO concentrated solution enters an HPRO treatment system 4, the HPRO permeate enters a two-stage MTRO treatment system, the water yield of the HPRO is 47%, and the operating pressure is 110 bar; the HPRO concentrated solution enters an MVR evaporation system for further concentration, the evaporated water enters a two-stage MTRO treatment system, the evaporated mother solution enters solidification equipment, the water yield of the evaporation system is 90%, and the water content of the mother solution is about 45%; the HPRO permeate and the evaporated effluent enter two-stage MTRO reverse osmosis treatment, the water yield of the MTRO is 90%, the operating pressure is 32bar, and in order to ensure that the effluent further reaches the standard, the water produced by the MTRO is treated by ion exchange resin; COD of the effluent reaches 7.51mg/L, ammonia nitrogen reaches 2.22mg/L, and total nitrogen reaches 10.4mg/L, which is far lower than the requirements of table two of the pollution control standards of municipal solid waste landfill (GB 16889-2008); the low-temperature evaporation mother liquor enters curing equipment for curing, cement and lime are adopted as curing agents, and the adding ratio is 0.3: 1, after mixing and stirring for 20 minutes generally, conveying the mixture to a mold through a conveyor for solidification and molding; the water content of the cured product is 28 percent, the total copper is 0.02mg/L, the total zinc is 0.004mg/L, the total lead is 0.05mg/L, the total chromium is 0.05mg/L, the hexavalent chromium is 0.007mg/L, the mercury is 0.01ug/L, the beryllium is 0.1ug/L, the barium is not detected, the total nickel is 0.02mg/L, the silver is 0.02mg/L, the total arsenic is 0.2ug/L, the selenium is 0.1ug/L, and the water content is far lower than the requirement of the pollution control standard of a domestic garbage landfill (GB 16889-2008) table.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (10)
1. The utility model provides an old garbage landfill leachate treatment system which characterized in that: comprises a regulating tank, an MBR treatment system, a two-stage DTRO treatment system, an HPRO treatment system, an evaporation system and a permeate treatment system; the regulating tank is communicated with a liquid inlet of the MBR treatment system, and a permeate outlet of the MBR treatment system is communicated with a liquid inlet of the two-stage DTRO treatment system; a concentrated solution outlet of the two-stage DTRO treatment system is communicated with a liquid inlet of the HPRO treatment system; and a permeate outlet of the HPRO treatment system is communicated with the permeate treatment system, and a concentrate outlet of the HPRO treatment system is communicated with the evaporation system.
2. The leachate treatment system of old landfill as claimed in claim 1, wherein: permeate liquid processing system includes two-stage RO processing system, HPRO processing system's permeate liquid export and evaporating system's evaporation effluent export all with two-stage RO processing system's inlet intercommunication, two-stage RO processing system's concentrate export with HPRO processing system's inlet intercommunication.
3. The leachate treatment system of old landfill as claimed in claim 2, wherein: the permeate liquid treatment system further comprises an ion exchange resin device, and the permeate liquid outlet of the two-stage RO treatment system is communicated with the liquid inlet of the ion exchange resin device.
4. The leachate treatment system of old landfill as claimed in claim 1, wherein: the evaporation system comprises an evaporator and a solidification device, the concentrated solution outlet of the HPRO treatment system is communicated with the liquid inlet of the evaporator, the evaporation water outlet of the evaporator is communicated with the liquid inlet of the two-stage RO treatment system, and the evaporation mother solution outlet of the evaporator is communicated with the solidification device.
5. The leachate treatment system of old refuse landfill of claim 4, wherein: the solidification device comprises a mixing stirrer and a curing agent bin, and evaporation mother liquor outlets of the curing agent bin and the evaporator are connected with the mixing stirrer.
6. The leachate treatment system of old landfill as claimed in claim 1, wherein: the two-stage DTRO treatment system comprises a one-stage DTRO treatment unit and a two-stage DTRO treatment unit, wherein a permeate liquid outlet of the MBR treatment system is communicated with a liquid inlet of the one-stage DTRO treatment unit, a permeate liquid outlet of the one-stage DTRO treatment unit is communicated with a liquid inlet of the two-stage DTRO treatment unit, and a concentrated liquid outlet of the one-stage DTRO treatment unit is communicated with a concentrated liquid outlet of the two-stage DTRO treatment unit and is communicated with a liquid inlet of the HPRO treatment system.
7. The leachate treatment system of old landfill as claimed in claim 1, wherein: the MBR treatment system comprises an MBR reaction tank, an aeration device, a sludge discharge device and a backwashing device, wherein the aeration device is communicated with the MBR reaction tank through an aeration pipe, and the sludge discharge device is communicated with the bottom of the MBR reaction tank; and an MBR membrane module is arranged in the MBR reaction tank, and the backwashing device is connected with the MBR membrane module.
8. A method for treating percolate of an old refuse landfill is characterized by comprising the following steps:
1) the leachate of the regulating tank enters an MBR treatment system, sulfides are separated out by the MBR treatment system and are discharged, and MBR permeate is obtained;
2) the MBR penetrating fluid enters a two-stage DTRO treatment system for treatment to obtain DTRO penetrating fluid and DTRO concentrated fluid, and the DTRO penetrating fluid is treated by a degassing tower and then discharged after reaching the standard;
3) the DTRO concentrated solution enters an HPRO treatment system for treatment to obtain HPRO permeate solution and HPRO concentrated solution, the HPRO concentrated solution enters an evaporator of an evaporation system for further concentration to obtain evaporated water and evaporated mother liquor, the evaporated mother liquor enters a solidification device of the evaporation system for solidification, and the obtained solidified product is safely buried;
4) the HPRO permeate and the evaporated effluent enter a two-stage RO treatment system for further optimization to obtain RO permeate and RO concentrated solution, and the RO concentrated solution returns to the HPRO treatment system for treatment again;
5) and treating the RO permeate by adopting an ion exchange resin device, and then discharging the treated RO permeate after reaching the standard.
9. The method for treating leachate from old refuse landfills according to claim 8, wherein the method comprises the following steps: in the step 3), before the DTRO concentrated solution enters an HPRO treatment system, the pH value of the DTRO concentrated solution is adjusted to 4-6, and then the DTRO concentrated solution enters the HPRO treatment system for HPRO treatment.
10. The method for treating leachate from old refuse landfills according to claim 8, wherein the method comprises the following steps: in the step 3), the evaporation mother liquor enters a mixing stirrer of a curing device, and a curing agent is added for curing; the curing agent comprises cement and lime, and the adding ratio of the cement to the lime is 0.1-0.5: 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910893718.0A CN110655273A (en) | 2019-09-20 | 2019-09-20 | Old refuse landfill leachate treatment system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910893718.0A CN110655273A (en) | 2019-09-20 | 2019-09-20 | Old refuse landfill leachate treatment system and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110655273A true CN110655273A (en) | 2020-01-07 |
Family
ID=69038271
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910893718.0A Pending CN110655273A (en) | 2019-09-20 | 2019-09-20 | Old refuse landfill leachate treatment system and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110655273A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111333253A (en) * | 2020-01-14 | 2020-06-26 | 武汉天源环保股份有限公司 | Method for treating leachate of waste incineration plant |
| CN111470663A (en) * | 2020-04-24 | 2020-07-31 | 辽宁北方环境保护有限公司 | Full-quantitative emergency treatment method and system for small-scale landfill leachate |
| CN114085002A (en) * | 2021-11-17 | 2022-02-25 | 武汉天源环保股份有限公司 | Percolate concentrate treatment system and method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20150158748A1 (en) * | 2013-12-09 | 2015-06-11 | Pall Filtration Pte. Ltd. | Process for treating concentrated brine |
| CN108975598A (en) * | 2018-06-21 | 2018-12-11 | 光大环保技术研究院（深圳）有限公司 | A kind of zero-emission old-age group Landfill Leachate processing unit |
| CN109607942A (en) * | 2018-12-14 | 2019-04-12 | 杭州市环境集团有限公司 | The processing system and technique of a kind of flying dust and consumer waste infiltration liquid combined sewage |
| US20190233296A1 (en) * | 2018-01-26 | 2019-08-01 | Ethan J. Novek | Systems and methods for ammonia recovery, acid gas separation, or combination thereof |
| CN211170310U (en) * | 2019-09-20 | 2020-08-04 | 武汉天源环保股份有限公司 | Old garbage landfill leachate treatment system |
-
2019
- 2019-09-20 CN CN201910893718.0A patent/CN110655273A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20150158748A1 (en) * | 2013-12-09 | 2015-06-11 | Pall Filtration Pte. Ltd. | Process for treating concentrated brine |
| US20190233296A1 (en) * | 2018-01-26 | 2019-08-01 | Ethan J. Novek | Systems and methods for ammonia recovery, acid gas separation, or combination thereof |
| CN108975598A (en) * | 2018-06-21 | 2018-12-11 | 光大环保技术研究院（深圳）有限公司 | A kind of zero-emission old-age group Landfill Leachate processing unit |
| CN109607942A (en) * | 2018-12-14 | 2019-04-12 | 杭州市环境集团有限公司 | The processing system and technique of a kind of flying dust and consumer waste infiltration liquid combined sewage |
| CN211170310U (en) * | 2019-09-20 | 2020-08-04 | 武汉天源环保股份有限公司 | Old garbage landfill leachate treatment system |
Non-Patent Citations (3)
| Title |
|---|
| 张瑞娜等: "《饮用水安全与人们的生活 保护生命之源》", 31 May 2012, 冶金工业出版社, pages: 211 * |
| 班福忱等: "《土壤固化及其应用 筑路材料与技术的变革》", 30 June 2009, 中国环境科学出版社, pages: 112 - 113 * |
| 班福忱等: "《生活垃圾焚烧厂渗滤液处理实例教程》", 中国环境科学出版社, pages: 122 - 28 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111333253A (en) * | 2020-01-14 | 2020-06-26 | 武汉天源环保股份有限公司 | Method for treating leachate of waste incineration plant |
| CN111470663A (en) * | 2020-04-24 | 2020-07-31 | 辽宁北方环境保护有限公司 | Full-quantitative emergency treatment method and system for small-scale landfill leachate |
| CN114085002A (en) * | 2021-11-17 | 2022-02-25 | 武汉天源环保股份有限公司 | Percolate concentrate treatment system and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110655253A (en) | Full-quantitative treatment system and method for aged refuse landfill leachate | |
| CN110655273A (en) | Old refuse landfill leachate treatment system and method | |
| CN105417842A (en) | Advanced treatment method for high-concentration degradation-resistant liquid crystal electronic industrial wastewater | |
| CN102531296A (en) | Comprehensive electroplating wastewater treatment method | |
| CN101351412A (en) | Apparatus and method for treating organic-containing wastewater | |
| CN100509651C (en) | Combined technique for garbage filter liquor treatment | |
| CN205133286U (en) | Full automatic processing equipment of nickeliferous waste water of high concentration | |
| CN210176671U (en) | High-salt high-concentration degradation-resistant organic wastewater treatment equipment | |
| CN201713415U (en) | Dye wastewater treatment device | |
| CN105152471A (en) | Combined treatment process for non-biodegradable organic wastewater | |
| CN204981513U (en) | Treatment unit for pesticide -containing wastewater | |
| CN109851150A (en) | A kind of processing system and application of consumer waste landfill percolate | |
| CN211170310U (en) | Old garbage landfill leachate treatment system | |
| CN107935300B (en) | Process device and method for treating landfill leachate by non-membrane method | |
| CN211170274U (en) | Full-quantitative treatment system for percolate of old refuse landfill | |
| CN202988918U (en) | Multi-stage multi-section combined type high concentration chemical wastewater treatment system | |
| CN205575835U (en) | Electroplating wastewater treatment system | |
| CN112047566A (en) | Full-quantitative treatment system and method for landfill leachate | |
| CN201648189U (en) | Separating and combining device for regenerating and reclaiming film of electronic industrial wastewater | |
| CN103304076A (en) | Catalytic micro-electrolysis water treatment equipment and process method thereof | |
| CN216890540U (en) | High-suspended solid high-concentration organic wastewater treatment device | |
| CN207671875U (en) | Printing and dyeing wastewater treatment system | |
| CN203295291U (en) | Catalytic micro-electrolysis water treatment equipment | |
| CN215712375U (en) | Glyphosate wastewater treatment device | |
| CN216337082U (en) | Landfill leachate treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |