CN109399854A - Liquid-film method zero-emission treatment process and integration apparatus is concentrated in landfill leachate - Google Patents
Liquid-film method zero-emission treatment process and integration apparatus is concentrated in landfill leachate Download PDFInfo
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- CN109399854A CN109399854A CN201811503441.8A CN201811503441A CN109399854A CN 109399854 A CN109399854 A CN 109399854A CN 201811503441 A CN201811503441 A CN 201811503441A CN 109399854 A CN109399854 A CN 109399854A
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- membrane
- dope
- landfill leachate
- reverse osmosis
- suspended matter
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- 239000000149 chemical water pollutant Substances 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 54
- 230000010354 integration Effects 0.000 title description 2
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 104
- 238000010612 desalination reaction Methods 0.000 claims abstract description 57
- 150000002500 ions Chemical class 0.000 claims abstract description 57
- 238000000909 electrodialysis Methods 0.000 claims abstract description 55
- 239000007788 liquid Substances 0.000 claims abstract description 48
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 39
- 150000003839 salts Chemical class 0.000 claims abstract description 28
- 239000013505 freshwater Substances 0.000 claims abstract description 25
- 239000012141 concentrate Substances 0.000 claims abstract description 22
- 239000007787 solid Substances 0.000 claims abstract description 18
- PALNZFJYSCMLBK-UHFFFAOYSA-K magnesium;potassium;trichloride;hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[Cl-].[Cl-].[Cl-].[K+] PALNZFJYSCMLBK-UHFFFAOYSA-K 0.000 claims abstract description 14
- 239000010865 sewage Substances 0.000 claims abstract description 10
- 239000012528 membrane Substances 0.000 claims description 212
- 238000001728 nano-filtration Methods 0.000 claims description 63
- 239000012466 permeate Substances 0.000 claims description 40
- 238000000926 separation method Methods 0.000 claims description 31
- 238000001704 evaporation Methods 0.000 claims description 15
- 230000008020 evaporation Effects 0.000 claims description 15
- 238000000746 purification Methods 0.000 claims description 15
- 238000000108 ultra-filtration Methods 0.000 claims description 14
- 239000012530 fluid Substances 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 5
- 239000003011 anion exchange membrane Substances 0.000 claims description 4
- 238000005341 cation exchange Methods 0.000 claims description 4
- 238000009738 saturating Methods 0.000 claims description 4
- 239000000706 filtrate Substances 0.000 claims 1
- 239000002910 solid waste Substances 0.000 abstract 1
- 239000005416 organic matter Substances 0.000 description 7
- 238000011084 recovery Methods 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 2
- 238000002306 biochemical method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000005684 electric field Effects 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 125000003277 amino group Chemical group 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 230000005685 electric field effect Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000005325 percolation Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- -1 salinities etc. Substances 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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
- C02F1/44—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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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)
Abstract
The invention belongs to landfill leachate dope process fields, specifically disclose a kind of device and method of landfill leachate thick liquid-film method zero-emission.The method of the landfill leachate dope includes: that (1) separates hardness ions and suspended matter from landfill leachate dope, obtains the clear liquid of dope and depleted hardness ions and suspended matter rich in hardness ions and suspended matter；(2) clear liquid is subjected to electrodialysis desalination processing, obtains the fresh water of concentrated water and depleted salt rich in salt；(3) fresh water is subjected to reverse osmosis treatment, obtains concentrate and dialyzate, concentrate is back to step (1), and dialyzate is as Treated sewage reusing；(4) by the moisture removal in the dope for being originated from step (1) and the concentrated water for being originated from step (2) to obtain solid carnallite.Using device and method provided by the invention can be realized by landfill leachate dope be processed into can reuse middle water and solid waste, achieve the purpose that zero-emission, alleviate the operating pressure of incinerator.
Description
Technical field
The invention belongs to landfill leachate dope process fields, and in particular to a kind of landfill leachate thick liquid-film method zero-emission
Device and method.
Background technique
Landfill leachate is a kind of complicated component, concentration height and intractable waste water.Current main processing technique is to adopt
It is handled with the processing mode that biochemistry is combined with embrane method, wherein biochemical method can remove number big absolutely in landfill leachate
COD value, ammonia-nitrogen content etc. is effectively reduced in organic matter；Feed liquid after biochemistry is using ultrafiltration, nanofiltration or the embrane methods point such as reverse osmosis
From further filtering the substances such as remaining organic matter, salinity, enabling that treated, waste water reaches discharge standard.Membrane separating
Process can generate the landfill leachate dope of overall accumulated amount 20~30%, be enriched landfill leachate in the landfill leachate dope
In a large amount of difficult biochemical organic matter, salinities etc., COD value and conductivity are 3~4 times of crude waste percolate, even as high as 5
Times, and with the extension of embrane method Refuse Leachate Treatment Plant runing time, the amount of produced landfill leachate dope gradually increases
Greatly, the concentration of salt and organic matter also gradually rises.
Being effectively treated for landfill leachate dope is the indispensable pith of entire garbage percolation liquid treating system.It should
If landfill leachate dope direct emission, it will cause secondary pollution.Currently used processing method mainly has following two
Kind.The first, garbage incinerating power plant is back that being sprayed onto burner hearth burns to the mainstream treatment process of landfill leachate dope, so
And part concentrate can only be handled using this method, it returns to be sprayed onto burner hearth and burn and will lead to fire grate seriously corroded, deduster is stifled
Ash, conical opening dirt are stifled etc., cause equipment to need to shut down regularly, and can also reduce furnace temperature using the processing method, to setting
Standby normal operation is very unfavorable.Second, garbage loading embeading factory is by its recharge to the mainstream treatment process of landfill leachate dope
To junk-heap body, the increase of percolate salinity will cause in this way, processing system load, which increases, even to collapse.
Therefore, be badly in need of developing it is a kind of can be to the device and method that landfill leachate dope is effectively treated.
Summary of the invention
The present invention is intended to provide a kind of device and method of new landfill leachate thick liquid-film method zero-emission.
Specifically, the method for landfill leachate thick liquid-film method zero-emission provided by the invention includes:
(1) hardness ions and suspended matter are separated from landfill leachate dope to be processed, is obtained rich in hardness
The clear liquid of the dope and depleted hardness ions and suspended matter of ion and suspended matter；
(2) clear liquid is subjected to electrodialysis desalination processing, obtains the fresh water of concentrated water and depleted salt rich in salt；
(3) fresh water is subjected to reverse osmosis treatment, obtains concentrate and dialyzate, the concentrate is back to step
(1) continue the separation of hardness ions and suspended matter, the dialyzate is as reuse in water；
(4) moisture removal in the dope for being originated from step (1) and the concentrated water for being originated from step (2) is miscellaneous to obtain solid
Salt.
Preferably, the pH value of the landfill leachate dope is 6~9, and permanent hardness is 1000~5000mg/L, conductivity
For 20~120ms/cm, COD value is 3000~12000mg/L.
Preferably, in step (1), the isolated mode and condition make the dope permanent hardness be 5000~
8000mg/L and COD value are 20000~60000mg/L, and the permanent hardness of the clear liquid is 500~1000mg/L and COD value is
500~1000mg/L.
Preferably, described to be separated into UF membrane in step (1), and film core used by the UF membrane be selected from ultrafiltration membrane,
At least two in nanofiltration membrane and reverse osmosis membrane.
Preferably, in step (1), the aperture of the ultrafiltration membrane is 4000~6000Da, and the aperture of the nanofiltration membrane is 100
~200Da, the aperture of the reverse osmosis membrane are 100Da or less.
Preferably, in step (1), the UF membrane carries out in mixed loading membrane separation device, the mixed loading membrane separation device
It is set including membrane tube and the reverse-osmosis membrane element being arranged in series in the membrane tube and nanofiltration membrane component, the reverse-osmosis membrane element
Set in membrane tube front, the nanofiltration membrane component setting at membrane tube rear portion, and the permeate central tube of the reverse-osmosis membrane element with
The permeate central tube of nanofiltration membrane component separates；The landfill leachate dope introduces reverse-osmosis membrane element from the feed inlet of membrane tube
Middle progress first time UF membrane, the reverse osmosis trapped fluid of gained, which is introduced into nanofiltration membrane component, carries out second of UF membrane, gained reverse osmosis
Saturating permeate and nanofiltration membrane permeate respectively enter the reverse-osmosis membrane element permeate central tube and nanofiltration membrane component it is saturating
It crosses liquid central tube and carries out electrodialysis desalination processing, gained nanofiltration collectively as the clear liquid of the depleted hardness ions and suspended matter
Film trapped fluid carries out moisture removal as the dope rich in hardness ions and suspended matter to obtain solid carnallite.
Preferably, in step (1), the running temperature of the UF membrane is 5~40 DEG C, and operating pressure is 15~25bar.
Preferably, in step (2), the conductivity 120 of the concentrated water that the condition of electrodialysis desalination processing makes~
The conductivity of 200ms/cm and fresh water is 1~10ms/cm.
Preferably, in step (2), the running temperature of the electrodialysis desalination processing is 5~40 DEG C, operating pressure 2bar
Below.
Preferably, in step (3), the conductivity 0.01 of the dialyzate that the condition of the reverse osmosis treatment makes~
5ms/cm。
Preferably, in step (3), the aperture of reverse osmosis membrane used by the reverse osmosis treatment is 100Da or less.
Preferably, in step (3), the running temperature of the reverse osmosis treatment is 5~40 DEG C, operating pressure is 15~
25bar。
The equipment of landfill leachate thick liquid-film method zero-emission provided by the invention includes:
MMS unit is obtained for separating hardness ions and suspended matter from landfill leachate dope to be processed
The clear liquid of dope and depleted hardness ions and suspended matter rich in hardness ions and suspended matter；
Electrodialysis desalination unit is rich in for carrying out electrodialysis desalination processing to the clear liquid for being originated from the MMS unit
The fresh water of the concentrated water of salt and depleted salt；
Reverse osmosis units are concentrated for carrying out reverse osmosis treatment to the fresh water for being originated from the electrodialysis desalination unit
Liquid and dialyzate, the concentrate are back to the MMS unit, and the dialyzate is as Treated sewage reusing；
Evaporation element is purified, for the dope of the MMS unit will to be originated from and from the electrodialysis desalination unit
Moisture removal in concentrated water is to obtain solid carnallite.
Preferably, the MMS unit is to load in mixture film separation unit.
Preferably, described to load in mixture film core used by film separation unit in ultrafiltration membrane, nanofiltration membrane and reverse osmosis membrane
At least two.
Preferably, the aperture of the ultrafiltration membrane is 4000~6000Da, and the aperture of the nanofiltration membrane is 100~200Da, institute
The aperture for stating reverse osmosis membrane is 100Da or less.
Preferably, the MMS unit is mixed loading membrane separation device comprising membrane tube and is arranged in series in the membrane tube
Reverse-osmosis membrane element and nanofiltration membrane component, reverse-osmosis membrane element setting is in membrane tube front, the nanofiltration membrane component setting
At membrane tube rear portion, and the permeate central tube of the reverse-osmosis membrane element and the permeate central tube of nanofiltration membrane component separate；Institute
It states landfill leachate dope and is introduced into reverse-osmosis membrane element progress first time UF membrane from the feed inlet of membrane tube, reverse osmosis section of gained
It stays liquid to be introduced into nanofiltration membrane component and carries out second of UF membrane, the reverse osmosis permeate of gained and nanofiltration membrane permeate respectively enter instead
The permeate central tube of permeable membrane device and the permeate central tube of nanofiltration membrane component and collectively as the depleted hardness ions
And the clear liquid of suspended matter is introduced into electrodialysis desalination unit and carries out electrodialysis desalination processing, described in the conduct of gained nanofiltration membrane trapped fluid
Dope rich in hardness ions and suspended matter, which is introduced into purification evaporation element, carries out moisture removal to obtain solid carnallite.
Preferably, amberplex used by the electrodialysis desalination unit includes the cation-exchange membrane of cross arrangement
With anion-exchange membrane.
Preferably, the aperture of reverse osmosis membrane used by the reverse osmosis units is 100Da or less.
Preferably, the purification evaporation element is that curtain type purifies evaporator.
Beneficial effects of the present invention are as follows:
(1) landfill leachate dope by successively being carried out hardness ions and suspension removing, electrodialysis desalination by the present invention
Processing, reverse osmosis treatment and dehydration, with realize by landfill leachate dope be processed into can reuse middle water and solid give up
Gurry, achievees the purpose that zero-emission, not only alleviates the operating pressure of incinerator, but also is able to produce out and meets reuse standard
Middle water, save water resource, improve energy utilization rate；
(2) using the device and method of landfill leachate thick liquid-film method zero-emission provided by the invention, low energy consumption, automation
Degree is high, and high production efficiency is good in economic efficiency, energy conservation and environmental protection.
Detailed description of the invention
Fig. 1 is the flow diagram of the method for landfill leachate thick liquid-film method zero-emission provided by the invention.
Fig. 2 is the structural schematic diagram of mixed loading membrane separation device provided by the invention.
Description of symbols
1-MMS unit；11- membrane tube；12- reverse-osmosis membrane element；13- nanofiltration membrane component；14- plug；121,131- is penetrated
Liquid central tube；2- electrodialysis desalination unit；3- reverse osmosis units；4- purifies evaporation element.
Specific embodiment
The present invention described in detail below.
The method of landfill leachate thick liquid-film method zero-emission provided by the invention includes:
(1) hardness ions and suspended matter are separated from landfill leachate dope to be processed, is obtained rich in hardness
The clear liquid of the dope and depleted hardness ions and suspended matter of ion and suspended matter；
(2) clear liquid is subjected to electrodialysis desalination processing, obtains the fresh water of concentrated water and depleted salt rich in salt；
(3) fresh water is subjected to reverse osmosis treatment, obtains concentrate and dialyzate, the concentrate is back to step
(1) continue the separation of hardness ions and suspended matter, the dialyzate is as Treated sewage reusing；
(4) moisture removal in the dope for being originated from step (1) and the concentrated water for being originated from step (2) is miscellaneous to obtain solid
Salt.
The landfill leachate dope is to carry out handling it using the biochemical method combined with embrane method by landfill leachate
Resulting dope afterwards.Generally, the pH value of the landfill leachate dope can be 6~9, permanent hardness can for 1000~
5000mg/L, conductivity can be 20~120ms/cm, and COD value can be 3000~12000mg/L.In the present invention, term
" permanent hardness " refers to the sum of permanent calcium hardness and permanent magnesium hardness.
There is no particular limitation for the present invention described to step (1) isolated mode and condition, it is preferable that the dope
Permanent hardness is 5000~8000mg/L and COD value is 20000~60000mg/L, and makes the permanent hardness of the clear liquid to be
500~1000mg/L and COD value are 500~1000mg/L.The separation is preferably UF membrane.Film used by the UF membrane
Core can be selected from least one of ultrafiltration membrane, nanofiltration membrane and reverse osmosis membrane, it is preferred to use at least two of three of the above film core
It is used cooperatively.Wherein, the aperture of the ultrafiltration membrane is preferably 4000~6000Da, and the aperture of the nanofiltration membrane is preferably 100~
200Da, the aperture of the reverse osmosis membrane are preferably 100Da or less.A preferred embodiment of the invention, such as Fig. 2 institute
Show, the UF membrane carries out in mixed loading membrane separation device, and the mixed loading membrane separation device includes membrane tube 11 and is arranged in series
Reverse-osmosis membrane element 12 and nanofiltration membrane component 13 in the membrane tube 11, the reverse-osmosis membrane element 12 are arranged before membrane tube 11
Portion, the nanofiltration membrane component 13 setting at 11 rear portion of membrane tube, and the permeate central tube 121 of the reverse-osmosis membrane element 12 with receive
The permeate central tube 131 of filter membrane component 13 separates.It is highly preferred that the 12 permeate central tube 121 of reverse-osmosis membrane element
Rear end and the front end of 13 permeate central tube 131 of nanofiltration membrane component are separated by plug 14.When operating, the landfill leachate
Dope is introduced into progress first time UF membrane, most of hardness ions and suspension in reverse-osmosis membrane element 12 from the feed inlet of membrane tube 11
Object is trapped, small part with dampening penetrate reverse-osmosis membrane element 12, the reverse osmosis trapped fluid of gained be introduced into nanofiltration membrane component 13 into
Second of UF membrane of row, feeding liquid are concentrated, and the reverse osmosis permeate of gained and nanofiltration membrane permeate respectively enter described reverse osmosis
The permeate central tube 121 of membrane component 12 and the permeate central tube 131 of nanofiltration membrane component 13 and collectively as described depleted hard
The clear liquid for spending ion and suspended matter carries out electrodialysis desalination processing, gained nanofiltration membrane trapped fluid as it is described rich in hardness ions and
The dope of suspended matter carries out moisture removal to obtain solid carnallite.
According to the present invention, in step (1), the running temperature of the UF membrane is preferably 5~40 DEG C, and operating pressure is preferably
15~25bar.In the present invention, the pressure refers both to gauge pressure.
Term " electrodialysis desalination processing " refers under electric field action, is separated using the selective penetrated property of amberplex
The method of different ions.There is no particular limitation to the condition that electrodialysis desalination described in step (2) is handled by the present invention, preferably makes
The conductivity of obtained concentrated water is 120~200ms/cm and the conductivity of fresh water is 1~10ms/cm.Specifically, the electrodialysis
The running temperature of desalting processing can be 5~40 DEG C, and operating pressure can be 2bar or less.
There is no particular limitation for condition of the present invention to step (3) described reverse osmosis treatment, it is preferable that the dialyzate arrived
Conductivity be 0.01~5ms/cm.Specifically, the aperture of reverse osmosis membrane used by the reverse osmosis treatment can be 100Da
Below.The running temperature of the reverse osmosis treatment can be 5~40 DEG C, and operating pressure can be 15~25bar.
As shown in Figure 1, the equipment of landfill leachate thick liquid-film method zero-emission provided by the invention includes:
MMS unit 1 is obtained for separating hardness ions and suspended matter from landfill leachate dope to be processed
To the clear liquid of dope and depleted hardness ions and suspended matter rich in hardness ions and suspended matter；
Electrodialysis desalination unit 2 obtains richness for carrying out electrodialysis desalination processing to the clear liquid for being originated from the MMS unit 1
The fresh water of the concentrated water of saliferous and depleted salt；
Reverse osmosis units 3 obtain dense for carrying out reverse osmosis treatment to the fresh water for being originated from the electrodialysis desalination unit 2
Contracting liquid and dialyzate, the concentrate are back to the MMS unit 1, and the dialyzate is as Treated sewage reusing；
Evaporation element 4 is purified, for that will be originated from the dope of the MMS unit 1 and be originated from the electrodialysis desalination unit 2
Concentrated water in moisture removal to obtain solid carnallite.
The MMS unit 1 is for removing hardness ions and suspended matter.Hardness ions in the refuse leachate concentrate
And suspended matter is separated to some extent in MMS unit 1, so that hardness ions and suspended matter are enriched to concentrate side, is protected
Protect the electrodialytic water inlet index request of subsequent handling.The MMS unit 1 is preferably film separation unit.The film separation unit institute
The film core of use can be selected from least one of ultrafiltration membrane, nanofiltration membrane and reverse osmosis membrane, it is preferred to use three of the above film core
At least two are used cooperatively.That is, the film separation unit is preferably at least two used in ultrafiltration membrane, nanofiltration membrane and reverse osmosis membrane
What kind film core was used cooperatively loads in mixture film separation unit.Wherein, the aperture of the ultrafiltration membrane is preferably 4000~6000Da, described to receive
The aperture of filter membrane is preferably 100~200Da, and the aperture of the reverse osmosis membrane is preferably 100Da or less.One kind according to the present invention
Preferred embodiment, as shown in Fig. 2, the UF membrane carries out in mixed loading membrane separation device, the mixed loading membrane separation device packet
The reverse-osmosis membrane element 12 and nanofiltration membrane component 13 for including membrane tube 11 and being arranged in series in the membrane tube 11, the reverse osmosis membrane
The setting of element 12 is arranged in 11 front of membrane tube, the nanofiltration membrane component 13 at 11 rear portion of membrane tube, and the reverse-osmosis membrane element 12
Permeate central tube 121 and the permeate central tube 131 of nanofiltration membrane component 13 separate.It is highly preferred that the reverse osmosis membrane element
The rear end of 12 permeate central tube 121 of part and the front end of 13 permeate central tube 131 of nanofiltration membrane component are separated by plug 14.Institute
It states landfill leachate dope and is introduced into progress first time UF membrane, gained reverse osmosis in reverse-osmosis membrane element 12 from the feed inlet of membrane tube 11
Saturating trapped fluid, which is introduced into nanofiltration membrane component 13, carries out second of UF membrane, the reverse osmosis permeate of gained and nanofiltration membrane permeate difference
It is simultaneously common into the permeate central tube 121 of the reverse-osmosis membrane element 12 and the permeate central tube 131 of nanofiltration membrane component 13
Clear liquid as the depleted hardness ions and suspended matter is introduced into the electrodialysis desalination unit 2 and carries out at electrodialysis desalination
Reason, gained nanofiltration membrane trapped fluid are introduced into the purification evaporation element 4 as the dope rich in hardness ions and suspended matter
Moisture removal is carried out to obtain solid carnallite.
For the salinity in concentrated waste penetrating fluid dope, the fresh water after desalination introduces anti-the electrodialysis desalination unit 2
Permeation unit 3, organic matter and monovalent salt are separated, and are enriched with organic matter in concentrate, and dialyzate reaches reuse standard, dense
Organic matter and monovalent salt in contracting liquid return after being largely enriched with to be set to 1 front end of MMS unit and continues hardness ions in turn and hang
The separation of floating object.
Amberplex used by the electrodialysis desalination unit 2 preferably include the cation-exchange membrane of cross arrangement with
Anion-exchange membrane, when being used for electrodialysis desalination processing, cation and anion can be retained down, and be come with this real
The purpose that now salt in the clear liquid 1 for being originated from MMS unit is removed.
The aperture of reverse osmosis membrane used by the reverse osmosis units 3 is preferably 100Da or less.
The purification evaporation element 4 is preferably that curtain type purifies evaporator.Wherein, the tool of the curtain type purification evaporator
Body structure is referring to CN108191170A.
The working principle of the MMS unit 1 and reverse osmosis units 3 is to utilize seperation film difference hole using pressure as motive force
Diameter carries out physical separation screening to solute in liquid；The working principle of the electrodialysis desalination unit 2 be using electric field as motive force,
Ion is migrated under DC electric field effect, and the solute particles (such as ion) charged in solution migrate to reach by film
The purpose of concentration.The working principle of the purification evaporation element 4 is to evaporate surplus in dope and concentrated water using psychrometric difference as motive force
Remaining moisture, reaches zero emission requirement.
As shown in Figure 1, when by the equipment of the landfill leachate thick liquid-film method zero-emission be used for landfill leachate dope into
When row processing, landfill leachate dope is introduced into MMS unit 1 separation for carrying out hardness ions and suspended matter, obtains rich in hardness
The clear liquid of the dope and depleted hardness ions and suspended matter of ion and suspended matter；Clear liquid from the MMS unit 1 introduces electricity
Electrodialysis desalination unit 2 carries out electrodialysis desalination processing, obtains the fresh water of concentrated water and depleted salt rich in salt；From the electrodialysis
The fresh water of desalination unit 2, which is introduced into reverse osmosis units 3, carries out reverse osmosis treatment, obtains concentrate and dialyzate, the concentrate
It is back to the MMS unit 1, the dialyzate is as Treated sewage reusing；It dope from the MMS unit 1 and is originated from described
The concentrated water of electrodialysis desalination unit 2 is introduced into purification evaporation element 4 to obtain solid carnallite for moisture removal therein.
The present invention will be described in detail by way of examples below.
In following embodiment:
MMS unit 1 is mixed loading membrane separation device comprising membrane tube 11 and the reverse osmosis being arranged in series in the membrane tube 11
Membrane element 12 and nanofiltration membrane component 13, the reverse-osmosis membrane element 12 are arranged in 11 front of membrane tube, the nanofiltration membrane component 13
It is arranged at 11 rear portion of membrane tube, and in the rear end of 12 permeate central tube 121 of reverse-osmosis membrane element and 13 permeate of nanofiltration membrane component
The front end of heart pipe 131 is separated by plug 14；
Amberplex used by electrodialysis desalination unit 2 is by one layer of sulfonic acid type cation exchange membrane and one layer of quaternary amine type
Anion exchange membrane facing is folded to be formed.
In following embodiment, the rate of recovery (%)=production water inventory/water inlet total amount × 100% of water.
Embodiment 1
As shown in Figure 1, landfill leachate dope (pH value 6.5, permanent hardness 2500mg/L, conductivity 50ms/
Cm, COD value 5000mg/L) introducing MMS unit 1, (wherein, the aperture of reverse-osmosis membrane element 12 is 80Da, nanofiltration membrane component 13
Aperture be 100Da) in the separation of hardness ions and suspended matter is carried out in the case where temperature is 35 DEG C and pressure is 25bar, obtain richness
The clear liquid of dope and depleted hardness ions and suspended matter containing hardness ions and suspended matter, wherein the permanent hardness of dope is
8000mg/L and COD value are 50000mg/L, and the permanent hardness of clear liquid is 800mg/L and COD value is 600mg/L；From described
The clear liquid of MMS unit 1 is introduced into electrodialysis desalination unit 2 to carry out at electrodialysis desalination in the case where temperature is 35 DEG C and pressure is 1bar
Reason, obtains the rich-salt concentrated water that conductivity is 130ms/cm and the depleted salt fresh water that conductivity is 20ms/cm；From the electric osmose
The depleted salt fresh water of analysis desalination unit 2 is introduced into reverse osmosis units 3 (aperture of used reverse osmosis membrane is 80Da) in temperature
For 40 DEG C and pressure be 25bar under carry out reverse osmosis treatment, obtain the dialyzate that concentrate and conductivity are 5ms/cm, it is described dense
Contracting liquid is back to the MMS unit 1, and the dialyzate is as Treated sewage reusing；It dope from the MMS unit 1 and is originated from
The concentrated water of the electrodialysis desalination unit 2 is introduced into purification evaporation element 4 (curtain type purification evaporator) with by moisture therein
Removing, obtains solid carnallite.The rate of recovery of water is 65%.
Embodiment 2
As shown in Figure 1, landfill leachate dope (pH value 6.5, permanent hardness 2500mg/L, conductivity 50ms/
Cm, COD value 5000mg/L) introducing MMS unit 1, (wherein, the aperture of reverse-osmosis membrane element 12 is 100Da, nanofiltration membrane component 13
Aperture be 200Da) in the separation of hardness ions and suspended matter is carried out in the case where temperature is 5 DEG C and pressure is 15bar, be rich in
The clear liquid of the dope and depleted hardness ions and suspended matter of hardness ions and suspended matter, wherein the permanent hardness of dope is
5000mg/L and COD value are 20000mg/L, and the permanent hardness of clear liquid is 1000mg/L and COD value is 1000mg/L；From described
The clear liquid of MMS unit 1, which is introduced into electrodialysis desalination unit 2, carries out electrodialysis desalination in the case where temperature is 5 DEG C and pressure is 0.5bar
Processing, obtains the rich-salt concentrated water that conductivity is 150ms/cm and the depleted salt fresh water that conductivity is 8ms/cm；From the electricity
The depleted salt fresh water of electrodialysis desalination unit 2 is introduced into reverse osmosis units 3 (aperture of used reverse osmosis membrane is 100Da) in temperature
Degree for 5 DEG C and pressure be 15bar under carry out reverse osmosis treatment, obtain concentrate and dialyzate that conductivity is 0.1ms/cm, institute
It states concentrate and is back to the MMS unit 1, the dialyzate is as Treated sewage reusing；Dope from the MMS unit 1 and
Concentrated water from the electrodialysis desalination unit 2 is introduced into purification evaporation element 4 (curtain type purification evaporator) with will be therein
Moisture removal obtains solid carnallite.The rate of recovery of water is 60%.
Embodiment 3
As shown in Figure 1, landfill leachate dope (pH value 7, permanent hardness 2000mg/L, conductivity 50ms/cm,
COD value is 3000mg/L) introducing MMS unit 1, (wherein, the aperture of reverse-osmosis membrane element 12 is 90Da, the hole of nanofiltration membrane component 13
Diameter is 150Da) in the separation of hardness ions and suspended matter is carried out in the case where temperature is 20 DEG C and pressure is 20bar, obtain rich in hard
Spend the dope of ion and suspended matter and the clear liquid of depleted hardness ions and suspended matter, wherein the permanent hardness of dope is
6500mg/L and COD value are 35000mg/L, and the permanent hardness of clear liquid is 500mg/L and COD value is 500mg/L；From described
The clear liquid of MMS unit 1 is introduced into electrodialysis desalination unit 2 to carry out at electrodialysis desalination in the case where temperature is 40 DEG C and pressure is 2bar
Reason, obtains the rich-salt concentrated water that conductivity is 125ms/cm and the depleted salt fresh water that conductivity is 10ms/cm；From the electric osmose
The depleted salt fresh water of analysis desalination unit 2 is introduced into reverse osmosis units 3 (aperture of used reverse osmosis membrane is 90Da) in temperature
For 20 DEG C and pressure be 20bar under carry out reverse osmosis treatment, obtain the dialyzate that concentrate and conductivity are 2ms/cm, it is described dense
Contracting liquid is back to the MMS unit 1, and the dialyzate is as Treated sewage reusing；It dope from the MMS unit 1 and is originated from
The concentrated water of the electrodialysis desalination unit 2 is introduced into purification evaporation element 4 (curtain type purification evaporator) with by moisture therein
Removing, obtains solid carnallite.The rate of recovery of water is 63%.
Although the embodiments of the present invention has been shown and described above, it is to be understood that above-described embodiment is example
Property, it is not considered as limiting the invention, those skilled in the art are not departing from the principle of the present invention and objective
In the case where can make changes, modifications, alterations, and variations to the above described embodiments within the scope of the invention.
Claims (10)
1. a kind of method of landfill leachate thick liquid-film method zero-emission, which is characterized in that this method comprises:
(1) hardness ions and suspended matter are separated from landfill leachate dope to be processed, is obtained rich in hardness ions
And suspended matter dope and depleted hardness ions and suspended matter clear liquid；
(2) clear liquid is subjected to electrodialysis desalination processing, obtains the fresh water of concentrated water and depleted salt rich in salt；
(3) fresh water is subjected to reverse osmosis treatment, obtains concentrate and dialyzate, the concentrate be back to step (1) after
The continuous separation for carrying out hardness ions and suspended matter, the dialyzate is as Treated sewage reusing；
(4) by the moisture removal in the dope for being originated from step (1) and the concentrated water for being originated from step (2) to obtain solid carnallite.
2. the method for landfill leachate thick liquid-film method zero-emission according to claim 1, which is characterized in that the rubbish seeps
The pH value of filtrate dope is 6~9, and permanent hardness is 1000~5000mg/L, and conductivity is 20~120ms/cm, and COD value is
3000~12000mg/L.
3. the method for landfill leachate thick liquid-film method zero-emission according to claim 2, which is characterized in that in step (1),
The isolated mode and condition make the permanent hardness of the dope be 5000~8000mg/L and COD value be 20000~
60000mg/L, the permanent hardness of the clear liquid is 500~1000mg/L and COD value is 500~1000mg/L.
4. the method for landfill leachate thick liquid-film method zero-emission according to claim 3, which is characterized in that in step (1),
It is described to be separated into UF membrane, and film core used by the UF membrane in ultrafiltration membrane, nanofiltration membrane and reverse osmosis membrane at least
Two kinds；Preferably, the aperture of the ultrafiltration membrane is 4000~6000Da, and the aperture of the nanofiltration membrane is 100~200Da, described
The aperture of reverse osmosis membrane is 100Da or less；
Preferably, the UF membrane carries out in mixed loading membrane separation device, and the mixed loading membrane separation device includes membrane tube and string
Joining the reverse-osmosis membrane element and nanofiltration membrane component being arranged in the membrane tube, the reverse-osmosis membrane element is arranged in membrane tube front,
Nanofiltration membrane component setting is at membrane tube rear portion, and the permeate central tube of the reverse-osmosis membrane element and nanofiltration membrane component is saturating
Liquid central tube is crossed to separate；The landfill leachate dope is introduced into progress first time film in reverse-osmosis membrane element from the feed inlet of membrane tube
Separation, the reverse osmosis trapped fluid of gained, which is introduced into nanofiltration membrane component, carries out second of UF membrane, the reverse osmosis permeate of gained and nanofiltration
Film permeate respectively enters the permeate central tube of the reverse-osmosis membrane element and the permeate central tube of nanofiltration membrane component and is total to
Electrodialysis desalination processing is carried out with as the clear liquid of the depleted hardness ions and suspended matter, gained nanofiltration membrane trapped fluid is as institute
It states the dope rich in hardness ions and suspended matter and carries out moisture removal to obtain solid carnallite；
Preferably, the running temperature of the UF membrane is 5~40 DEG C, and operating pressure is 15~25bar.
5. the method for landfill leachate thick liquid-film method zero-emission described in any one of -4, feature exist according to claim 1
In, in step (2), the 120~200ms/cm of conductivity for the concentrated water that the condition of electrodialysis desalination processing makes and light
The conductivity of water is 1~10ms/cm；Preferably, the running temperature of the electrodialysis desalination processing is 5~40 DEG C, operating pressure
For 2bar or less.
6. the method for landfill leachate thick liquid-film method zero-emission described in any one of -4, feature exist according to claim 1
In, in step (3), the 0.01~5ms/cm of conductivity for the dialyzate that the condition of the reverse osmosis treatment makes；Preferably,
The aperture of reverse osmosis membrane used by the reverse osmosis treatment is 100Da or less；Preferably, the operation temperature of the reverse osmosis treatment
Degree is 5~40 DEG C, and operating pressure is 15~25bar.
7. a kind of equipment of landfill leachate thick liquid-film method zero-emission characterized by comprising
MMS unit is rich in for separating hardness ions and suspended matter from landfill leachate dope to be processed
The clear liquid of the dope and depleted hardness ions and suspended matter of hardness ions and suspended matter；
Electrodialysis desalination unit is obtained for carrying out electrodialysis desalination processing to the clear liquid for being originated from the MMS unit rich in salt
The fresh water of concentrated water and depleted salt；
Reverse osmosis units, for be originated from the electrodialysis desalination unit fresh water carry out reverse osmosis treatment, obtain concentrate and
Dialyzate, the concentrate are back to the MMS unit, and the dialyzate is as Treated sewage reusing；
Evaporation element is purified, for the dope of the MMS unit will to be originated from and the concentrated water from the electrodialysis desalination unit
In moisture removal to obtain solid carnallite.
8. the equipment of landfill leachate thick liquid-film method zero-emission according to claim 7, which is characterized in that the MMS is mono-
Member is to load in mixture film separation unit；Preferably, described to load in mixture film core used by film separation unit and be selected from ultrafiltration membrane, nanofiltration membrane and anti-
At least two in permeable membrane；Preferably, the aperture of the ultrafiltration membrane is 4000~6000Da, and the aperture of the nanofiltration membrane is
100~200Da, the aperture of the reverse osmosis membrane are 100Da or less；
Preferably, the MMS unit is mixed loading membrane separation device comprising membrane tube and is arranged in series in anti-in the membrane tube
Permeable membrane device and nanofiltration membrane component, in membrane tube front, the nanofiltration membrane component is arranged in film for the reverse-osmosis membrane element setting
Pipe rear portion, and the permeate central tube of the reverse-osmosis membrane element and the permeate central tube of nanofiltration membrane component separate；The rubbish
Rubbish percolate dope is introduced into progress first time UF membrane, the reverse osmosis trapped fluid of gained in reverse-osmosis membrane element from the feed inlet of membrane tube
It is introduced into nanofiltration membrane component and carries out second of UF membrane, the reverse osmosis permeate of gained and nanofiltration membrane permeate respectively enter described anti-
The permeate central tube of permeable membrane device and the permeate central tube of nanofiltration membrane component and collectively as the depleted hardness ions
And the clear liquid of suspended matter is introduced into progress electrodialysis desalination processing, gained nanofiltration membrane trapped fluid conduct in the electrodialysis desalination unit
It is miscellaneous to obtain solid that the dope rich in hardness ions and suspended matter is introduced into progress moisture removal in the purification evaporation element
Salt.
9. the equipment of landfill leachate thick liquid-film method zero-emission according to claim 7, which is characterized in that the electrodialysis
Amberplex used by desalination unit includes the cation-exchange membrane and anion-exchange membrane of cross arrangement.
10. the equipment of landfill leachate thick liquid-film method zero-emission according to claim 7, which is characterized in that
The aperture of reverse osmosis membrane used by the reverse osmosis units is 100Da or less；
The purification evaporation element is that curtain type purifies evaporator.
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