CN106391652A - Cooperative treatment method for refuse incineration fly ash and refuse leachate - Google Patents
Cooperative treatment method for refuse incineration fly ash and refuse leachate Download PDFInfo
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- CN106391652A CN106391652A CN201610799980.5A CN201610799980A CN106391652A CN 106391652 A CN106391652 A CN 106391652A CN 201610799980 A CN201610799980 A CN 201610799980A CN 106391652 A CN106391652 A CN 106391652A
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- 238000000034 method Methods 0.000 title claims abstract description 83
- 239000010881 fly ash Substances 0.000 title claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 15
- 231100000419 toxicity Toxicity 0.000 claims abstract description 8
- 230000001988 toxicity Effects 0.000 claims abstract description 8
- 239000002904 solvent Substances 0.000 claims abstract description 7
- 229910052782 aluminium Inorganic materials 0.000 claims abstract 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims abstract 2
- 239000000428 dust Substances 0.000 claims description 52
- 230000008569 process Effects 0.000 claims description 40
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 33
- 239000007788 liquid Substances 0.000 claims description 33
- 239000000203 mixture Substances 0.000 claims description 22
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 17
- 238000000926 separation method Methods 0.000 claims description 17
- 229910052814 silicon oxide Inorganic materials 0.000 claims description 17
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 16
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 16
- 239000000292 calcium oxide Substances 0.000 claims description 16
- 238000003756 stirring Methods 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 15
- 230000018044 dehydration Effects 0.000 claims description 9
- 238000006297 dehydration reaction Methods 0.000 claims description 9
- 238000002156 mixing Methods 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 231100000770 Toxic Equivalency Factor Toxicity 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 5
- 230000007246 mechanism Effects 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- 229910001018 Cast iron Inorganic materials 0.000 claims description 3
- 229910000831 Steel Inorganic materials 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 238000003825 pressing Methods 0.000 claims description 3
- 239000010959 steel Substances 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims 1
- 229910052760 oxygen Inorganic materials 0.000 claims 1
- 239000001301 oxygen Substances 0.000 claims 1
- 229950000845 politef Drugs 0.000 claims 1
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 33
- 239000002956 ash Substances 0.000 abstract description 7
- 238000002386 leaching Methods 0.000 abstract description 5
- 230000003647 oxidation Effects 0.000 abstract description 3
- 238000007254 oxidation reaction Methods 0.000 abstract description 3
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 abstract 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 abstract 1
- 229910052799 carbon Inorganic materials 0.000 abstract 1
- 238000000354 decomposition reaction Methods 0.000 abstract 1
- 239000002957 persistent organic pollutant Substances 0.000 abstract 1
- 239000011148 porous material Substances 0.000 abstract 1
- 230000009257 reactivity Effects 0.000 abstract 1
- 230000000630 rising effect Effects 0.000 abstract 1
- 229910052710 silicon Inorganic materials 0.000 abstract 1
- 239000010703 silicon Substances 0.000 abstract 1
- 238000005406 washing Methods 0.000 description 21
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 16
- 230000000694 effects Effects 0.000 description 11
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 9
- 239000000460 chlorine Substances 0.000 description 9
- 229910052801 chlorine Inorganic materials 0.000 description 9
- 229910017053 inorganic salt Inorganic materials 0.000 description 7
- 229910021536 Zeolite Inorganic materials 0.000 description 6
- 229910052793 cadmium Inorganic materials 0.000 description 6
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 6
- 229910052745 lead Inorganic materials 0.000 description 6
- 239000010813 municipal solid waste Substances 0.000 description 6
- 238000007711 solidification Methods 0.000 description 6
- 230000008023 solidification Effects 0.000 description 6
- 239000010457 zeolite Substances 0.000 description 6
- 229910052725 zinc Inorganic materials 0.000 description 6
- 239000004568 cement Substances 0.000 description 5
- 229910052802 copper Inorganic materials 0.000 description 5
- 239000010949 copper Substances 0.000 description 5
- 238000005260 corrosion Methods 0.000 description 5
- 229910052809 inorganic oxide Inorganic materials 0.000 description 5
- 229910052748 manganese Inorganic materials 0.000 description 5
- 229910052759 nickel Inorganic materials 0.000 description 5
- 230000007797 corrosion Effects 0.000 description 4
- 239000008247 solid mixture Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000033228 biological regulation Effects 0.000 description 3
- 239000006210 lotion Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- RSWGJHLUYNHPMX-ONCXSQPRSA-N abietic acid Chemical compound C([C@@H]12)CC(C(C)C)=CC1=CC[C@@H]1[C@]2(C)CCC[C@@]1(C)C(O)=O RSWGJHLUYNHPMX-ONCXSQPRSA-N 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 239000010426 asphalt Substances 0.000 description 2
- 239000010882 bottom ash Substances 0.000 description 2
- 239000013043 chemical agent Substances 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 229940058401 polytetrafluoroethylene Drugs 0.000 description 2
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 2
- 239000004810 polytetrafluoroethylene Substances 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 238000004056 waste incineration Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 229910000323 aluminium silicate Inorganic materials 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000002738 chelating agent Substances 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 230000000185 dioxinlike effect Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000001027 hydrothermal synthesis Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000010309 melting process Methods 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 231100000004 severe toxicity Toxicity 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
-
- 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
- C02F2101/20—Heavy metals or heavy metal compounds
-
- 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
- C02F2101/30—Organic compounds
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention relates to a cooperative treatment method for refuse incineration fly ash and refuse leachate. According to the cooperative treatment method for the refuse incineration fly ash and the refuse leachate, a solvent which has quite high oxidation performance in the subcritical state or the critical state is used for simultaneous treatment of dioxin in the fly ash, the flay ash and heavy metal and organic pollutants in the refuse leachate. Under the alkaline hydrothermal condition, carbon, aluminum and silicon matter in the refuse incineration fly ash can easily synthesize a zeolite-like structure, so that a large amount of heavy metal in the fly ash is adsorbed into pores of the zeolite-like structure, and therefore the leaching toxicity of the heavy metal in the fly ash is lowered. Under the hydrothermal condition, along with continuous rising of the temperature and the pressure in a sealed reactor, the water solubility of the dioxin is greatly improved, the reactivity is improved beneficially, and oxidation and decomposition of the dioxin are accelerated.
Description
Technical field
The present invention relates to a kind of method processing incineration of refuse flyash and percolate, more particularly to a kind of collaborative place
Reason incineration of refuse flyash and the method for percolate, dioxin and a huge sum of money in especially a kind of collaborative process incineration of refuse flyash
The method of organic pollution and heavy metal in genus, percolate.
Background technology
Incineration of refuse flyash is the material collected in pick up the heat system, flue gas purification system after waste incineration.Mainly
The dust that bottom ash, the bottom ash of reaction tower generation and the sack cleaner producing from waste heat boiler is collected.Wherein contain substantial amounts of
The severe toxicity pollutant such as heavy metal and dioxin, belong to the hazardous waste (numbering of national regulation：HW18) it is necessary to carry out safe place
Put.
The key property of flying dust is also the difficult point disposed is containing dioxin, heavy metal, and solvable chloride content is high.Fly
Grey fine size, the dioxin that waste incineration produces has greatly absorption in ash surface.Meanwhile, also contain in flying dust higher
(as Pb content is up to 750～3500mg/kg, Zn content is up to 900 to multiple harmful heavy metal such as Pb, Zn, Cr and Cd of concentration
～3500mg/kg).And, it is the key factor of restriction flying dust disposal containing substantial amounts of solvable villaumite in incineration of refuse flyash, its
Content reaches as high as more than 25%.
Flying ash method of disposal mainly has：Cement solidification method, bitumen solidification method, chemical agent process, sintering are disposed
Method and melting process etc..
Cement solidification method in the presence of carbonating (acidifying), heavy metal in firming body and inorganic salt most of with when
Between passage long-term, potential threat will be had by rainwater gradually dissolution to environment.Dispose in view of these problem flying dusts
Field is built and the standard of operation will greatly improve, increase-volume after cement solidification, and operating cost increases, and limits answering for a long time of the method
With.
Bitumen solidification method it is necessary to suitably be adjusted the size of flying dust and moisture, is use up in disposal process simultaneously
Amount goes the removal of impurity, to enable the clad of Colophonium that place glove is completely covered.Disposing capacity is low, and Colophonium usage amount is big, cost
Height is it is more difficult to be promoted use.
When processing not homogenized flying dust, dispose according to chemical agent process, then high-molecular chelating agent adds into
This meeting is of a relatively high.Due to the complexity of flying dust component and heavy metal existing forms, and its reaction mechanism is lacked enough
Understanding and research, therefore, mix the genuine with the fictitious in stabilizer market, level is uneven.
At present, the domestic garbage burning factory except main cities such as Shanghai, Guangzhou, Shenzhen, Dalian is carried out to flying ash
Outside safe disposal, most of garbage burning factories also do not carry out necessary appropriate disposal to flying ash.Common mode is
By the way of Simple cement solidification and lime stabilization, but the effect of these disposal options heavy metal long term stabilizations is not
Ideal, removal and control action to dioxin-like chemical are also very limited, so that lime stabilizationization is disposed as a example, in low ph environment
Middle heavy metal can leach once again, and causes secondary pollution.
Percolate refers to the moisture, the sleet water of entrance landfill yard that rubbish contains in itself in refuse landfill
And other moisture, deduction rubbish, the saturation moisture capacity of overburden layer, and a kind of high concentration experiencing waste layer and overburden layer and being formed
Waste water.The water quality of percolate is considerably complicated, typically contains high-enriched organics, heavy metallic salt and ammonia nitrogen, percolate
Not only contaminated soil and earth surface water source, also can pollute to subsoil water, for COD in percolate and ammonia nitrogen removal
There is many research, typically adopt bioanalysises to dispose more, but disposal effect is undesirable, and operating cost is of a relatively high.
Under normal conditions, both garbages are all to process respectively, so processing cost is high, Treatment Stability is low.Cause
This, find a kind of handling process, processing equipment simply, processing cost is cheap, and the technique of obvious processing effect just seems outstanding
For important.
Content of the invention
The purpose of the present invention is to propose to a kind of handling process, processing equipment is simple, processing cost is cheap, obvious processing effect
Technique, organic pollution and heavy metal in dioxin and heavy metal, percolate in process flying dust can be worked in coordination with, realize rubbish
Rubbish flying ash and the harmlessness disposing of percolate, rationally, cost of disposal is moderate for handling process, disposes effect is significant.
For achieving the above object, the invention provides a kind of collaborative side processing incineration of refuse flyash and percolate
Method, methods described comprises the steps：
A, by flying dust according to solid-liquid mass ratio be 1:3～1:10 ratio is added to the water, with 300～3000r/min's
Rotating speed stirs 20min～60min, carries out solid-liquid separation afterwards on centrifuge；
B, the solid content that step A is isolated and percolate are by 1:3～1:15 solid-liquid mass ratio example mixing, stirring
Uniformly, form solidliquid mixture；
Silicon oxide, aluminium oxide, the mixture of calcium oxide is added in C, solidliquid mixture in stepb；
D, by step C mixture add reactor in, check air-tightness, determine reactor air-tightness well after temperature
Degree parameter regulation is to 120～350 DEG C, and the pressure of reactor is set to 1.5～17.0Mpa；
E, it is stirred continuously, after the temperature in reactor is increased to the temperature value of setting, continue reaction 1～10h；
F, by process after mixture carry out solid-liquid separation, afterwards again dehydration after solidss carry out harmless treatment
Or recycling.
Preferably, the washing-separation process of repeating said steps A 1～2 time.
Preferably, in described step B, silicon oxide, aluminium oxide, the mass content of calcium oxide are 1～10%.
Preferably, the heating rate of described reactor is 1～10 DEG C/min.
Preferably, described reactor is pressure reactor, and described reactor inner materials are rustless steel, ceramic or polytetrafluoro
Ethylene, outside material is cast iron.
Preferably, the device with automatic stirring in described reactor, constantly at the uniform velocity stirs solid-liquid in heating process
Mixture.
Preferably, the solid-liquid separation method in step F is mechanism filter-pressing dehydration or centrifuge dehydration.
Preferably, process according to methods described, when the content of silicon oxide in step B, aluminium oxide, calcium oxide is flying dust quality
1～5% when, the international toxicity equivalent of the flying dust after process is less than 0.5ng I-TEQ/g.
Preferably, process according to methods described, when the temperature setting of reactor is 220 DEG C～350 DEG C, flying after process
The international toxicity equivalent of ash is less than 0.3ng I-TEQ/g.
Preferably, when processing flying dust and percolate, solvent is in subcritical or critical state to reactor.
Based on technique scheme, it is an advantage of the invention that：
The invention provides a kind of collaborative process in dioxin and heavy metal, percolate in flying dust organic pollution and
The method of heavy metal, has extremely strong oxidisability using the solvent being under subcritical or critical state, processes flying dust simultaneously
In dioxin and the heavy metal in flying dust and percolate and organic pollution.Meanwhile, the handling process of the present invention,
Processing equipment is simple, and processing cost is cheap, and the method for the present invention is high to the treatment effeciency of dioxin and organic pollution,
Heavy metal ion has stronger stability after treatment so that the solidss after processing can achieve harmless treatment or resource
Change and utilize.
Further, the method for the present invention, by washing out chlorine element in flying dust and inorganic salt, is dissolved in water lotion, reduces
The corrosion to equipment for the villaumite, and to inorganic salt efficient recovery, realize resource circulation utilization.Supplement can form class zeolite knot simultaneously
The necessary material of structure, the such as material such as silicon oxide, aluminium oxide, calcium oxide, the harmful substance such as zeolite structured adsorbable heavy metal of class in
In space, reduce Leaching Heavy Metals.
Specific embodiment
Below by embodiment, technical scheme is described in further detail.
The invention provides a kind of collaborative method processing incineration of refuse flyash and percolate, methods described include as
Lower step：
A, by flying dust according to solid-liquid mass ratio be 1:3～1:10 ratio is added to the water, with 300～3000r/min's
Rotating speed stirs 20min～60min, carries out solid-liquid separation afterwards on centrifuge.Preferably, repeat described step A washing-
Separation process 1～2 time, to improve washing efficiency.After 3 washings, the washing rate of chlorine can reach more than 99%, the corruption to equipment
Corrosion significantly reduces, and significantly extends the service life of reactor.By washing out chlorine element in flying dust and inorganic salt, it is dissolved into
In water lotion, reduce the corrosion to equipment for the villaumite, and to inorganic salt efficient recovery, realize resource circulation utilization.
B, the solid content that step A is isolated and percolate are by 1:3～1:15 solid-liquid mass ratio example mixing, stir
Mix uniformly, form solidliquid mixture；In order to obtain preferably treatment effect, the alcohols materials such as methanol can be added wherein, also may be used
Add the materials such as copper powder, iron powder, metal-oxide, as catalyst, to accelerate reaction rate, cost-effective.
Silicon oxide, aluminium oxide, the mixture of calcium oxide is added in C, solidliquid mixture in stepb.Preferably, described
The ratio that silicon oxide in step B, aluminium oxide, the content of calcium oxide account for flying dust quality is 1～5%.Permissible by supplementing simultaneously
Form the zeolite structured necessary material of class, the such as material such as silicon oxide, aluminium oxide, calcium oxide, the zeolite structured adsorbable heavy metal of class
Deng harmful substance in space, reduce Leaching Heavy Metals.
D, by step C mixture add reactor in, check air-tightness, determine reactor air-tightness well after temperature
Degree parameter regulation is to 120～350 DEG C, and the pressure of reactor is set to 1.5～17.0Mpa.During the intensification of described reactor,
Its heating rate is 1～10 DEG C/min.And the device with automatic stirring in described reactor, can be in heating process
Constantly at the uniform velocity stirring solidliquid mixture, so that solidliquid mixture is heated evenly, fully reacts.Pressure and anti-corrosion due to having
Erosion requires it is preferable that described reactor is pressure reactor, and described reactor inner materials are rustless steel, ceramic or polytetrafluoro
Ethylene, outside material is cast iron.
E, it is stirred continuously, after the temperature in reactor is increased to the temperature value of setting, continue reaction 1～10h.Close and add
Hot device, naturally cools to room temperature.When processing flying dust and percolate, solvent is in subcritical or critical shape to reactor
State.It is in subcritical or critical state solvent there is extremely strong oxidisability just because of this, so that it can decompose
Dioxin.Meanwhile, after hydro-thermal reaction, the heavy metal in flying dust and percolate is defined with the silicate in flying dust
There are other aluminosilicates of rock-steady structure, so that the Leaching of heavy metal is reduced.
F, by process after mixture carry out solid-liquid separation, afterwards again dehydration after solidss carry out harmless treatment
Or recycling.Preferably, described solid-liquid separation method is mechanism filter-pressing dehydration or centrifuge dehydration.Solidss after dehydration
Can directly fill or be mixed into cement landfill, its toxicity is very low, complies fully with state specified standards it is also possible to be mixed into coagulation
Soil, carries out recycling.
The invention provides a kind of collaborative process in dioxin and heavy metal, percolate in flying dust organic pollution and
The method of heavy metal, has extremely strong oxidisability using the solvent being under subcritical or critical state, processes flying dust simultaneously
In dioxin and the heavy metal in flying dust and percolate and organic pollution.Preferably, process according to methods described, when
When the temperature setting of reactor is 220 DEG C～350 DEG C, the international toxicity equivalent of the flying dust after process is less than 0.3ng I-
TEQ/g.
Further, the method for the present invention, by washing out chlorine element in flying dust and inorganic salt, is dissolved in water lotion, reduces
The corrosion to equipment for the villaumite, and to inorganic salt efficient recovery, realize resource circulation utilization.Supplement can form class zeolite knot simultaneously
The necessary material of structure, the such as material such as silicon oxide, aluminium oxide, calcium oxide, the harmful substance such as zeolite structured adsorbable heavy metal of class in
In space, reduce Leaching Heavy Metals.Preferably, process according to methods described, when silicon oxide, aluminium oxide, oxidation in step B
When the content of calcium is the 1～5% of flying dust quality, the international toxicity equivalent of the flying dust after process is less than 0.5ng I-TEQ/g.
Embodiment 1
In the present embodiment, by flying dust according to solid-liquid mass ratio be 1:6 ratio is added to the water, with 2000r/min's
Rotating speed stirs 20min, carries out solid-liquid separation afterwards on centrifuge, and washing times are 3 times, and the washing rate of chlorine can reach 99%.
Afterwards, add inorganic oxide in the flying dust toward after washing, oxide uses calcium oxide, silicon oxide, addition is flying dust matter
The 5% of amount, will mix solid content and press 1 with percolate:4 solid-liquid ratio mixing, the temperature setting of reactor is 250 DEG C,
Process 3h in a kettle..
Flying dust dioxin decrement more than 96.66% after treatment, the heavy metal such as Mn, Ni, Cu, Zn, Cd, Pb, process
Efficiency is respectively 96.35%, 97.56%, 96.25%, 98.59%, 97.22%, 96.81%, and treatment effeciency all reaches
More than 96%, show excellent treatment effect.
Embodiment 2
In the present embodiment, by flying dust according to solid-liquid mass ratio be 1:4 ratio is added to the water, with 2000r/min's
Rotating speed stirs 20min, carries out solid-liquid separation afterwards on centrifuge, and washing times are 2 times, and the washing rate of chlorine can reach 93%.
Afterwards, add inorganic oxide in the flying dust toward after washing, oxide uses calcium oxide, silicon oxide, addition is flying dust matter
The 3% of amount, solid mixture is pressed 1 with percolate:4 solid-liquid ratio mixing, the temperature setting of reactor is 300 DEG C,
Process 3h in a kettle..
Flying dust dioxin decrement more than 98.12% after treatment, the heavy metal such as Mn, Ni, Cu, Zn, Cd, Pb, process
Efficiency is respectively 97.12%, 97.35%, 97.25%, 97.86%, 97.28%, 98.16%, and treatment effeciency all reaches
More than 97%, show excellent treatment effect.
Embodiment 3
In the present embodiment, by flying dust according to solid-liquid mass ratio be 1:8 ratio is added to the water, with 2000r/min's
Rotating speed stirs 20min, carries out solid-liquid separation afterwards on centrifuge, and washing times are 2 times, and the washing rate of chlorine can reach 98%.
Afterwards, add inorganic oxide in the flying dust toward after washing, oxide uses calcium oxide, silicon oxide, addition is flying dust matter
The 4% of amount, solid mixture is pressed 1 with percolate:15 solid-liquid ratio mixing, the temperature setting of reactor is 275 DEG C,
Process 5h in a kettle..
Flying dust dioxin decrement more than 98.50% after treatment, the heavy metal such as Mn, Ni, Cu, Zn, Cd, Pb, process
Efficiency is respectively 98.62%, 97.12%, 98.10%, 98.02%, 97.22%, 98.16%, and treatment effeciency all reaches
More than 97%, show excellent treatment effect.
Embodiment 4
In the present embodiment, by flying dust according to solid-liquid mass ratio be 1:10 ratio is added to the water, with 2000r/min's
Rotating speed stirs 20min, carries out solid-liquid separation afterwards on centrifuge, and washing times are 3 times, and the washing rate of chlorine can reach 99%.
Afterwards, add inorganic oxide in the flying dust toward after washing, oxide uses calcium oxide, silicon oxide, addition is flying dust matter
The 5% of amount, solid mixture is pressed 1 with percolate:3 solid-liquid ratio mixing, the temperature setting of reactor is 280 DEG C,
Process 4h in a kettle..
In the processing mode described in embodiment 1, the waste liquid after process, dioxin decrement more than 95.12%, Mn,
The heavy metals such as Ni, Cu, Zn, Cd, Pb, treatment effeciency be respectively 95.12%, 96.35%, 96.25%, 96.95%, 96.22%,
96.01%, treatment effeciency has all reached more than 95%, shows excellent treatment effect.
Embodiment 5
In the present embodiment, by flying dust according to solid-liquid mass ratio be 1:3 ratio is added to the water, with 2000r/min's
Rotating speed stirs 20min, carries out solid-liquid separation afterwards on centrifuge, and washing times are 2 times, and the washing rate of chlorine can reach 96%.
Afterwards, add inorganic oxide in the flying dust toward after washing, oxide uses calcium oxide, silicon oxide, addition is flying dust matter
The 2% of amount, solid mixture is pressed 1 with percolate:4 solid-liquid ratio mixing, the temperature setting of reactor is 350 DEG C,
Process 3h in a kettle..
In the processing mode described in embodiment 1, the waste liquid after process, dioxin decrement more than 97.36%, Mn,
The heavy metals such as Ni, Cu, Zn, Cd, Pb, treatment effeciency be respectively 97.52%, 97.25%, 97.56%, 98.20%,
96.262%th, 97.81%, treatment effeciency has all reached more than 97%, shows excellent treatment effect.
Finally it should be noted that:Above example is only not intended to limit in order to technical scheme to be described；To the greatest extent
Pipe has been described in detail to the present invention with reference to preferred embodiment, and those of ordinary skill in the art should be understood：Still
The specific embodiment of the present invention can be modified or equivalent is carried out to some technical characteristics；Without deviating from this
The spirit of bright technical scheme, it all should be covered in the middle of the technical scheme scope that the present invention is claimed.
Claims (10)
1. a kind of collaborative method processing incineration of refuse flyash and percolate it is characterised in that：Methods described includes as follows
Step：
A, by flying dust according to solid-liquid mass ratio be 1:2～1:10 ratio is added to the water, with the rotating speed of 300～3000r/min
Stirring 20min～60min, carries out solid-liquid separation afterwards on centrifuge；
B, the solid content that step A is isolated and percolate are by 1:3～1:15 solid-liquid mass ratio example mixing, stirring is all
Even, form solidliquid mixture；
Silicon oxide, aluminium oxide, the mixture of calcium oxide is added in C, solidliquid mixture in stepb；
D, by step C mixture add reactor in, check air-tightness, determine that reactor air-tightness after good is joined temperature
Number is adjusted to 120～350 DEG C, and the pressure of reactor is set to 1.5～7.0Mpa；
E, it is stirred continuously, after the temperature in reactor is increased to the temperature value of setting, continue reaction 1～10h；
F, by process after mixture carry out solid-liquid separation, afterwards again dehydration after solidss carry out harmless treatment or
Recycling.
2. method according to claim 1 it is characterised in that：Washing-the separation process of repeating said steps A 1～2 time.
3. method according to claim 1 it is characterised in that：The matter of silicon oxide, aluminium oxide, calcium oxide in described step B
Amount content is 1～10%.
4. method according to claim 1 it is characterised in that：The heating rate of described reactor is 1～10 DEG C/min.
5. method according to claim 1 it is characterised in that：Described reactor is pressure reactor, in described reactor
Portion's material is rustless steel, ceramic or politef, and outside material is cast iron.
6. method according to claim 1 it is characterised in that：Device with automatic stirring in described reactor, is adding
Solidliquid mixture is constantly at the uniform velocity stirred in thermal process.
7. method according to claim 1 it is characterised in that：Solid-liquid separation method in step F is dehydrated for mechanism filter-pressing
Or centrifuge dehydration.
8. method according to claim 1 it is characterised in that：Process according to methods described, when silicon oxide, oxygen in step B
When change aluminum, the content of calcium oxide are the 1～5% of flying dust quality, the international toxicity equivalent of the flying dust after process is less than 0.5ng
I-TEQ/g.
9. method according to claim 1 it is characterised in that：Process according to methods described, when the temperature setting of reactor
During for 220 DEG C～350 DEG C, the international toxicity equivalent of the flying dust after process is less than 0.3ng I-TEQ/g.
10. method according to claim 1 it is characterised in that：Reactor is processing flying dust and during percolate, solvent
It is in subcritical or critical state.
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| CN108721824A (en) * | 2018-05-22 | 2018-11-02 | 重庆大学 | The method of incineration of refuse flyash synchronism stability heavy metal and degrading polycyclic aromatic hydrocarbons |
| CN112893416A (en) * | 2021-02-05 | 2021-06-04 | 南京理工大学 | Recycling method of fly ash and fly ash hydrothermal treatment fluid |
| CN113458127A (en) * | 2021-08-12 | 2021-10-01 | 杭州灰弘环保科技有限公司 | Cooperative disposal method for household garbage incineration fly ash and pyrite tailing |
| CN114904898A (en) * | 2022-06-02 | 2022-08-16 | 天津中材工程研究中心有限公司 | System and method for self-enriching dioxin in fly ash |
| CN115106373A (en) * | 2022-06-14 | 2022-09-27 | 光大环境科技（中国）有限公司 | Treatment process of secondary fly ash in plasma melting of household garbage incineration fly ash |
| CN116813374A (en) * | 2022-12-14 | 2023-09-29 | 张锦彬 | Ceramic manufactured by fly ash of garbage power plant |
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| CN108721824A (en) * | 2018-05-22 | 2018-11-02 | 重庆大学 | The method of incineration of refuse flyash synchronism stability heavy metal and degrading polycyclic aromatic hydrocarbons |
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| CN112893416A (en) * | 2021-02-05 | 2021-06-04 | 南京理工大学 | Recycling method of fly ash and fly ash hydrothermal treatment fluid |
| CN113458127A (en) * | 2021-08-12 | 2021-10-01 | 杭州灰弘环保科技有限公司 | Cooperative disposal method for household garbage incineration fly ash and pyrite tailing |
| CN114904898A (en) * | 2022-06-02 | 2022-08-16 | 天津中材工程研究中心有限公司 | System and method for self-enriching dioxin in fly ash |
| CN115106373A (en) * | 2022-06-14 | 2022-09-27 | 光大环境科技（中国）有限公司 | Treatment process of secondary fly ash in plasma melting of household garbage incineration fly ash |
| CN115106373B (en) * | 2022-06-14 | 2023-05-02 | 光大环境科技（中国）有限公司 | Disposal process for secondary fly ash in plasma melting of household garbage incineration fly ash |
| CN116813374A (en) * | 2022-12-14 | 2023-09-29 | 张锦彬 | Ceramic manufactured by fly ash of garbage power plant |
| CN116813374B (en) * | 2022-12-14 | 2024-04-09 | 张锦彬 | Ceramic manufactured by fly ash of garbage power plant |
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Application publication date: 20170215 |