CN107159684B - Domestic waste incineration fly ash and waste SCR catalyst co-treatment method - Google Patents
Domestic waste incineration fly ash and waste SCR catalyst co-treatment method Download PDFInfo
- Publication number
- CN107159684B CN107159684B CN201710517227.7A CN201710517227A CN107159684B CN 107159684 B CN107159684 B CN 107159684B CN 201710517227 A CN201710517227 A CN 201710517227A CN 107159684 B CN107159684 B CN 107159684B
- Authority
- CN
- China
- Prior art keywords
- fly ash
- catalytic oxidation
- waste
- oxidation device
- gas
- 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.)
- Expired - Fee Related
Links
- 239000010881 fly ash Substances 0.000 title claims abstract description 235
- 239000003054 catalyst Substances 0.000 title claims abstract description 95
- 239000002699 waste material Substances 0.000 title claims abstract description 94
- 238000000034 method Methods 0.000 title claims abstract description 52
- 238000011278 co-treatment Methods 0.000 title claims description 8
- 239000010791 domestic waste Substances 0.000 title claims description 6
- 238000004056 waste incineration Methods 0.000 title description 11
- 230000003197 catalytic effect Effects 0.000 claims abstract description 127
- 230000003647 oxidation Effects 0.000 claims abstract description 125
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 125
- 239000007789 gas Substances 0.000 claims abstract description 70
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 49
- 238000010438 heat treatment Methods 0.000 claims abstract description 39
- 239000002912 waste gas Substances 0.000 claims abstract description 17
- 230000000087 stabilizing effect Effects 0.000 claims description 15
- 239000002956 ash Substances 0.000 claims description 13
- 238000001723 curing Methods 0.000 claims description 13
- 230000008569 process Effects 0.000 claims description 11
- 239000000126 substance Substances 0.000 claims description 11
- 239000004568 cement Substances 0.000 claims description 10
- 229910001385 heavy metal Inorganic materials 0.000 claims description 10
- 231100000053 low toxicity Toxicity 0.000 claims description 8
- 230000002195 synergetic effect Effects 0.000 claims description 8
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 7
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 7
- 239000004571 lime Substances 0.000 claims description 7
- 230000009471 action Effects 0.000 claims description 6
- 238000000354 decomposition reaction Methods 0.000 claims description 6
- 239000002245 particle Substances 0.000 claims description 6
- 239000003814 drug Substances 0.000 claims description 5
- 239000005416 organic matter Substances 0.000 claims description 5
- 229910001220 stainless steel Inorganic materials 0.000 claims description 5
- 239000010935 stainless steel Substances 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 2
- 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 claims 1
- 238000003672 processing method Methods 0.000 claims 1
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 69
- 238000005516 engineering process Methods 0.000 description 36
- 238000002474 experimental method Methods 0.000 description 17
- 230000015556 catabolic process Effects 0.000 description 14
- 238000006731 degradation reaction Methods 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 12
- 230000000694 effects Effects 0.000 description 12
- 230000006872 improvement Effects 0.000 description 7
- 239000002957 persistent organic pollutant Substances 0.000 description 7
- 238000007711 solidification Methods 0.000 description 7
- 230000008023 solidification Effects 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 150000002013 dioxins Chemical class 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- 239000000428 dust Substances 0.000 description 5
- 239000003546 flue gas Substances 0.000 description 5
- 230000008018 melting Effects 0.000 description 5
- 238000002844 melting Methods 0.000 description 5
- 239000000779 smoke Substances 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 231100000770 Toxic Equivalency Factor Toxicity 0.000 description 4
- 238000002144 chemical decomposition reaction Methods 0.000 description 4
- 230000007423 decrease Effects 0.000 description 4
- 239000003344 environmental pollutant Substances 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000006722 reduction reaction Methods 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000006298 dechlorination reaction Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000000593 degrading effect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 239000002920 hazardous waste Substances 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000011159 matrix material Substances 0.000 description 2
- 230000000813 microbial effect Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 238000005303 weighing Methods 0.000 description 2
- 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
- 229910010413 TiO 2 Inorganic materials 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 239000002671 adjuvant Substances 0.000 description 1
- 239000010426 asphalt Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 238000005538 encapsulation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 239000010814 metallic waste Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229920000620 organic polymer Polymers 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 230000001699 photocatalysis Effects 0.000 description 1
- 238000001782 photodegradation Methods 0.000 description 1
- 238000006303 photolysis reaction Methods 0.000 description 1
- 230000015843 photosynthesis, light reaction Effects 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000009284 supercritical water oxidation Methods 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
Images
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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8659—Removing halogens or halogen compounds
- B01D53/8662—Organic halogen compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/22—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention provides a household garbage incineration fly ash and waste SCR catalyst cooperative treatment system, which comprises an ozone generating device, a fly ash catalytic oxidation device and the like, wherein a gas inlet, a fly ash inlet, a gas outlet and a fly ash outlet are formed in the fly ash catalytic oxidation device, a gas inlet and a gas outlet are formed in the waste SCR catalytic oxidation device, the gas inlet is communicated with the ozone generating device, the gas outlet is communicated with a gas inlet of the waste SCR catalytic oxidation device, the fly ash outlet is communicated with a fly ash collecting device, a spiral blade and a fly ash heating device are respectively arranged in an inner cavity of the fly ash catalytic oxidation device, a catalyst component is arranged in the waste SCR catalytic oxidation device, and a waste gas heating device is arranged in an inner cavity of the waste SCR catalytic oxidation device. The invention also provides a method for cooperatively treating the incineration fly ash of the household garbage and the waste SCR catalyst by using the treatment system.
Description
Technical Field
The invention belongs to the technical field of environmental protection, and mainly relates to a system and a method for cooperatively treating household garbage incineration fly ash and a waste SCR catalyst.
Background
Currently, the disposal of household garbage has become a significant social problem. The annual output of municipal domestic waste in China exceeds 1.5 hundred million tons, the harmless treatment rate is only about 54 percent, and great threats are caused to the ecological environment and the health of people. Because the domestic garbage incineration treatment speed is high, the occupied area is small, and the reduction and harmless effects are obvious, the method is widely applied to medium and large-sized cities which are generally short in urban land and have high domestic garbage treatment pressure in China. However, the fly ash, which is the residue after the incineration of the household garbage, usually contains toxic and harmful pollutants such as dioxin, heavy metals and the like, and the treatment and disposal of the fly ash become one of the key problems which disturb the popularization of the garbage incineration technology, and become important factors which restrict the development of the garbage incineration power generation technology.
Sources of dioxins are numerous, with waste incineration being an important source of dioxin emissions. The emission situation in europe, the usa and japan shows that the proportion of dioxin emission as an incineration source is high. The emission amount of incineration-derived dioxins still accounts for 63% of the total emission amount in 2004 in japan. According to the domestic published experimental data, the dioxin emission of domestic garbage incineration in China is estimated, and if the incinerator is operated for 330 days in a year, the smoke yield of domestic garbage incineration is 5 Nm & lt 500 & gtNm 3 The yield of the fly ash is 3 percent, and the dioxin in the flue gas reaches 1.0 ng (I-TEQ)/m of the national standard 3 And the dioxin in the fly ash is 2.0 ng (I-TEQ)/g, so that the total amount of dioxin discharged to the atmosphere by domestic garbage incineration in China at present is about 54.45 g (I-TEQ)/a, and the total amount of dioxin discharged by the fly ash is about 594.0 g (I-TEQ)/a, which is equivalent to 10 times of the emission amount of smoke. Therefore, the treatment and disposal of dioxin in incineration fly ash are particularly important.
Dioxin generated in the waste incineration process is mainly concentrated in smoke and fly ash, wherein the control technology for the dioxin in the smoke comprises the following steps: and (1) activated carbon adsorption and high-efficiency dust removal. The activated carbon has huge specific surface area and good adsorbability, and can adsorb gaseous and solid dioxin. At present, in a flue gas purification system, activated carbon powder is generally injected into a front-section pipeline of a dust remover to adsorb dioxin in flue gas, and the dioxin is collected by the dust remover at the downstream. However, the activated carbon adsorption technology is essentially to trap and separate dioxin, transfer the dioxin to a solid phase (fly ash, activated carbon), and the activated carbon adsorbed with dioxin needs further harmless treatment, and the technology has no effect of reducing the total amount of dioxin. And (2) Selective Catalytic Reduction (SCR). SCR is widely used in coal-fired power plants to oxidize and reduce NO in flue gas X The function of (1). At present, SCR is installed in part of waste incineration facilities, and research shows that the SCR has the function of decomposing dioxin at the same time of denitration, and the decomposition product is CO 2 、H 2 O and HCl. And (3) advanced oxidation. Research shows that the photocatalytic oxidation is effective in degrading dioxin in a gaseous state, and the degradation rate of the total amount and the toxicity equivalent is over 50 percent. Plasma oxidation is generally concerned due to its strong oxidizing power and good degradation effect. Of the above smoke control technologies, the first two are mature technologies that have been commercially used, and the last two are still in the experimental stage. The first active carbon adsorption and bag dust removal technology are used for trapping and separating dioxin, and no reduction effect is produced on the total amount of the dioxin; the latter three technologies are all gas-phase dioxin in-situ degradation technologies, but have respective defects: in the SCR technology, catalyst poisoning is the key to influencing the stable operation of the SCR technology; the ultraviolet technology has low removal efficiency due to energy efficiency, and the reaction efficiency can be converted into the practical application technology only by further improving the reaction efficiency by other methods; the plasma oxidation technology is likely to be put into commercial popularization only by further improving the stability of the reactor and reducing the equipment and operation costs.
The control technology for dioxin in the fly ash comprises the following steps: (1) high-temperature melting method. The dioxin in the fly ash is thoroughly decomposed and destroyed by the high-temperature environment, so that the aim of reducing the dioxin is fulfilled. The higher the melting temperature, the higher the decomposition rate, while the oxidative atmosphere has a higher decomposition rate than the inert atmosphere. And (2) carrying out low-temperature heat treatment. The method is characterized in that dioxin in fly ash is degraded through two paths of hydrogenation/dechlorination and decomposition in an inert atmosphere or an oxidizing atmosphere at a relatively low temperature range of 300-600 ℃ for a certain treatment time. And (3) supercritical water and hydrothermal degradation. Hydrothermal solution degradation technology is similar to supercritical water oxidation technology, and when water is used as a medium, the temperature is satisfied>374 ℃ and pressure>Supercritical water is obtained at 22.1MPa, in this state, because gas-liquid interface mass transfer resistance does not exist, the reaction efficiency is improved, and complete oxidation is realized, and in the hydrothermal liquid state, the temperature and pressure of water are lower than the above critical values, and in this state, organic matter is dissolved in waterDegree, [ H ] + ]、[OH - ]Significantly increased, and a reaction which could not be performed at normal temperature could occur. And (4) an alkaline chemical decomposition method. The chemical decomposition method is also called BCD method, and is suitable for harmless treatment of soil polluted by dioxin compounds. (5) plasma method. The plasma is divided into thermal plasma and non-thermal plasma according to the property, the thermal plasma is high-temperature plasma, and the high-temperature plasma generates 1400 ℃ high temperature to melt the waste incineration fly ash. The method has extremely high degradation rate on dioxin, and the degradation rate is usually more than 99.9 percent. And (6) carrying out a photolysis method. The property that benzene rings of dioxin molecules can generate dechlorination under the irradiation of ultraviolet light is utilized to carry out photodegradation treatment on the dioxin. And (7) performing a biodegradation method. Dioxins are highly resistant to microbial degradation, and only 5% of microbial strains in nature are capable of decomposing dioxins. (8) mechanochemical method. It is a treatment method in which mechanical energy is applied to a solid, liquid or other condensed substance by means of shearing, friction, impact, extrusion, or the like, to induce changes in the structure and physicochemical properties thereof. The technology for degrading the dioxin in the fly ash is more abundant than the flue gas treatment technology, but the technology for treating the dioxin in the solid phase medium is only that which can be really applied in a large scale: high-temperature melting technology, low-temperature heat treatment and alkaline chemical decomposition. The high-temperature melting technology can decompose dioxin in the fly ash and solidify heavy metals contained in the fly ash at the same time, and has an excellent treatment effect. But the technology has huge energy consumption and expensive equipment cost; the low-temperature heat treatment technology has the degradation rate of more than 90 percent on the fly ash dioxin generally, has lower equipment investment and operation cost, and is put into industrial application in part of waste incineration plants in Japan and Germany; the alkaline chemical decomposition is mainly applied to harmless treatment of soil, the removal rate of dioxin can reach more than 90 percent, but the process is complicated, and NaHCO is required to be added in the middle process 3 And an organic solvent as an additive. Other degradation technologies have defects, so that the other degradation technologies are difficult to be put into industrial application.
The SCR catalyst is a conventional catalyst, and the basic component of the SCR catalyst is V2O5-WO3-TiO2. It is generally considered that when the catalytic activity of the SCR catalyst drops to 80% of the original activity, the catalyst is considered to have been deactivated and become a waste SCR catalyst. There are two main ways of treating the current waste SCR catalyst: (1) The catalyst is directly discarded as dangerous waste, and accounts for about 70 percent of the total catalyst; (2) After pretreatment, the product is recovered, for example, by washing with water, drying, and crushing, and is reused in the preparation of a new catalyst, which accounts for about 30% of the total catalyst. The utilization efficiency of the SCR catalyst is low.
Therefore, improvements in the prior art are needed.
Disclosure of Invention
The invention aims to provide an efficient system and an efficient method for co-processing household garbage incineration fly ash and a waste SCR catalyst.
In order to solve the technical problem, the invention provides a household garbage incineration fly ash and waste SCR catalyst cooperative treatment system which comprises a fly ash feeding device, an ozone generating device, a fly ash catalytic oxidation device, a waste SCR catalytic oxidation device and a fly ash collecting device; the fly ash catalytic oxidation device is provided with a gas inlet, a fly ash inlet, a gas outlet and a fly ash outlet; the waste SCR catalytic oxidation device is provided with an air inlet and an air outlet; the gas inlet is communicated with the ozone generating device, the gas outlet is communicated with the gas inlet of the waste SCR catalytic oxidation device, and the fly ash outlet is communicated with the fly ash collecting device;
the inner cavity of the fly ash catalytic oxidation device is respectively provided with a helical blade and a fly ash heating device;
the fly ash feeding device comprises an ash bucket and a fly ash quantitative feeder communicated with a discharge hole of the ash bucket; the fly ash quantitative feeder is communicated with the fly ash inlet;
at least one catalyst assembly is arranged in the waste SCR catalytic oxidation device, and the catalyst assembly is connected with the inner wall of the waste SCR catalytic oxidation device; and a waste gas heating device is arranged in the inner cavity of the waste SCR catalytic oxidation device.
As an improvement of the co-treatment system of the household garbage incineration fly ash and the waste SCR catalyst, the invention comprises the following steps: and an induced draft fan is arranged on the gas outlet of the waste SCR catalytic oxidation device.
As a further improvement of the co-treatment system of the household garbage incineration fly ash and the waste SCR catalyst, the invention comprises the following steps: the waste SCR catalytic oxidation device is provided with an opening which can be opened and closed and is matched with the catalyst assembly, and the catalyst assembly is inserted into or pulled out of the opening.
As a further improvement of the co-treatment system of the household garbage incineration fly ash and the waste SCR catalyst, the invention comprises the following steps: the catalyst assembly consists of a catalyst layer consisting of waste SCR catalysts and porous stainless steel plates arranged on two sides of the catalyst layer, the thickness of the catalyst layer is 5-10mm, and the pore diameter of each porous stainless steel plate is 0.3-0.4mm; the waste SCR catalyst is a particle with the particle size of 0.5-1mm.
The invention also provides a method for the synergistic treatment of the household garbage incineration fly ash and the waste SCR catalyst, which comprises the following steps:
the fly ash is added into a fly ash quantitative feeder through an ash hopper, and the fly ash quantitative feeder adds the fly ash into a fly ash catalytic oxidation device through a fly ash inlet; meanwhile, the ozone generating device generates ozone, and the ozone enters the fly ash catalytic oxidation device from the gas inlet;
the fly ash and the ozone are stirred and mixed by the helical blades in the fly ash catalytic oxidation device and move to the gas outlet and the fly ash outlet slowly, and dioxin organic matters contained in the fly ash are degraded into CO by catalytic oxidation of the ozone in the process 2 、H 2 O and HCl, or low molecular weight and low toxicity organic matter decomposed into gas;
the fly ash treated by the fly ash catalytic oxidation device enters the fly ash collecting device through a fly ash outlet, the waste gas treated by the fly ash catalytic oxidation device enters the waste SCR catalytic oxidation device through a gas outlet and an air inlet, and gaseous organic matters in the waste gas are finally degraded into harmless CO through catalytic oxidation of a catalyst layer in the waste SCR catalytic oxidation device 2 And H 2 And O, discharging the treated clean gas from the gas outlet under the action of the induced draft fan.
The improvement of the method for the synergistic treatment of the fly ash from the incineration of the household garbage and the waste SCR catalyst comprises the following steps: the fly ash treated by the fly ash catalytic oxidation device in the fly ash collecting device is then solidified and stabilized, so that heavy metal substances contained in the treated fly ash are removed.
As a further improvement of the method for the synergistic treatment of the fly ash from the incineration of the household garbage and the waste SCR catalyst, the method comprises the following steps: the residence time of the fly ash in the fly ash catalytic oxidation device is more than 1min, and the adding quantity ratio of the ozone to the fly ash in the fly ash catalytic oxidation device is 0.1 to 0.5g of ozone/kg of fly ash.
As a further improvement of the method for the synergistic treatment of the fly ash from the incineration of the household garbage and the waste SCR catalyst, the method comprises the following steps: the fly ash heating device is used for heating fly ash and ozone in the fly ash catalytic oxidation device, and the heating temperature is 50-90 ℃.
The invention is further improved as the method for the synergistic treatment of the fly ash from the incineration of the household garbage and the waste SCR catalyst: the waste gas heating device is used for heating waste gas in the waste SCR catalytic oxidation device, the heating temperature is 90-200 ℃, and the air speed of gas in the waste SCR catalytic oxidation device is 5000-10000/h.
The invention is further improved as the method for the synergistic treatment of the fly ash from the incineration of the household garbage and the waste SCR catalyst: the curing and stabilizing treatment is a cement curing method, lime curing or a medicament stabilizing method.
The invention has the technical advantages that:
1. the household garbage incineration fly ash and waste SCR catalyst cooperative treatment system and method provided by the invention degrade dioxin organic matters in the household garbage incineration fly ash into harmless or low-toxicity substances by utilizing the catalytic performance of the fly ash and combining ozone oxidation, and then deeply oxidize the low-toxicity substances which are not completely degraded at the front end by utilizing the catalytic oxidation performance of the SCR catalyst, so that the problem of dioxin pollution in the fly ash is finally solved;
2. the waste SCR catalyst is used as a catalyst for deep treatment of the waste gas, so that the recycling of the SCR catalyst is realized, and the utilization efficiency of the SCR catalyst is improved;
3. the catalytic performance of metal substances contained in the fly ash is utilized, and the auxiliary effect of ozone is combined, so that the dioxin in the fly ash is efficiently decomposed in situ, and a new solution is provided for the treatment of the incineration fly ash.
Drawings
The following describes embodiments of the present invention in further detail with reference to the accompanying drawings.
FIG. 1 is a schematic structural diagram of a co-treatment system for fly ash from incineration of domestic waste and waste SCR catalyst;
FIG. 2 is a graph showing the ozone addition amount and the dioxin degradation rate in the fly ash catalytic oxidation apparatus 3;
fig. 3 is a graph showing the reaction temperature and the dioxin degradation rate of the fly ash catalytic oxidation apparatus 3.
Detailed Description
The invention will be further described with reference to specific examples, but the scope of the invention is not limited thereto.
Example 1, a system for co-processing fly ash from incineration of household garbage and waste SCR catalyst, as shown in fig. 1-3, includes an ozone generating device 2, a fly ash feeding device 1, a fly ash catalytic oxidation device 3, a fly ash collecting device 5, and a waste SCR catalytic oxidation device 4. The fly ash catalytic oxidation device 3 is provided with a gas inlet 32, a fly ash inlet 31, a gas outlet 33 and a fly ash outlet 34, and the waste SCR catalytic oxidation device 4 is provided with a gas inlet 41 and a gas outlet 42. The gas inlet 32 is communicated with the ozone generating device 2, the fly ash inlet 31 is communicated with the fly ash feeding device 1, the gas outlet 33 is communicated with the gas inlet 41 of the waste SCR catalytic oxidation device 4, and the fly ash outlet 34 is communicated with the fly ash collecting device 5.
The spiral blade 35 is arranged in the inner cavity of the fly ash catalytic oxidation device 3, and the spiral blade 35 is driven by a self-contained motor, so that fly ash and ozone slowly move from the fly ash inlet 31 to the fly ash outlet 34 in a stirring state; the inner wall of the inner cavity of the fly ash catalytic oxidation device 3 is provided with a fly ash heating device 36, the fly ash heating device 36 is an electric heating layer, the heating temperature is 50-90 ℃, and the fly ash heating device 36 can heat fly ash in the fly ash catalytic oxidation device 3 to strengthen the catalytic oxidation effect. Since ozone decomposes rapidly after exceeding 100 ℃, the temperature of the fly ash heating device 36 is controlled below 90 ℃ to ensure that rapid decomposition of ozone is not caused.
The fly ash feeding device 1 comprises an ash hopper 11 and a fly ash quantitative feeder 12 communicated with a discharge port of the ash hopper 11, the fly ash quantitative feeder 12 comprises a storage bin and a weighing device arranged below the storage bin, the weighing device weighs fly ash in the storage bin, a discharge valve is arranged below the storage bin, the storage bin is communicated with the ash hopper 11, and the discharge valve is communicated with a fly ash inlet 31. The fly ash enters a fly ash quantitative feeder 12 through an ash hopper 11, and the addition amount of the fly ash to the fly ash catalytic oxidation device 3 is controlled by the fly ash quantitative feeder 12.
At least one catalyst component 43 is arranged in the waste SCR catalytic oxidation device 4, the catalyst component 43 comprises a catalyst layer consisting of waste SCR catalysts, the thickness of the catalyst layer is 5-10mm, two sides of the catalyst layer are provided with porous stainless steel plates, and the aperture is 0.3-0.4mm; the waste SCR catalyst is particles with the particle diameter of 0.5 to 1mm, and the component comprises V 2 O 5 、WO 3 And TiO 2 . The granular waste SCR catalyst is obtained by crushing waste blocky waste SCR catalysts, the waste SCR catalysts are SCR catalysts with reduced catalytic activity after long-term use, and cannot achieve due denitration effect, and the replaced SCR catalysts (namely, when the catalytic activity of the SCR catalysts is reduced to 80% of the original catalytic activity, the catalysts are considered to be deactivated and become waste SCR catalysts). The catalyst component 43 adopts a drawer type mode, the catalyst component 43 is connected with the inner wall of the inner cavity of the waste SCR catalytic oxidation device 4, an opening which can be opened and closed and is matched with the catalyst component 43 is arranged on the waste SCR catalytic oxidation device 4, the catalyst component 43 can be inserted into or pulled out of the opening, when the catalyst component 43 needs to be replaced, the fly ash and ozone adding is stopped, and the catalyst component 43 is taken out after the opening is opened; the opening is in a closed state during normal operation, and gas cannot leak out of the opening. The waste SCR catalytic oxidation device 4 is provided with a waste gas heating device 44, the waste gas heating device 44 is a heating layer, the heating temperature is 90-200 ℃, and the waste gas in the waste SCR catalytic oxidation device 4 can be assisted in catalytic oxidation. An induced draft fan 45 is arranged on a gas outlet 42 of the waste SCR catalytic oxidation device 4, the induced draft fan 45 can discharge the treated gas from the gas outlet 42, and the air speed of the gas in a catalyst assembly 43 of the waste SCR catalytic oxidation device 4 is controlled to be 5000-10000/h.
The using process of the invention is as follows:
the fly ash is added into a fly ash quantitative feeder 12 through an ash hopper 11, and the fly ash quantitative feeder 12 controls the fly ash to be added into the fly ash catalytic oxidation device 3 through a fly ash inlet 31; meanwhile, the ozone generating device 2 generates ozone, and the ozone enters the fly ash catalytic oxidation device 3 from the gas inlet 32; the adding quantity ratio of the ozone to the fly ash is 0.1 to 0.5g of ozone/kg of fly ash;
the fly ash and the ozone are stirred and mixed by the helical blades 35 in the fly ash catalytic oxidation device 3 and are pushed to the gas outlet 33 and the fly ash outlet 34, in the process, the fly ash heating device 36 heats for assisting catalytic oxidation (the heating temperature is 50-90 ℃), and the air speed of the gas in the waste SCR catalytic oxidation device 4 is 5000-10000/h. The dioxins organic matter (most) contained in the fly ash is degraded into CO by ozone catalytic oxidation 2 、H 2 O, HCl, etc., or low molecular weight and low toxicity organic substances decomposed into gaseous state (a small portion of dioxin is not catalytically oxidized or decomposed, i.e., the treatment efficiency of dioxin does not reach 100%); the residence time of the fly ash in the fly ash catalytic oxidation device 3 is more than 1min, so that dioxin in the fly ash can be catalytically oxidized as much as possible, and ozone is converted into oxygen at the moment.
The fly ash treated by the fly ash catalytic oxidation device 3 enters the fly ash collecting device 5 through the fly ash outlet 34, and then is subjected to solidification and stabilization treatment, so that heavy metal substances contained in the fly ash are removed; the waste gas treated by the fly ash catalytic oxidation device 3 enters the waste SCR catalytic oxidation device 4 through the gas outlet 33 and the gas inlet 41, and the waste gas heating device 44 assists in catalytic oxidation (the heating temperature is 90-200 ℃, the catalytic activity of the catalyst component 43 is activated after the heating temperature exceeds 90 ℃, the degradation effect is ideal, so that dioxin and other gaseous organic pollutants are not detected in the gas outlet 42 of the waste SCR catalytic oxidation device 4 after the temperature of the waste SCR catalytic oxidation device 4 exceeds 90 ℃). Because the reaction temperature in the fly ash catalytic oxidation device 3 assists catalytic oxidation, part of dioxin organic matters are decomposed into gaseous low-molecular-weight and low-toxicity organic matters, the waste gas from the gas outlet 33 contains other gaseous organic matters, and the gaseous organic matters are gaseous low-toxicity organic mattersLow molecular weight and low toxicity organic matter. The gaseous organic matters enter the waste SCR catalytic oxidation device 4 along with the exhaust gas, are subjected to catalytic oxidation action of the catalyst layer of the catalyst assembly 43 and finally are degraded into harmless CO 2 And H 2 And O, discharging the treated clean gas from the gas outlet 42 under the action of the induced draft fan 45. After a further period of use, the catalytic oxidation performance of the spent SCR catalyst decreases, after which the catalyst assembly 43 may be recycled or regenerated.
Regeneration of the catalyst assembly 43 is conventional and involves ultrasonic water washing with an organic polymer cleaning agent.
The curing and stabilizing treatment may be carried out by a conventional cement curing method, a lime curing method or a chemical stabilizing method.
1. Method for setting cement
The curing treatment is to mix a curing agent and the waste incineration fly ash to form a cured body, so that the dissolution of heavy metals is reduced. Cement is the most common hazardous waste curing agent, so the incineration fly ash is usually cured by cement in engineering. After the fly ash is mixed into the matrix of the cement, under certain conditions, through a series of physical and chemical actions, the mobility of pollutants in a waste cement matrix system is reduced (such as the formation of metal oxides with much smaller solubility than metal ions). Sometimes, some adjuvants are also added to enhance the reaction process, eventually turning the granular material into a cohesive concrete mass. Thereby stabilizing a large amount of waste by solidification. The research result of stabilizing treatment on the waste incineration fly ash shows that the treated building block cannot achieve high strength no matter the fly ash pretreatment processes such as water washing, crushing and the like are adopted. In addition, when the heavy metal leaching in the fly ash is researched, the influence of chloride ions in the fly ash is found, and the ions such as iron, copper, zinc and the like in the solidified building block are easy to leach, so that the pollutants exceed the standard.
2. Lime curing process
Lime solidification refers to an operation of solidifying or stabilizing hazardous waste using a substance having a funicular reaction (pozzolanic re.action), such as lime, fly ash, cement kiln dust, and slag of a melting furnace, as a solidification base material. The cable is carried out to react under a proper catalytic environment, and heavy metal components in the waste are adsorbed in the generated colloidal crystals. The structural strength of the lime cured is not as strong as the cement and is therefore less used alone. In addition, asphalt solidification, plastic material solidification technology, self-cementing solidification, large encapsulation and the like exist, but the method is rarely applied to the treatment of the household garbage incineration fly ash due to technical and economic limitations.
3. Method for stabilizing drug
The medicament stabilizing technology mainly treats heavy metal waste, and various heavy metal stabilizing technologies such as a pH value control technology, an oxidation and reduction potential control technology, a precipitation technology, an adsorption technology, an ion exchange technology and the like are developed at present. The technology is less applied to the stabilization treatment of the waste incineration fly ash at present, but the development direction is in one direction. Especially, compared with other stabilizing methods, the medicament stabilizing method has the advantages of simple process, good stabilizing effect, low cost and the like.
Experiment one, fly ash (dioxin content about 150 ng/g) from a waste incineration power plant was treated according to the method described in example 1, and the process parameters were as follows: the feeding amount of the fly ash is 10g/min, the adding amount of the ozone is 0.3g/h, the reaction temperature of the fly ash catalytic oxidation device 3 is controlled at 90 ℃, and the retention time of the fly ash in the fly ash catalytic oxidation device 3 is about 2min. The heating temperature of the waste SCR catalytic oxidation device 4 is 90 ℃, and the air speed of the gas is 8000 h -1 . The various performance data of the treated fly ash and gas are as follows: the content of dioxin in the fly ash discharged from a fly ash outlet 34 of the fly ash catalytic oxidation device 3 is 20ng/g, and the removal rate of the dioxin reaches 87%; and dioxin and other gaseous organic pollutants are not detected in the gas discharged from the gas outlet 42 of the waste SCR catalytic oxidation device 4.
Comparative example 1, will experiment one ozone generating device 2 removal, i.e. the reaction process does not pass ozone, only let in air. The reaction process is carried out by means of a thermocatalytic reaction; the rest are equivalent to experiment one.
The device is detected as an experiment, and the processed performance data are as follows: the content of dioxin in the fly ash discharged from a fly ash outlet 34 of the fly ash catalytic oxidation device 3 is 92ng/g, and the removal rate of the dioxin is only 39 percent; but dioxin was not detected in the gas discharged from the gas outlet 42 of the waste SCR catalytic oxidation apparatus 4.
Comparative example 2, the waste SCR catalytic oxidation device 4 in the first experiment was removed, and incineration fly ash was treated only by the fly ash catalytic oxidation device 3; the rest is identical to experiment one.
The device is detected as an experiment I, and the processed performance data are as follows: the content of dioxin in the fly ash discharged from a fly ash outlet 34 of the fly ash catalytic oxidation device 3 is 20ng/g, and the removal rate of the dioxin is 87%; although no dioxin was detected in the gas discharged from the gas outlet 33, other gaseous organic pollutants were detected at a concentration of about 30ng/g.
Comparative example 3, changing the ozone adding amount in the first experiment to 0.1 and 0.5 g/h respectively; the rest is the same as the first experiment.
The device is detected as an experiment I, and the processed performance data are as follows: the fly ash discharged from the fly ash outlet 34 of the fly ash catalytic oxidation device 3 has dioxin contents of 65ng/g and 8ng/g and dioxin removal rates of 57% and 95%, and dioxin and other gaseous organic pollutants are not detected in the gas discharged from the gas outlet 42 of the waste SCR catalytic oxidation device 4. This shows that the addition of ozone has an important influence on the removal of dioxin, and the removal effect of dioxin increases with the increase of the amount of ozone added. However, since ozone itself is a pollutant and excessive ozone easily causes secondary pollution, the amount of ozone added should be controlled to 0.1 to 0.5ng/g (fly ash).
Comparative example 4, the heating temperatures of the fly ash catalytic oxidation apparatus 3 in the first experiment were changed to 50 ℃ and 150 ℃, respectively. The rest is the same as the first experiment.
The device is detected as an experiment I, and the processed performance data are as follows: the fly ash discharged from the fly ash outlet 34 of the fly ash catalytic oxidation device 3 has dioxin contents of 38ng/g and 56ng/g and the dioxin removal rate of 75% and 63%, and dioxin and other gaseous organic pollutants are not detected in the gas discharged from the gas outlet 42 of the waste SCR catalytic oxidation device 4. This shows that the reaction temperature of the fly ash catalytic oxidation apparatus 3 has an influence on the removal of dioxin, and the heating temperature of about 90 ℃ in the first experiment is optimum, and the temperature decreases, the catalytic activity decreases, the temperature increases, and the activity of ozone decreases.
Comparative example 5, the heating temperatures of the waste SCR catalytic oxidation apparatus 4 in the first experiment were changed to 50 ℃ and 150 ℃, respectively, and the rest of the first experiment was performed.
The device is detected as an experiment I, and the processed performance data are as follows: the content of dioxin in the fly ash discharged from a fly ash outlet 34 of the fly ash catalytic oxidation device 3 is 20ng/g, and the removal rate of the dioxin is 87%; dioxin is not detected in the gas discharged from the gas outlet 42 of the waste SCR catalytic oxidation device 4 at the temperature of 50 ℃, but other gaseous organic pollutants are detected, and the concentration is about 20 ng/g; dioxin and other gaseous organic pollutants were not detected in the gas discharged from the gas outlet 42 of the waste SCR catalytic oxidation unit 4 at 150 ℃.
Finally, it should be noted that: the above embodiments are only used for illustrating the technical solution of the present invention, and not for limiting the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions.
Claims (5)
1. A domestic waste burns flying ash and abandonment SCR catalyst coprocessing method, utilize domestic waste to burn flying ash and abandonment SCR catalyst coprocessing system and carry on work, characterized by that:
the household garbage incineration fly ash and waste SCR catalyst cooperative treatment system comprises a fly ash feeding device (1), an ozone generating device (2), a fly ash catalytic oxidation device (3), a waste SCR catalytic oxidation device (4) and a fly ash collecting device (5); the fly ash catalytic oxidation device (3) is provided with a gas inlet (32), a fly ash inlet (31), a gas outlet (33) and a fly ash outlet (34); the waste SCR catalytic oxidation device (4) is provided with an air inlet (41) and an air outlet (42); the gas inlet (32) is communicated with the ozone generating device (2), the gas outlet (33) is communicated with the gas inlet (41) of the waste SCR catalytic oxidation device (4), and the fly ash outlet (34) is communicated with the fly ash collecting device (5);
the inner cavity of the fly ash catalytic oxidation device (3) is respectively provided with a helical blade (35) and a fly ash heating device (36);
the fly ash feeding device (1) comprises an ash bucket (11) and a fly ash quantitative feeder (12) communicated with a discharge hole of the ash bucket (11); the fly ash quantitative feeder (12) is communicated with a fly ash inlet (31);
at least one catalyst component (43) is arranged in the waste SCR catalytic oxidation device (4), and the catalyst component (43) is connected with the inner wall of the waste SCR catalytic oxidation device (4); an exhaust gas heating device (44) is arranged in the inner cavity of the waste SCR catalytic oxidation device (4);
an induced draft fan (45) is arranged on an air outlet (42) of the waste SCR catalytic oxidation device (4);
the catalyst assembly (43) consists of a catalyst layer consisting of waste SCR catalysts and porous stainless steel plates arranged on two sides of the catalyst layer, the thickness of the catalyst layer is 5-10mm, and the pore diameter of each porous stainless steel plate is 0.3-0.4mm; the waste SCR catalyst is particles with the particle size of 0.5-1mm;
the cooperative processing method comprises the following steps:
the fly ash is added into a fly ash quantitative feeder (12) through an ash hopper (11), and the fly ash quantitative feeder (12) adds the fly ash into a fly ash catalytic oxidation device (3) through a fly ash inlet (31); meanwhile, the ozone generating device (2) generates ozone, and the ozone enters the fly ash catalytic oxidation device (3) from the gas inlet (32);
the fly ash and the ozone are stirred and mixed by the helical blade (35) in the fly ash catalytic oxidation device (3) and move to the gas outlet (33) and the fly ash outlet (34) slowly, and dioxin organic matters contained in the fly ash are degraded into CO by catalytic oxidation of the ozone in the process 2 、H 2 O and HCl, or decomposition to the gaseous stateLow molecular weight and low toxicity organic matter;
the fly ash treated by the fly ash catalytic oxidation device (3) enters the fly ash collecting device (5) through a fly ash outlet (34), the waste gas treated by the fly ash catalytic oxidation device (3) enters the waste SCR catalytic oxidation device (4) through a gas outlet (33) and an air inlet (41), and gaseous organic matters in the waste gas are degraded into harmless CO through the catalytic oxidation of a catalyst layer in the waste SCR catalytic oxidation device (4) 2 And H 2 O, discharging the treated clean gas from the gas outlet (42) under the action of a draught fan (45);
the fly ash heating device (36) is used for heating fly ash and ozone in the fly ash catalytic oxidation device (3), and the heating temperature is 90 ℃;
the waste gas heating device (44) is used for heating waste gas in the waste SCR catalytic oxidation device (4), the heating temperature is 90 to 150 ℃, and the air speed of gas in the waste SCR catalytic oxidation device (4) is 5000 to 10000/h.
2. The method for the synergistic treatment of fly ash from incineration of household garbage and waste SCR catalyst as claimed in claim 1, wherein: the fly ash treated by the fly ash catalytic oxidation device (3) in the fly ash collecting device (5) is then solidified and stabilized, so that heavy metal substances contained in the treated fly ash are removed.
3. The method for the co-treatment of fly ash from incineration of household garbage and waste SCR catalyst as claimed in claim 2, wherein: the residence time of the fly ash in the fly ash catalytic oxidation device (3) is more than 1min, and the adding amount ratio of the ozone to the fly ash in the fly ash catalytic oxidation device (3) is 0.1 to 0.5g of ozone/kg of fly ash.
4. The method for the co-treatment of fly ash from incineration of household garbage and waste SCR catalyst as claimed in claim 3, wherein: the curing and stabilizing treatment is a cement curing method, lime curing or a medicament stabilizing method.
5. The method for the synergistic treatment of the fly ash from the incineration of domestic garbage and the waste SCR catalyst as claimed in any one of claims 1 to 4, wherein: the waste SCR catalytic oxidation device (4) is provided with an opening which can be opened and closed and is matched with the catalyst component (43), and the catalyst component (43) is inserted into or pulled out of the opening.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710517227.7A CN107159684B (en) | 2017-06-29 | 2017-06-29 | Domestic waste incineration fly ash and waste SCR catalyst co-treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710517227.7A CN107159684B (en) | 2017-06-29 | 2017-06-29 | Domestic waste incineration fly ash and waste SCR catalyst co-treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107159684A CN107159684A (en) | 2017-09-15 |
| CN107159684B true CN107159684B (en) | 2023-04-07 |
Family
ID=59827156
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710517227.7A Expired - Fee Related CN107159684B (en) | 2017-06-29 | 2017-06-29 | Domestic waste incineration fly ash and waste SCR catalyst co-treatment method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107159684B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108817026A (en) * | 2018-05-25 | 2018-11-16 | 镇江新区固废处置股份有限公司 | A kind of trash receptacle, solidification and landfill system |
| CN110548748A (en) * | 2019-07-23 | 2019-12-10 | 周昊 | Collaborative melting treatment method for waste SCR flue gas denitration catalyst and fly ash |
| CN113669731B (en) * | 2021-08-20 | 2022-09-20 | 北科蕴宏环保科技(北京)有限公司 | High-efficiency fly ash heat treatment method and device |
| CN113929199B (en) * | 2021-10-26 | 2022-11-08 | 伊犁新天煤化工有限责任公司 | Method for reducing chemical oxygen demand of coal gasification wastewater by utilizing coal gasification ash |
| CN116174453B (en) * | 2023-01-16 | 2024-02-06 | 浙江大学 | Fly ash low-temperature pyrolysis detoxification device for dividing wall heat exchange |
| CN118204356B (en) * | 2024-05-20 | 2024-09-03 | 浙江大维高新技术股份有限公司 | Device and method for circularly treating waste incineration fly ash |
| CN118204357B (en) * | 2024-05-20 | 2024-09-06 | 浙江大维高新技术股份有限公司 | Device and method for treating dioxin in waste incineration fly ash |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003010813A (en) * | 2001-06-29 | 2003-01-14 | Furukawa Co Ltd | System for decomposing organic chlorine compound contained in fly ash |
| CN101716463B (en) * | 2010-01-05 | 2012-07-04 | 浙江大学 | Simultaneous removing device and method of various pollutants by electrocatalytical oxidation combining lime-gypsum method |
| CN201684521U (en) * | 2010-06-04 | 2010-12-29 | 重庆大学 | Flue gas demercuration reactor |
| CN102671524B (en) * | 2012-05-10 | 2014-04-16 | 浙江大学 | Device and method for removing dioxin in incineration flue gas fly ash by using ultrasonic coupling multi-energy field |
| CN203355611U (en) * | 2013-05-16 | 2013-12-25 | 上海宝钢节能技术有限公司 | Device for removing NOX and dioxins in sintering and pelletizing flue gas through SCR (Selective Catalytic Reduction) |
| CN104138771A (en) * | 2014-07-30 | 2014-11-12 | 索平 | Method for regeneration of SCR denitration catalyzer |
| CN105344214A (en) * | 2014-08-21 | 2016-02-24 | 山西易通环保技术有限公司 | Liquid-state catalyst flue gas purification integration system and liquid-state catalyst flue gas purification integration process |
| CN206997331U (en) * | 2017-06-29 | 2018-02-13 | 浙江富春江环保热电股份有限公司 | Domestic garbage incineration flyash and discarded SCR catalyst coprocessing system |
-
2017
- 2017-06-29 CN CN201710517227.7A patent/CN107159684B/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN107159684A (en) | 2017-09-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107159684B (en) | Domestic waste incineration fly ash and waste SCR catalyst co-treatment method | |
| Zhang et al. | Degradation technologies and mechanisms of dioxins in municipal solid waste incineration fly ash: A review | |
| Kulkarni et al. | Dioxins sources and current remediation technologies—a review | |
| JP3772961B2 (en) | Method for treating exhaust gas containing dioxin and composite catalyst for dioxin suppression | |
| CN106424077B (en) | Method for treating fly ash by using sludge | |
| CN110357578A (en) | Utilize the method for haydite kiln disposal of solid waste and the haydite kiln of disposal of solid waste | |
| CN111068612B (en) | Method for preparing zeolite-like porous material by using solid waste, zeolite-like porous material and application thereof | |
| CN108787713B (en) | Method for treating medical waste based on flotation combined microwave method | |
| Li et al. | Review of thermal treatments for the degradation of dioxins in municipal solid waste incineration fly ash: Proposing a suitable method for large-scale processing | |
| CN104028087A (en) | Method and device for removing dioxin in high-temperature smoke | |
| CN110564433A (en) | Super-enriched plant-based biochar and preparation method and application thereof | |
| CN101507896B (en) | POPs removal method from flue gas based on pulse filter and active carbon reclamation | |
| CN104150733A (en) | Method for removing organic pollutants and stabilizing heavy metals based on sludge hydro-thermal treatment | |
| CN111847480A (en) | Purification treatment and resource recycling method for industrial sodium chloride waste salt | |
| CN105233641B (en) | The method and device of bioxin caused by incineration of waste and mercury deep purifying | |
| CN205717254U (en) | The high-efficiency environment friendly exhaust gas processing device that a kind of chemical plant is special | |
| CN211011385U (en) | Plasma gasification furnace and waste incineration power plant's innocent treatment system | |
| CN206997331U (en) | Domestic garbage incineration flyash and discarded SCR catalyst coprocessing system | |
| JP2002301447A (en) | Method for use of incineration ash | |
| KR101179523B1 (en) | Manufacture device of activation matter using sewage sludges | |
| CN110715297A (en) | Harmless treatment system and method for plasma gasification furnace and waste incineration power plant | |
| JP2007000853A (en) | Method for cleaning and treating pcb-contaminated soil | |
| CN113587104B (en) | Waste pyrolysis waste gas purification system and process | |
| CN102059043A (en) | Control method of harmful waste gas generated in recycling of waste electric and electronic products | |
| CN102380228B (en) | Extracting agent for treating dioxin in flying ash and method for extracting dioxin by extracting agent |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20230407 |