CN114888056A - Method for synchronously solidifying carbon dioxide and deeply dechlorinating waste incineration fly ash - Google Patents
Method for synchronously solidifying carbon dioxide and deeply dechlorinating waste incineration fly ash Download PDFInfo
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- CN114888056A CN114888056A CN202210379689.8A CN202210379689A CN114888056A CN 114888056 A CN114888056 A CN 114888056A CN 202210379689 A CN202210379689 A CN 202210379689A CN 114888056 A CN114888056 A CN 114888056A
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- fly ash
- carbon dioxide
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 132
- 239000010881 fly ash Substances 0.000 title claims abstract description 88
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 66
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 66
- 238000004056 waste incineration Methods 0.000 title claims abstract description 61
- 238000000034 method Methods 0.000 title claims abstract description 33
- 230000000382 dechlorinating effect Effects 0.000 title claims abstract description 23
- 238000005406 washing Methods 0.000 claims abstract description 112
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000002002 slurry Substances 0.000 claims abstract description 14
- 239000007788 liquid Substances 0.000 claims description 36
- 238000003756 stirring Methods 0.000 claims description 27
- 238000000926 separation method Methods 0.000 claims description 14
- 239000007787 solid Substances 0.000 claims description 13
- 239000004575 stone Substances 0.000 claims description 8
- 238000005119 centrifugation Methods 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 11
- 239000002893 slag Substances 0.000 description 24
- 239000007789 gas Substances 0.000 description 16
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 10
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 10
- 239000000460 chlorine Substances 0.000 description 10
- 229910052801 chlorine Inorganic materials 0.000 description 10
- 239000003546 flue gas Substances 0.000 description 10
- 238000006298 dechlorination reaction Methods 0.000 description 9
- 239000000706 filtrate Substances 0.000 description 8
- 239000000292 calcium oxide Substances 0.000 description 6
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 6
- 150000001804 chlorine Chemical class 0.000 description 6
- 238000004090 dissolution Methods 0.000 description 6
- 239000008399 tap water Substances 0.000 description 5
- 235000020679 tap water Nutrition 0.000 description 5
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 3
- 230000002378 acidificating effect Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 230000001376 precipitating effect Effects 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 230000033558 biomineral tissue development Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 150000003841 chloride salts Chemical class 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 239000012629 purifying agent Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Classifications
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- 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
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a method for synchronously solidifying carbon dioxide and deeply dechlorinating waste incineration fly ash, which is characterized in that three-stage countercurrent washing is carried out on the waste incineration fly ash, in the processes of primary countercurrent washing and secondary countercurrent washing, carbon dioxide-containing gas is introduced into slurry formed by the waste incineration fly ash and water for reaction.
Description
Technical Field
The invention relates to a water washing treatment method for waste incineration fly ash, in particular to a method for synchronously solidifying carbon dioxide and deeply dechlorinating the waste incineration fly ash, belonging to the field of recycling treatment of fly ash solid wastes.
Background
Domestic waste treatment in China enters a stage mainly based on incineration and is in an industry mature period. In the process of waste incineration, organic matters are converted into gas to be discharged into the atmosphere, while inorganic matters form solid particles, and the finer particles are conveyed into the next system along flue gas from the incinerator, and finally the particles and added purifying agent and reaction products form waste incineration fly ash.
The quantity of fly ash generated by burning garbage every year in China is large, the CaO content in the fly ash is high, and the fly ash is easy to react with CO 2 Formation of CaCO 3 And (4) precipitating. The fly ash used for carbonization has great potential for sealing carbon dioxide, and the carbonized fly ash can be reused as building aggregate after being carbonized.
Based on the characteristics of waste incineration fly ash, no process can simultaneously carry out carbon sequestration and deep dechlorination at present. The treatment method of the waste incineration fly ash comprises the technologies of washing, sintering, stabilizing and the like. The water washing is an economic and feasible mode, the operation is simple, the cost is low, and most of soluble chloride in the waste incineration fly ash can be dissolved. In the application of the existing waste incineration fly ash washing technology, the technology improvement focusing on common washing is mostly adopted, various leaching agents are added on the basis of washing, the cost is high, the water consumption is huge, and most of the leaching agents are difficult to be applied to specific engineering. The prior various processes have low dechlorination degree on the waste incineration fly ash, can not carry out deep dechlorination and also limit the resource utilization of the waste incineration fly ash.
Disclosure of Invention
Aiming at the technical problem that the resource utilization of the waste incineration fly ash is limited due to the fact that the conventional washing of the waste incineration fly ash is difficult to realize deep dechlorination in the prior art, the invention aims to provide a method for synchronously solidifying carbon dioxide and deeply dechlorinating the waste incineration fly ash, the method introduces gas containing carbon dioxide in the process of washing and dechlorinating the waste incineration fly ash, utilizes the characteristics of high specific surface area, high porosity and active calcium oxide of the waste incineration fly ash to realize the fixation of the carbon dioxide, meanwhile, the carbon dioxide is utilized to promote the dissolution of chloride in the process of washing and dechlorinating, the dechlorinating efficiency of the waste incineration fly ash is greatly improved, compared with the traditional washing mode of the waste incineration fly ash, the dechlorination rate can be improved under the condition of lower solid and liquid, and can effectively and synchronously fix carbon dioxide, and the carbon dioxide can be derived from industrial flue gas, thereby conforming to the development concept of carbon neutralization.
In order to realize the technical purpose, the invention provides a method for synchronously solidifying carbon dioxide and deeply dechlorinating waste incineration fly ash.
The technical scheme of the invention skillfully introduces carbon dioxide gas into the waste incineration fly ash, fully utilizes the mutual benefit relation of the waste incineration fly ash and the waste incineration fly ash in the water washing process, fixes the carbon dioxide through the waste incineration fly ash, and promotes the dissolution of chloride in the waste incineration fly ash by utilizing the carbon dioxide. The waste incineration fly ash has large specific surface area and high porosity and can be mixed withCO 2 Active ingredients of the reaction, such as alkali metals (Ca, Mg, Na, K) and oxides thereof (CaO, MgO) and the like, which react with CO in the flue gas 2 When contacted, it will be converted into carbonate, thereby leading to CO 2 Mineralization of, effecting CO 2 The carbon dioxide can promote deep dechlorination of the waste incineration fly ash, the difficultly soluble chloride in the waste incineration fly ash is mainly Friedel Salt, and the following reactions can occur after the carbon dioxide is introduced: 3 CaO. Al 2 O 3 ·CaCl 2 ·10H 2 O+3CO 2 →3CaCO 3 +Al 2 O 3 ·xH 2 O+CaCl 2 +(10-x)H 2 And O, the part of the insoluble chlorine salt can be promoted to be converted into soluble salt by introducing carbon dioxide, and the pH of the whole system is controlled to be weakly acidic from original strong basicity along with the introduction of the carbon dioxide, so that the conversion and the dissolution of the part of the insoluble chlorine salt are promoted, and the removal rate of the fly ash chlorine salt is improved.
As a preferable scheme, the waste incineration fly ash and water in each stage of the three-stage countercurrent water washing form slurry according to the liquid-solid ratio of 3mL:1 g-4 mL:1 g. Compared with the method without introducing carbon dioxide, the method greatly reduces the liquid-solid ratio of water washing, saves water and reduces the generation of waste water. The washing water used is not particularly limited, and may be tap water or purified water of industrial wastewater or the like.
In a preferable scheme, in the first stage of countercurrent washing, carbon dioxide-containing gas is introduced into the slurry at a flow rate of 100-200L/min per kilogram of waste incineration fly ash.
Preferably, in the first stage of counter-current water washing, the pH of the slurry is controlled within a range of 6.0-6.5.
In a preferable scheme, in the second stage of counter-current water washing process, carbon dioxide-containing gas is introduced into the slurry according to the flow rate of 60-100L/min per kilogram of waste incineration fly ash.
Preferably, in the second stage of counter-current water washing process, the pH of the slurry is controlled within the range of 5.5-6.0.
In the first-stage countercurrent washing and the second-stage countercurrent washing, the carbon dioxide gas is introduced to promote the dissolution of part of the insoluble chlorine salt, and meanwhile, the weakly acidic carbon dioxide continuously consumes other alkaline substances, so that the pH value of the solution is reduced, the conversion and the dissolution of part of the insoluble chlorine salt are promoted, and the removal rate of the fly ash chlorine salt is further improved. Introducing CO in the first stage of countercurrent washing process 2 The flow is larger than that of the second-stage countercurrent washing process, and is mainly based on that the chlorine content of the waste incineration fly ash is relatively higher in the first-stage countercurrent washing process, and carbon dioxide with a large flow rate is needed to realize the reaction, the chlorine content of the waste incineration fly ash is relatively reduced in the second-stage countercurrent washing process, the flow of the needed carbon dioxide is relatively small, but the introduction flow of the carbon dioxide is kept within a certain range, and the deep removal of chlorine can be ensured.
As a preferable mode, the content of carbon dioxide in the carbon dioxide-containing gas is 5% to 30% by volume. The gas containing carbon dioxide has wide sources and can be industrial flue gas. Such as flue gas in steel industry, flue gas from waste incineration, flue gas from power plants, etc.
As a preferred option, a bubbled stone is used to achieve uniform bubbling during the passage of the carbon dioxide containing gas into the slurry. The carbon dioxide can be stably dispersed into water by adopting the air stones, and the contact reaction efficiency of the carbon dioxide and the waste incineration fly ash is increased.
As a preferable scheme, the conditions of each stage of countercurrent water washing in the three-stage countercurrent water washing process are as follows: the temperature is 40-60 ℃, the time is 40-60 min, and the stirring speed is 500-800 r/min. Under the preferable temperature condition, the waste incineration fly ash can achieve the maximum dechlorination efficiency, if the temperature is too low, the deep dechlorination effect can not be achieved, and if the water washing pretreatment is carried out by using too high temperature, the energy loss is increased, the treatment cost is increased, and the CO is treated at high temperature 2 The solubility of (b) is also lowered, which is disadvantageous for carbon fixation, and if the temperature is too low, the reaction efficiency is lowered. And the proper stirring action is beneficial to improving the gas-liquid-solid three-phase contact reaction efficiency.
As a preferred scheme, the third stage countercurrent water washing adopts a conventional water washing process.
As a preferable scheme, after each stage of the three stages of countercurrent washing is completed, solid-liquid separation is realized by centrifugation, and the water content of solid is lower than 35%. The residual chlorine level can be reduced by dewatering the solids to a lower moisture level.
Compared with the prior art, the technical scheme of the invention has the beneficial technical effects that:
(1) the method for synchronously solidifying carbon dioxide and deeply dechlorinating the fly ash saves water consumption, has the solid-liquid ratio of only 3: 1-4: 1, and recycles water through a three-stage countercurrent process.
(2) The method for synchronously solidifying carbon dioxide and deeply dechlorinating the fly ash provided by the invention not only can realize the fixation of the carbon dioxide by utilizing the waste incineration fly ash, but also can promote the deep dechlorination of the waste incineration fly ash by utilizing the carbon dioxide. The waste incineration fly ash has large specific surface area and high porosity, is rich in active substances such as CaO which can react with carbon dioxide and CO 2 Formation of CaCO 3 And (4) precipitating, namely, utilizing the waste incineration fly ash to seal and store carbon dioxide, and reusing the carbonized fly ash as building aggregate to realize resource utilization. Meanwhile, the insoluble chloride Salt in the waste incineration fly ash is mainly Friedel Salt, and when the water-washed fly ash before and after carbonation is detected by XRD, the peak of the insoluble chloride Friedel Salt in the fly ash after the flue gas is introduced disappears, mainly because the following reaction occurs after the carbon dioxide is introduced: 3 CaO. Al 2 O 3 ·CaCl 2· 10H 2 O+3CO 2 →3CaCO 3 +Al 2 O 3 ·xH 2 O+CaCl 2 +(10-x)H 2 And O. The pH value of the whole system is controlled to be weakly acidic from original strong basicity, the conversion and the dissolution of partial insoluble chloride are directly promoted, and the removal rate of the fly ash chloride is further improved.
(3) The method for synchronously solidifying carbon dioxide and deeply dechlorinating fly ash provided by the invention can also fix heavy metals in the fly ash, the heavy metals in the solution exist in an unstable hydroxide form under an alkaline condition, and CO is introduced 2 Then, the resulting product reacts with the carbonate to form a carbonate which is hardly soluble.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings used in the description of the embodiments will be briefly introduced below. It is obvious that the drawings in the following description are only some embodiments of the invention, and that for a person skilled in the art, other drawings can be derived from them without inventive effort.
FIG. 1 is a flow chart of a method for synchronously solidifying carbon dioxide and deeply dechlorinating waste incineration fly ash.
FIG. 2 is an XRD comparison graph of the waste incineration fly ash after carbonating water washing and normal water washing.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
The original chloride ion content of the incineration fly ash used is 20.75%, and the introduced carbon dioxide comes from flue gas and has the volume content of 13%. Adding fly ash into a water washing reactor, controlling the liquid-solid ratio to be 3:1, introducing gas containing carbon dioxide at the flow rate of 100L/min per kilogram of fly ash, and dispersing the fly ash by using air stones. Stirring for 1h at 500r/min by using an electric stirrer, controlling the stirring temperature to be 40 ℃ and the pH value to be 6.5, and carrying out a first-stage water washing process. And carrying out solid-liquid separation to obtain a washing liquid and washing slag. And (4) introducing the washing slag into a second-stage washing process, introducing gas containing carbon dioxide at the flow rate of 60L/min per kilogram of fly ash, and dispersing the gas by using air stones. Stirring with an electric stirrer at 500r/min for 1 hr, with the stirring temperature controlled at 40 deg.C and pH 6.0. And carrying out solid-liquid separation to obtain a washing liquid and washing slag. And carrying out a third-stage washing process on the washing slag, stirring for 1h at the speed of 500r/min by using an electric stirrer, and controlling the stirring temperature to be 40 ℃. Wherein the first-stage water washing liquid is derived from the second-stage water washing filtrate, the second-stage water washing liquid is derived from the third-stage water washing filtrate, the third-stage water washing liquid is additionally added tap water, and the solid-liquid separation of each stage is to ensure that the water in the washing slag is removed to be below 35%. The chlorine content of the final washing slag is detected to be 0.86 percent, and the requirements of the 6.3-c bar of HJ-1134-Buchner 2020 are met: the soluble chlorine content of the treated product should not exceed 2%, preferably not higher than 1%.
Example 2
The original chloride ion content of the incineration fly ash used is 19.25%, and the introduced carbon dioxide comes from flue gas and has the volume content of 30%. The fly ash is placed in a reactor. The liquid-solid ratio was controlled to 4:1, the flow rate of carbon dioxide-containing gas was 200L/min per kg of fly ash, and the fly ash was dispersed using air stones. Stirring for 1h at 800r/min by using an electric stirrer, controlling the stirring temperature to be 60 ℃ and the pH value to be 6.0, and carrying out a first-stage water washing process. And carrying out solid-liquid separation to obtain a washing liquid and washing slag. And (4) introducing the washing slag into a second-stage washing process, introducing gas containing carbon dioxide at the flow rate of 100L/min per kilogram of fly ash, and dispersing the gas by using air stones. Stirring for 1h at 800r/min by using an electric stirrer, controlling the stirring temperature at 60 ℃ and the pH value at 5.5. And carrying out solid-liquid separation to obtain a washing liquid and washing slag. And carrying out a third-stage washing process on the washing slag, stirring for 1h at the speed of 800r/min by using an electric stirrer, and controlling the stirring temperature to be 60 ℃. Wherein the first-stage water washing liquid is derived from the second-stage water washing filtrate, the second-stage water washing liquid is derived from the third-stage water washing filtrate, the third-stage water washing liquid is additionally added tap water, and the solid-liquid separation of each stage is to ensure that the water in the washing slag is removed to be below 35%. The chlorine content of the final washing slag is detected to be 0.70 percent, and the requirements of the 6.3-c bar of HJ-1134-Buchner 2020 are met: the soluble chlorine content of the treated product should not exceed 2%, preferably not higher than 1%.
Comparative example 1
The incineration fly ash used had an original chloride ion content of 20.75%, and was placed in a reactor. Controlling the liquid-solid ratio to be 3:1, stirring for 1h at the speed of 500r/min by using an electric stirrer, controlling the stirring temperature to be 40 ℃, and carrying out a first-stage water washing process. And carrying out solid-liquid separation to obtain a washing liquid and washing slag. And (4) allowing the washing slag to enter a second-stage washing process, stirring for 1h at the speed of 500r/min by using an electric stirrer, and controlling the stirring temperature to be 40 ℃. And carrying out solid-liquid separation to obtain a washing liquid and washing slag. And carrying out a third-stage washing process on the washing slag, stirring for 1h at the speed of 500r/min by using an electric stirrer, and controlling the stirring temperature to be 40 ℃. Wherein the first-stage water washing liquid is derived from the second-stage water washing filtrate, the second-stage water washing liquid is derived from the third-stage water washing filtrate, the third-stage water washing liquid is additionally added tap water, and the solid-liquid separation of each stage is to ensure that the water in the washing slag is removed to be below 35%. The chlorine content of the final washing slag was determined to be 2.85%.
Comparative example 2
The incineration fly ash used had an original chloride ion content of 19.25%, and was placed in a reactor. Controlling the liquid-solid ratio to be 4:1, stirring for 1h at the speed of 800r/min by using an electric stirrer, controlling the stirring temperature to be 60 ℃, carrying out a first-stage water washing process, introducing gas containing carbon dioxide at the flow rate of 200L/min per kilogram of fly ash, and dispersing by using air stones. And carrying out solid-liquid separation to obtain a washing liquid and washing slag. And (4) allowing the washing slag to enter a second-stage washing process, stirring for 1h at the speed of 800r/min by using an electric stirrer, and controlling the stirring temperature to be 60 ℃. And carrying out solid-liquid separation to obtain a washing liquid and washing slag. And carrying out a third-stage washing process on the washing slag, stirring for 1h at the speed of 800r/min by using an electric stirrer, and controlling the stirring temperature to be 60 ℃. Wherein the first-stage water washing liquid is derived from the second-stage water washing filtrate, the second-stage water washing liquid is derived from the third-stage water washing filtrate, the third-stage water washing liquid is additionally added tap water, and the solid-liquid separation of each stage is to ensure that the water in the washing slag is removed to be below 35%. The chlorine content of the final washing slag was measured to be 1.64%.
Claims (10)
1. A method for synchronously solidifying carbon dioxide and deeply dechlorinating waste incineration fly ash is used for carrying out three-level countercurrent washing on the waste incineration fly ash and is characterized by comprising the following steps of: in the first stage countercurrent water washing and the second stage countercurrent water washing, gas containing carbon dioxide is introduced into slurry formed by the waste incineration fly ash and water to react.
2. The method for synchronously solidifying carbon dioxide and deeply dechlorinating the waste incineration fly ash according to the claim 1, characterized by comprising the following steps: in the three-stage countercurrent washing process, the waste incineration fly ash and water form slurry according to the liquid-solid ratio of 3mL to 1 g-4 mL to 1 g.
3. The method for synchronously solidifying carbon dioxide and deeply dechlorinating the waste incineration fly ash according to the claim 1, characterized by comprising the following steps: and in the first stage of counter-current water washing process, introducing gas containing carbon dioxide into the slurry at a flow rate of 100-200L/min per kilogram of waste incineration fly ash.
4. The method for synchronously solidifying carbon dioxide and deeply dechlorinating the waste incineration fly ash according to the claim 1 or the 3, characterized by comprising the following steps: and in the first stage of counter-current washing process, the pH of the slurry is controlled within the range of 6.0-6.5.
5. The method for synchronously solidifying carbon dioxide and deeply dechlorinating the waste incineration fly ash according to the claim 1, characterized by comprising the following steps: and in the second stage of counter-current water washing, introducing gas containing carbon dioxide into the slurry at a flow rate of 60-100L/min per kilogram of waste incineration fly ash.
6. The method for synchronously solidifying carbon dioxide and deeply dechlorinating the waste incineration fly ash according to the claim 1 or the 5, characterized by comprising the following steps: and in the second stage of counter-current washing process, the pH of the slurry is controlled within the range of 5.5-6.0.
7. The method for synchronously solidifying carbon dioxide and deeply dechlorinating the waste incineration fly ash according to the claim 1, 3 or 5, characterized by comprising the following steps: the volume percentage content of carbon dioxide in the carbon dioxide-containing gas is 5-30%.
8. The method for synchronously solidifying carbon dioxide and deeply dechlorinating the waste incineration fly ash according to the claim 1, 3 or 5, characterized by comprising the following steps: and the gas containing the carbon dioxide is uniformly bubbled by using a bubbled stone in the process of introducing the gas into the slurry.
9. The method for synchronously solidifying carbon dioxide and deeply dechlorinating the waste incineration fly ash according to the claim 1, is characterized in that: the conditions of all levels of countercurrent washing in the three levels of countercurrent washing processes are as follows: the temperature is 40-60 ℃, the time is 40-60 min, and the stirring speed is 500-800 r/min.
10. The method for synchronously solidifying carbon dioxide and deeply dechlorinating the waste incineration fly ash according to the claim 1, characterized by comprising the following steps: and after all levels of countercurrent washing of the three levels of countercurrent washing are finished, solid-liquid separation is realized by centrifugation, and the solid water content is lower than 35%.
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| CN115532797A (en) * | 2022-09-30 | 2022-12-30 | 上海环境卫生工程设计院有限公司 | Slag water washing dechlorination method |
| CN115532785A (en) * | 2022-09-13 | 2022-12-30 | 浙江大学 | Disposal system and method for thermal decomposition and collaborative mineralization of fly ash dioxin |
| CN115569968A (en) * | 2022-09-23 | 2023-01-06 | 重庆三峰环境集团股份有限公司 | Method for treating waste incineration fly ash by cooperating with waste incineration flue gas |
| CN115889405A (en) * | 2022-09-23 | 2023-04-04 | 重庆三峰环境集团股份有限公司 | Fly ash resource utilization system and method for co-processing waste incineration flue gas |
| CN118527462A (en) * | 2024-06-06 | 2024-08-23 | 重庆大学 | Efficient detoxification, upgrading and recycling method and system for waste incineration fly ash |
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