CN219004061U - System for waste incineration fly ash heavy metal solidification is flue gas purification in coordination - Google Patents
System for waste incineration fly ash heavy metal solidification is flue gas purification in coordination Download PDFInfo
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- CN219004061U CN219004061U CN202222533057.0U CN202222533057U CN219004061U CN 219004061 U CN219004061 U CN 219004061U CN 202222533057 U CN202222533057 U CN 202222533057U CN 219004061 U CN219004061 U CN 219004061U
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Abstract
The utility model relates to a system for solidifying and cooperating with purifying flue gas by using heavy metal in waste incineration fly ash, which comprises a low-temperature thermal degradation unit, wherein an ash outlet of the low-temperature thermal degradation unit is communicated with an ash inlet of a primary water washing tank, an ash outlet of the primary water washing tank is communicated with a liquid inlet of a primary centrifugal dehydrator, the primary centrifugal dehydrator is provided with a water outlet and a slag outlet, the slag outlet of the primary centrifugal dehydrator is communicated with a slag inlet of a secondary water washing tank, the liquid outlet of the secondary centrifugal dehydrator is communicated with a water inlet of the primary water washing tank, the slag outlet of the secondary centrifugal dehydrator is communicated with a slag inlet of a tertiary water washing tank, the liquid outlet of the tertiary water washing tank is communicated with a liquid inlet of the tertiary centrifugal dehydrator, the tertiary centrifugal dehydrator is provided with a slag outlet and a water outlet, the water outlet of the tertiary centrifugal dehydrator is communicated with a water inlet of the secondary water washing tank, and the primary water washing tank, the secondary water washing tank and the tertiary water washing tank are provided with a flue gas inlet.
Description
Technical Field
The utility model belongs to the field of treatment of household garbage incineration fly ash, and relates to a system for solidifying heavy metal of garbage incineration fly ash and purifying smoke cooperatively.
Background
The incineration fly ash is powder material with lighter volume weight and small particle size, which is collected at the positions of a flue gas pipeline, a flue gas purification device, a separator, a dust remover device and the like in the garbage incineration process. Fly ash is classified by the country as a solid hazardous waste (code HW 18) because it contains heavy metals, soluble salts and organic chlorides (polychlorinated biphenyl and dioxin). The main treatment method of the household garbage incineration fly ash at present comprises the following steps: cement solidification, hydrothermal treatment, fusion solidification, mineralization stabilization and the like. The fly ash is subjected to landfill treatment after solidification or stabilization treatment, a large amount of land resources are occupied by the landfill treatment, the landfill leachate is easy to pollute underground water and soil, and the environment is potentially threatened for a long time by the non-removed dioxin, heavy metals and salts. Therefore, the utilization of the fly ash as a resource is a new treatment means in the development of the fly ash treatment technology, and the harmless, decrement and resource treatment of the household garbage incineration fly ash can be truly realized.
Before the fly ash is recycled, heavy metals, chloride ions, dioxins and the like in the fly ash need to be removed so as to meet the emission requirement. At present, a water washing pretreatment method is mainly adopted to remove chloride ions in the fly ash, and meanwhile, chemical agents are used for fixing heavy metals in the fly ash, including sodium dihydrogen phosphate, phosphoric acid, sodium sulfide and the like, so that the dosage of the agents is large, the input cost is high, and secondary pollution exists.
At present, the ultra-low emission control technology of the atmospheric pollutants has the defects of low technical maturity, large initial investment, high operation cost, complex process and the like. Flue gas CO of power plant 2 The trapping mainly adopts a chemical absorption method, the flue gas passes through a denitration, desulfurization and dust removal device, enters an absorption tower, adopts an alcohol amine aqueous solution as an absorbent, and absorbs CO 2 The rich liquid enters a regeneration tower to be boiled, and CO is resolved 2 The whole process is complex and the cost is extremely high. Therefore, there is an urgent need to find a low-cost, high-efficiency technique for reducing the emission of atmospheric pollutants and carbon dioxide.
Disclosure of Invention
In view of the above, the utility model aims to provide a system for solidifying heavy metal of waste incineration fly ash and purifying smoke cooperatively.
In order to achieve the above purpose, the present utility model provides the following technical solutions:
the system comprises a low-temperature thermal degradation unit, a primary water washing tank, a primary centrifugal dehydrator, a secondary water washing tank, a secondary centrifugal dehydrator, a tertiary water washing tank and a tertiary centrifugal dehydrator, wherein an ash outlet of the low-temperature thermal degradation unit is communicated with an ash inlet of the primary water washing tank, a liquid outlet of the primary water washing tank is communicated with a liquid inlet of the primary centrifugal dehydrator, a slag outlet of the primary centrifugal dehydrator is communicated with a slag inlet of the secondary water washing tank, a liquid outlet of the secondary water washing tank is communicated with a liquid inlet of the secondary centrifugal dehydrator, a slag outlet of the secondary centrifugal dehydrator is communicated with a slag inlet of the tertiary water washing tank, and a liquid outlet of the tertiary water washing tank is communicated with a liquid inlet of the tertiary centrifugal dehydrator.
Further, the primary water washing tank, the secondary water washing tank and the tertiary water washing tank are respectively provided with a flue gas inlet.
Further, the flue gas is flue gas containing carbon dioxide.
Further, the water outlet of the secondary centrifugal dehydrator is communicated with the water inlet of the primary washing tank.
Further, the primary water washing tank is provided with a water inlet.
Further, the water outlet of the three-stage centrifugal dehydrator is communicated with the water inlet of the two-stage washing tank.
The utility model has the beneficial effects that:
according to the utility model, harmless treatment of the fly ash is combined with flue gas purification of a garbage incineration plant, and the heavy metal in the fly ash is fixed by utilizing carbon dioxide in the flue gas, so that the leaching concentration of the heavy metal in the fly ash is controlled below the maximum allowable emission concentration value specified in GB 8978, thereby effectively reducing the recycling treatment cost of the fly ash and reducing secondary pollution.
The fly ash of the utility model can wash part of SO in the flue gas 2 、NO x Atmospheric pollutants such as HCl and CO 2 And the greenhouse gas is absorbed, the emission of atmospheric pollutants is reduced, and the emission index of the atmospheric pollutants is improved.
The utility model has simple process, less investment and low operation cost, and has no influence on the whole fly ash recycling system.
Additional advantages, objects, and features of the utility model will be set forth in part in the description which follows and in part will become apparent to those having ordinary skill in the art upon examination of the following or may be learned from practice of the utility model. The objects and other advantages of the utility model may be realized and obtained by means of the instrumentalities and combinations particularly pointed out in the specification.
Drawings
For the purpose of making the objects, technical solutions and advantages of the present utility model more apparent, the present utility model will be described in the following preferred detail with reference to the accompanying drawings, in which:
FIG. 1 is a process flow diagram of the utility model.
Detailed Description
Other advantages and effects of the present utility model will become apparent to those skilled in the art from the following disclosure, which describes the embodiments of the present utility model with reference to specific examples. The utility model may be practiced or carried out in other embodiments that depart from the specific details, and the details of the present description may be modified or varied from the spirit and scope of the present utility model. It should be noted that the illustrations provided in the following embodiments merely illustrate the basic idea of the present utility model by way of illustration, and the following embodiments and features in the embodiments may be combined with each other without conflict.
Wherein the drawings are for illustrative purposes only and are shown in schematic, non-physical, and not intended to limit the utility model; for the purpose of better illustrating embodiments of the utility model, certain elements of the drawings may be omitted, enlarged or reduced and do not represent the size of the actual product; it will be appreciated by those skilled in the art that certain well-known structures in the drawings and descriptions thereof may be omitted.
The same or similar reference numbers in the drawings of embodiments of the utility model correspond to the same or similar components; in the description of the present utility model, it should be understood that, if there are terms such as "upper", "lower", "left", "right", "front", "rear", etc., that indicate an azimuth or a positional relationship based on the azimuth or the positional relationship shown in the drawings, it is only for convenience of describing the present utility model and simplifying the description, but not for indicating or suggesting that the referred device or element must have a specific azimuth, be constructed and operated in a specific azimuth, so that the terms describing the positional relationship in the drawings are merely for exemplary illustration and should not be construed as limiting the present utility model, and that the specific meaning of the above terms may be understood by those of ordinary skill in the art according to the specific circumstances.
Please refer to fig. 1, a system for purifying waste incineration fly ash heavy metal solidification cooperated with flue gas comprises a low-temperature thermal degradation unit, a first-stage water washing tank, a first-stage centrifugal dehydrator, a second-stage water washing tank, a second-stage centrifugal dehydrator, a third-stage water washing tank and a third-stage centrifugal dehydrator, wherein the low-temperature thermal degradation unit is used for removing dioxin in the fly ash, the first-stage water washing tank is provided with an ash outlet, the ash outlet of the low-temperature thermal degradation unit is communicated with the ash inlet of the first-stage water washing tank, and the first-stage water washing tank is used for carrying out first-stage water washing on the fly ash coming out of the low-temperature thermal degradation unit.
The primary water washing tank is provided with a liquid outlet, the primary centrifugal dehydrator is provided with a liquid inlet, the liquid outlet of the primary water washing tank is communicated with the liquid inlet of the primary centrifugal dehydrator, and the primary centrifugal dehydrator carries out centrifugal dehydration to obtain water washing liquid and ash. The primary centrifugal dehydrator is provided with a slag outlet and a liquid outlet, the secondary water washing tank is provided with a slag inlet, the slag outlet of the primary centrifugal dehydrator is communicated with the slag inlet of the secondary water washing tank, and fly ash subjected to primary centrifugal dehydration enters the secondary water washing tank for secondary water washing.
The secondary centrifugal dehydrator is provided with a slag outlet and a water outlet, the slag outlet of the secondary centrifugal dehydrator is communicated with the slag inlet of the tertiary washing tank, and the water outlet of the secondary centrifugal dehydrator is communicated with the water inlet of the primary washing tank.
The tertiary washing jar carries out the cubic washing to the flying dust that passes through secondary centrifugal dehydration, and tertiary washing jar is provided with the water inlet, and the washing liquid that the water inflow obtained from the centrifugal dehydrator of one-level is through the clear liquid after the water treatment, and tertiary washing jar is provided with the liquid outlet, and tertiary centrifugal dehydrator is provided with the inlet, and the liquid outlet of tertiary washing jar communicates with the inlet of tertiary centrifugal dehydrator, and tertiary centrifugal dehydrator obtains lime-ash and water through centrifugal dehydration, and the lime-ash that obtains this time can be as materials such as baking-free brick and building aggregate. The three-stage centrifugal dehydrator is provided with a water outlet, and the water outlet of the three-stage centrifugal dehydrator is communicated with the water inlet of the second-stage washing tank.
The primary water washing tank, the secondary water washing tank and the tertiary water washing tank are respectively provided with a flue gas inlet, and the primary water washing tank, the secondary water washing tank and the tertiary water washing tank are respectively filled with flue gas containing carbon dioxide from the flue gas inlet.
The specific method comprises the following steps:
s1: the fly ash is subjected to low-temperature thermal degradation to remove dioxin, and the pyrolysis temperature is preferably 350-450 ℃ and the pyrolysis time is 60-120 minutes when the low-temperature thermal degradation is performed in a low-temperature thermal degradation unit.
S2: primary water washing, namely, primary water washing is carried out in a primary water washing tank, and flue gas containing carbon dioxide is filled in the primary water washing tank, so that slurry is formed after water washing;
s3: carrying out primary centrifugal dehydration on the slurry subjected to primary water washing in a primary centrifugal dehydrator to obtain ash and water washing liquid;
s4: secondary water washing, namely performing secondary water washing on ash residues obtained through primary centrifugal dehydration in a secondary water washing tank, and filling smoke containing carbon dioxide into the ash residues to form slurry after the secondary water washing;
s5: carrying out secondary centrifugal dehydration, namely carrying out secondary centrifugal dehydration on slurry obtained through secondary water washing in a secondary centrifugal dehydrator to obtain ash and water, wherein the obtained water enters a primary water washing tank, and the obtained ash enters a tertiary water washing tank;
s6: three-stage water washing, namely, enabling ash residues obtained through two-stage centrifugal dehydration to enter a three-stage water washing tank for three-stage water washing to obtain slurry, and filling carbon dioxide-containing flue gas during water washing of the three-stage water washing tank;
s7: and carrying out third centrifugal dehydration on slurry obtained by three-stage water washing in a three-stage centrifugal dehydrator to obtain ash and water, wherein the obtained water enters a second-stage water washing tank, and the obtained ash can be used as materials such as baking-free bricks, building aggregate and the like.
The third-stage countercurrent washing of fly ash and carbonation of fly ash are carried out, carbon dioxide-containing flue gas is introduced into a first-stage washing tank, a second-stage washing tank and a third-stage washing tank, carbon dioxide in the flue gas is absorbed by alkaline solution in the washing process to generate carbonate, and the carbonate can react with heavy metal ions to produce precipitate so as to achieve the aim of fixing heavy metal, and the heavy metal in the solid slag of the fly ash washing is ensured to reach the standard by adjusting the flow of the flue gas and controlling the carbonation time.
Wherein the mass ratio of the fly ash to the water is 1:1-1:5, the water washing time is 15-60 min, and the stirring frequency is 60-300 r/min. The ratio of fly ash to flue gas in the water washing tank is 1:250-1:1250 (corresponding to 250-1250 Nm per ton of fly ash) 3 Smoke of/h), wherein the smoke component is CO 2 、SO 2 、NO x HCl, etc., CO 2 The content is 8-12%, SO 2 The content is 0.1-80 mg/m 3 ，NO x The content is 0.1-250 mg/m 3 HCl content of 0.1-50 mg/m 3 . The carbonation time is controlled between 1 and 5 hours. The water content of the ash after centrifugal dehydration is 40-50%.
Treating fly ash water washing liquid, carrying out decalcification, multistage filtration, pH adjustment and the like on the water washing liquid obtained by the primary centrifugal dehydration, and then carrying out evaporation crystallization and salt separation to obtain sodium chloride and potassium chloride.
The physicochemical property of the separated sodium salt can reach the second grade standard of the sun-cured industrial salt in industrial salt (GB/T5462-2015), and the potassium chloride meets the standard of class II (agricultural potassium chloride) in potassium chloride GB 6549-2011.
Examples:
the fly ash is subjected to low-temperature thermal degradation to remove dioxin, wherein the pyrolysis temperature is 400 ℃, and the pyrolysis time is 60 minutes.
And (3) three-stage countercurrent washing of the fly ash and carbonation of the fly ash.
Wherein the mass ratio of the fly ash to the water is 1:3, the water washing time is 30min, and the stirring frequency is 300r/min. The ratio of fly ash to flue gas in the water washing tank is 1:420 (420 Nm for each ton of fly ash) 3 Smoke of/h), wherein the smoke component is CO 2 、SO 2 、NO x HCl, etc., CO 2 The content is 10% SO 2 The content is 16.58mg/m 3 ，NO x The content is 172.05mg/m 3 HCl content of 4.70mg/m 3 . The carbonation treatment time is controlled to be 4 hours, the leaching concentration of heavy metal in fly ash after the carbonation treatment is lower than 1mg/L, and SO in flue gas 2 The concentration of NOx and HCl is reduced to 0.77mg/m 3 、134.11mg/m 3 、0.65mg/m 3 CO in flue gas 2 Reduced to 7%.
Finally, it is noted that the above embodiments are only for illustrating the technical solution of the present utility model and not for limiting the same, and although the present utility model has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications and equivalents may be made thereto without departing from the spirit and scope of the present utility model, which is intended to be covered by the claims of the present utility model.
Claims (6)
1. The utility model provides a system for waste incineration flying ash heavy metal solidification is flue gas purification in coordination which characterized in that: the low-temperature heat treatment device comprises a low-temperature heat degradation unit, a primary water washing tank, a primary centrifugal dehydrator, a secondary water washing tank, a secondary centrifugal dehydrator, a tertiary water washing tank and a tertiary centrifugal dehydrator, wherein an ash outlet of the low-temperature heat degradation unit is communicated with an ash inlet of the primary water washing tank, a liquid outlet of the primary water washing tank is communicated with a liquid inlet of the primary centrifugal dehydrator, a slag outlet of the primary centrifugal dehydrator is communicated with a slag inlet of the secondary water washing tank, a liquid outlet of the secondary water washing tank is communicated with a liquid inlet of the secondary centrifugal dehydrator, a slag outlet of the secondary centrifugal dehydrator is communicated with a slag inlet of the tertiary water washing tank, and a liquid outlet of the tertiary water washing tank is communicated with a liquid inlet of the tertiary centrifugal dehydrator.
2. The system for purifying waste incineration fly ash heavy metal solidification cooperative flue gas according to claim 1, wherein: the primary water washing tank, the secondary water washing tank and the tertiary water washing tank are respectively provided with a flue gas inlet.
3. The system for purifying waste incineration fly ash heavy metal solidification cooperative flue gas according to claim 2, wherein: the flue gas is carbon dioxide-containing flue gas.
4. The system for purifying waste incineration fly ash heavy metal solidification cooperative flue gas according to claim 1, wherein: the water outlet of the secondary centrifugal dehydrator is communicated with the water inlet of the primary washing tank.
5. The system for purifying waste incineration fly ash heavy metal solidification cooperative flue gas according to claim 1, wherein: the primary water washing tank is provided with a water inlet.
6. The system for purifying waste incineration fly ash heavy metal solidification cooperative flue gas according to claim 1, wherein: the water outlet of the three-stage centrifugal dehydrator is communicated with the water inlet of the two-stage washing tank.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222533057.0U CN219004061U (en) | 2022-09-23 | 2022-09-23 | System for waste incineration fly ash heavy metal solidification is flue gas purification in coordination |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222533057.0U CN219004061U (en) | 2022-09-23 | 2022-09-23 | System for waste incineration fly ash heavy metal solidification is flue gas purification in coordination |
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| CN219004061U true CN219004061U (en) | 2023-05-12 |
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