CN215745469U - Waste incineration fly ash treatment system - Google Patents
Waste incineration fly ash treatment system Download PDFInfo
- Publication number
- CN215745469U CN215745469U CN202121800086.8U CN202121800086U CN215745469U CN 215745469 U CN215745469 U CN 215745469U CN 202121800086 U CN202121800086 U CN 202121800086U CN 215745469 U CN215745469 U CN 215745469U
- Authority
- CN
- China
- Prior art keywords
- pipeline
- outlet
- pyrolyzer
- fly ash
- hot
- 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.)
- Active
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Abstract
The utility model discloses a waste incineration fly ash treatment system, which comprises a pyrolyzer, a roasting furnace, a melting furnace, a chilling device, a metal recovery device and a heat exchanger, wherein a pyrolysis gas outlet of the pyrolyzer is connected with a fuel inlet of the roasting furnace, a hot ash outlet of the pyrolyzer is connected with a material inlet of the roasting furnace, a hot slag outlet of the roasting furnace is connected with a material inlet of the melting furnace, a hot flue gas outlet of the melting furnace is connected with a heat source gas inlet of a heating chamber of the pyrolyzer, a hot flue gas outlet of the roasting furnace is connected with the heat exchanger, and an outlet of the heat exchanger is connected with the metal recovery device. Eliminating high-temperature and high-chlorine corrosion in the melting section, improving the treatment efficiency and reducing the cost.
Description
Technical Field
The utility model relates to the technical field of environmental protection and hazardous waste treatment, in particular to a waste incineration fly ash treatment system.
Background
The waste incineration fly ash contains metal, dioxin, chlorine salt, sulfate, carbonate and other harmful components, the fly ash is directly roasted or melted at 1100-1500 ℃, so that part of toxic metal in the fly ash can be fully sealed by a vitreous structure and the dioxin in the fly ash can be decomposed, however, the fly ash contains a large amount of chlorine salt such as CaCl2, the chlorine salt reacts with the metal in the fly ash to form metal chloride, the metal chloride has a low boiling point and is easy to volatilize, 98-100% of Pb, Cd and Cu volatilize under the air atmosphere of 1100 ℃, therefore, in the melting, solidifying and sintering treatment process, no matter how working condition parameters (temperature, time and additives) are changed, a part of metal in the fly ash still volatilizes, dust and coagulates are formed in the smoke condensation process to form secondary fly ash, and the content of some metals in the secondary fly ash is several times or even dozens of times higher than the content of metals in the fly ash, from the perspective of resource recycling, just because the secondary fly ash contains high content of metals, the secondary fly ash not only has important research value, but also has significance of recycling.
The low-temperature pyrolysis technology is derived from coal dry distillation, materials containing organic matters are subjected to heat treatment under the low-temperature condition of air isolation, the organic matters can be thermally volatilized or thermally decomposed to form pyrolysis gas, chloridizing roasting is a roasting method for enabling certain substances in the materials to react with a chlorinating agent to generate chlorides in the heating process so as to realize substance separation, and the roasting method is usually used for separating and recovering toxic and harmful metals in solid wastes. Compared with Cl2 and HCl, the solid chlorinating agents such as CaCl2, NaCl, KCl and the like are still in essence indirectly chlorinated by decomposing to generate chlorine simple substances, the solid chlorinating agents can be used for large-scale chlorination of solid materials, the corrosivity of the solid chlorinating agents to reaction equipment is much smaller than that of chlorine, the solid chlorinating agents are applied to the industry to a certain extent, and the original waste incineration fly ash contains a large amount of CaCl2, NaCl and other chlorine salts, so that the separation, enrichment and recycling of metals can be realized in a chlorination roasting mode.
In the prior art, the problems of key equipment development of direct high-temperature melting of fly ash and how to reduce energy consumption are mainly solved, and a process technology aiming at fly ash metal thermal separation is provided. The utility model patent with publication number CN111396893A discloses a melting chlorination roasting volatilization furnace and a method for harmless treatment of hazardous waste incineration substances, the core of the utility model is an L-shaped melting chlorination roasting volatilization furnace, although the metal can be recovered by chlorination volatilization, the boundary of a chlorination section and a melting section is not clear, the temperature is not easily controlled, and the chlorinated flue gas and the molten flue gas are mixed together, thereby increasing the flue gas treatment load; the utility model patent with publication number CN111112299A discloses a system and a method for treating incineration fly ash, the method takes the waste incineration fly ash as chlorinating agent, melts with metallurgical waste slag and recovers metals, but the chlorination and melting processes are both carried out in an electric arc melting furnace, the chlorination effect is limited and the quality of the smoke is not treated.
SUMMERY OF THE UTILITY MODEL
The technical problem to be solved by the present invention is to provide a system for graded temperature control and staged treatment of waste incineration fly ash, aiming at the defects of the prior art.
In order to realize the purpose, the technical scheme of the utility model is as follows:
the waste incineration fly ash treatment system comprises a pyrolyzer, a roasting furnace, a melting furnace, a metal recovery device and a heat exchanger;
furthermore, the pyrolyzer comprises a pyrolysis chamber and a heating chamber, wherein the pyrolysis chamber comprises a fly ash inlet, a pyrolysis gas outlet and a hot ash outlet, and the heating chamber comprises a heat source gas inlet and a heat source gas outlet; a heat source in the heating chamber indirectly heats the substances in the pyrolysis chamber, and the substances in the pyrolysis chamber are heated and analyzed;
further, a fuel inlet, a material inlet, a hot slag outlet and a hot flue gas outlet are arranged on the roasting furnace;
further, a material inlet, a molten slag outlet and a hot flue gas outlet are arranged on the melting furnace;
further, a pyrolysis gas outlet of the pyrolyzer is connected into a fuel inlet of the roasting furnace through a pipeline; a hot ash outlet of the pyrolyzer is connected with a material inlet of the roasting furnace;
further, a hot slag outlet of the roasting furnace is connected with a material inlet of the melting furnace through a pipeline;
further, a hot flue gas outlet of the melting furnace is connected with a heat source gas inlet of a heating chamber of the pyrolyzer through a pipeline;
furthermore, a hot flue gas outlet of the roasting furnace is connected with a heat exchanger, and an outlet of the heat exchanger is connected with a metal recovery device.
Further, the metal recovery device comprises a chilling device, a washing device, a water tank and a water pump;
further, the outlet of the heat exchanger is communicated with the chilling device through a pipeline;
further, a flue gas outlet arranged at the upper end of the chilling device is connected with a washing device through a pipeline; the lower end of the chilling device is connected with a second pipeline, and liquid in the chilling device is discharged into a water tank along the second pipeline;
furthermore, the upper end of the washing device is provided with a smoke outlet, the lower end of the washing device is connected with a third pipeline, and liquid in the washing device is discharged into a water tank along the third pipeline;
furthermore, one end of the water pump is connected into the water tank, the other end of the water pump is connected with the washing device through a first pipeline, the pipeline comprises a branch pipeline, and the branch pipeline is connected with the chilling device.
Further, the washing device is a venturi washing device, and the washing device comprises a venturi tube and a liquid remover connected with the venturi tube.
Further, the liquid carried in the water tank is alkaline liquid.
Further, the pyrolyzer is a low-temperature pyrolyzer, and the roasting furnace is a chlorination roasting furnace.
Furthermore, the hot ash outlet of the pyrolyzer is connected with the material inlet of the roasting furnace through a screw or a pipeline.
The utility model decomposes the traditional fly ash direct melting into three temperature sections of low-temperature pyrolysis pretreatment, chloridizing roasting and high-temperature melting by means of graded temperature control and sectional treatment, and compared with the prior art, the utility model has the following beneficial effects:
1. in the thermal decomposition stage, the fly ash is preheated to 200-500 ℃ by utilizing the heat of hot flue gas discharged by the melting furnace, dioxin organic matters in the fly ash are heated and analyzed to form pyrolysis gas, the hot ash is directly and thermally sent to the chlorination roasting furnace, the fuel consumption required in the chlorination roasting stage is reduced, the utility model decouples the traditional direct melting of the fly ash into low-temperature pyrolysis pretreatment by means of graded temperature control and segmented treatment, the treatment process of three temperature sections of chloridizing roasting and high-temperature melting, the fly ash is reduced step by step, and the flue gas of each section is not mixed with each other, so that the metal chloridizing separation and enrichment and the thorough decomposition of dioxin in the waste incineration fly ash can be realized, the aim of detoxifying the fly ash is achieved, the ineffective heating can be reduced, the flue gas of different sections is subjected to quality-based treatment, finally, the molten product glassy slag can be used as a building material raw material for utilization, and the heavy metal recovery can be further recycled as a metallurgical raw material.
2. The low-temperature pyrolysis section of the original fly ash is arranged, the low-temperature pyrolysis reaction is carried out by utilizing the waste heat of the flue gas, the original fly ash is thermally decomposed into the hot ash and the pyrolysis gas, and dioxin organic pollutants are in the pyrolysis gas and are efficiently analyzed out of the dioxin organic pollutants in the original fly ash.
3. The utility model utilizes the characteristics that the fly ash is rich in chloride salt and secondary fly ash is easy to form in the high-temperature melting process, a chlorination roasting section is arranged before the high-temperature melting section, so that the quality-divided treatment of flue gas in the chlorination section and the melting section can be realized, the flue gas treatment capacity and the pollutant control effect are reduced, gas-phase pollutants in the fly ash heat treatment process are concentrated in the chlorination roasting section to be released, namely volatile metal chlorides, small molecular compounds and the like are concentrated in hot flue gas I, the hot flue gas I sequentially passes through an air heat exchanger (800-850 ℃), a chilling chamber (180-200 ℃), a Venturi washing chamber (less than or equal to 50 ℃), and a dry method and a wet method combined recovery and purification process of three temperature sections is adopted, so that the secondary synthesis of dioxin can be prevented, heavy metal volatile matters with different freezing points can be recovered, and the flue gas can be discharged up to the standard.
4. The high-temperature melting section is arranged behind the chloridizing roasting section, the hot slag containing the metal oxides which are not easy to volatilize enters the melting section, and only the reduced and detoxified hot slag is required to be continuously heated to the melting temperature and then chilled to form vitreous body slag, so that the residual heavy metal is solidified in the vitreous body; compared with direct melting, the method greatly reduces the flue gas treatment capacity and treatment cost, the flue gas in the melting section almost does not contain pollutants, the problem of high-temperature and high-chlorine corrosion in the melting section is solved, the flue gas can be directly discharged after waste heat utilization, and the treatment efficiency and the treatment cost are greatly improved.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention.
FIG. 2 is a schematic flow chart of the present invention.
In the figure: 1-a pyrolyzer; 2, roasting the furnace; 3-melting furnace; 4-chilling device; 5-a washing device; 51-a venturi tube; 52-liquid removal device; 6, a water pool; 7, a water pump; 8, a heat exchanger; 9-a first conduit; 91-branch pipes; 10-a second conduit; 11-third conduit.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention clearer, the present invention is further described below with reference to the accompanying drawings.
The waste incineration fly ash treatment system comprises a pyrolyzer 1, a roasting furnace 2, a melting furnace 3, a metal recovery device and a heat exchanger 8.
The pyrolyzer 1 is a low-temperature pyrolyzer, the low-temperature pyrolyzer 1 is an anoxic or anaerobic atmosphere furnace provided with a stirring inner component, and original fly ash is pyrolyzed indirectly by utilizing a heat source, such as hot flue gas.
The roasting furnace 2 is a chlorination roasting furnace, the chlorination roasting furnace 2 is a gas type or electric heating type furnace commonly used in the field of mineral separation and smelting, and is one of furnace types such as a fluidized roasting furnace, a multi-hearth roasting furnace, a shaft furnace, a rotary kiln and the like, or is a combined roasting furnace, and the roasting atmosphere is air atmosphere or oxygen-enriched atmosphere.
The chlorination roasting furnace 2 can be a one-section type chlorination roasting device and a two-section combined type chlorination roasting device according to the chlorine salt content of the fly ash; when the chlorine salt content of the fly ash is more than or equal to 10 wt% -20 wt%, a one-stage type chlorination roasting device is preferably selected; on the contrary, a two-section combined chlorination roasting device is preferred, namely, the fly ash is roasted to the chlorination segregation temperature in the first-section furnace, and then the chlorinating agent is added into the second-section furnace and the atmosphere is adjusted, so that the chlorination segregation effect is ensured.
The melting furnace 3 is a gas-fired melting furnace or an electric melting furnace.
The low-temperature pyrolyzer 1 comprises a pyrolysis chamber and a heating chamber, wherein a heat source in the heating chamber indirectly heats the pyrolysis chamber; the pyrolysis chamber comprises a fly ash inlet, a pyrolysis gas outlet and a hot ash outlet, and the heating chamber comprises a heat source gas inlet and a heat source gas outlet.
The chlorination roasting furnace 2 is provided with a fuel inlet, a material inlet, a hot slag outlet and a hot flue gas outlet.
The melting furnace 3 is provided with a material inlet, a molten slag outlet and a hot flue gas outlet.
The pyrolysis gas outlet of the low-temperature pyrolyzer 1 is connected to the fuel inlet of the chlorination roaster 2 through a pipeline.
The hot ash outlet of the low-temperature pyrolyzer 1 is connected with the material inlet of the chlorination roasting furnace 2 through a screw or a pipeline.
The hot slag outlet of the chlorination roasting furnace 2 is connected with the material inlet of the melting furnace 3 through a pipeline.
The hot flue gas outlet of the chlorination roasting furnace 2 is connected with an air heat exchanger 8 with an ash removal function, and the temperature of the flue gas outlet of the heat exchanger 8 is 800-850 ℃.
The metal recovery device comprises a chilling device 4, a washing device 5, a water tank 6 and a water pump 7, wherein the outlet of a heat exchanger 8 passes through a pipeline and a chilling deviceThe device 4 is communicated; the chilling device 4 is water-cooled, the washing device 5 is a Venturi washing device, and the liquid in the water tank 6 is alkaline solution, such as NaOH and Ca (OH)2And when the pH value of the alkaline solution is 10-12, the alkaline solution is used for precipitation separation and acid gas absorption of metal chlorides, and the water pump 7 realizes circulation of the alkaline liquid among the chilling device 4, the washing device 5 and the water tank 6.
The original fly ash of the waste incineration enters a pyrolysis chamber through a fly ash inlet of a low-temperature pyrolyzer 1, a heat source in a heating chamber of the low-temperature pyrolyzer 1 indirectly heats the original fly ash in the pyrolysis chamber, the heat source can be natural gas when the device is started, and a heat source is hot flue gas II after the system is stabilized; carrying out low-temperature pyrolysis on original fly ash in a pyrolysis chamber at the temperature of 200-500 ℃ to obtain pyrolysis gas and hot ash; the pyrolysis gas is discharged from a pyrolysis gas outlet of a low-temperature pyrolyzer 1, enters a chlorination roasting furnace 2 through a fuel inlet of the chlorination roasting furnace 2 for roasting, the hot ash is discharged from a hot ash outlet of the low-temperature pyrolyzer 1, enters the chlorination roasting furnace 2 through a material inlet of the chlorination roasting furnace 2 for roasting, and the pyrolysis gas and the hot ash are roasted in the chlorination roasting furnace 2 at the temperature of 800-1100 ℃ for 10-100 min to obtain hot slag and hot flue gas I; the hot slag is discharged from a hot slag outlet of the chlorination roasting furnace 2, enters the melting furnace 3 through a material inlet of the melting furnace 3, is melted at high temperature of 1200-1450 ℃ to form liquid slag and generate hot flue gas II, the liquid slag is discharged from a molten slag outlet of the melting furnace 3, the liquid slag is cooled after being discharged to form glassy slag, and the glassy slag can be periodically collected to be used as roadbed materials, building materials and the like.
In the chlorination roasting furnace 2, chlorine salt in the fly ash reacts with metal oxide and the like to form metal chloride, so that the separation of metal from the fly ash is realized, and the metal chloride is enriched in hot flue gas I and is discharged from a hot flue gas outlet of the chlorination roasting furnace 2 along with the hot flue gas I to enter a heat exchanger 8.
The dioxin can be decomposed by 100% almost after being roasted for 10min to 100min at the temperature of more than 800 ℃, so that the dioxin in the fly ash is completely decomposed into small molecular compounds in the chlorination roasting furnace 2 and is discharged from a hot flue gas outlet of the chlorination roasting furnace 2 along with the hot flue gas I to enter the heat exchanger 8.
The hot flue gas I generated in the chlorination roasting furnace 2 is dust-containing high-temperature flue gas containing metal chlorides and micromolecular compounds, the hot flue gas I is discharged from a hot flue gas outlet of the chlorination roasting furnace 2 and enters an air heat exchanger 8 with an ash removal function, an outlet of the heat exchanger 8 is connected with a chilling device 4 through a pipeline, and the hot flue gas I further enters the chilling device 4.
The venturi device 5 comprises a venturi tube 51 and a liquid remover 52, the venturi tube 51 is communicated with the liquid remover 52, the water pump 7 is connected with the water tank 6, the water pump 7 is connected with the venturi tube 51 through a first pipeline 9, the first pipeline 9 comprises a branch pipeline 91, the branch pipeline 91 is connected with the chilling device 4, the branch pipeline 91 is connected with a spray head, and the spray head is positioned inside the chilling device 4; the upper end of the chilling device 4 is provided with a flue gas outlet which is connected with a Venturi tube 51 through a pipeline, and the lower end of the chilling device 4 is connected with a second pipeline 10.
The upper end of the liquid remover 52 is provided with a smoke outlet, the lower end is connected with a third pipeline 11, and the liquid in the third pipeline 11 flows into the water tank 6.
Since the second pipe 10 is connected to the third pipe 11, the second pipe 10 may not be provided with a valve, and the third pipe 11 may be provided with a valve to control the liquid discharge of the second pipe 10 and the third pipe 11.
Under the action of the water pump 7, the alkaline solution in the water tank 6 is sprayed into the chilling device 4 through the first pipeline 9, the branch pipeline 91 and the spray header, the temperature of the hot flue gas I in the chilling device 4 is cooled and washed, the temperature of the hot flue gas I in the chilling device 4 is rapidly reduced to 180-200 ℃, part of the flue dust containing metal chloride flows into the second pipeline 10 along with the alkaline solution, then flows to the third pipeline 11 from the second pipeline 10, and is discharged into the water tank 6 from the third pipeline 11.
The micromolecular compound after the dioxin is decomposed can be synthesized into the dioxin again at the temperature of 270-500 ℃, and the temperature of hot flue gas I in the chilling device 4 is rapidly reduced to be below 200 ℃ through the rapid chilling of the chilling device 4, so that the secondary synthesis of the dioxin is prevented.
After the hot flue gas I is cooled and washed in the chilling device 4, the hot flue gas I is discharged from a flue gas discharge port arranged at the upper end of the chilling device 4, and then enters the venturi tube 51 and further enters the liquid removing device 52 through a pipeline connected between the flue gas discharge port and the venturi tube 51.
Under the action of the water pump 7, alkaline solution in the water tank 6 enters the liquid remover 52 through the pipeline 9 and the venturi tube 51; the hot flue gas I is cooled and washed again in the liquid remover 52 by the alkaline solution, the temperature of the hot flue gas I in the liquid remover 52 is reduced to below 50 ℃, the flue dust containing metal chloride flows into the third pipeline 11 along with the alkaline solution in the liquid remover 52, and is discharged into the water pool 6 from the third pipeline 11; after the hot flue gas I is purified in the liquid remover 52, the purified hot flue gas I is discharged into the atmosphere from the flue gas discharge port at the upper part of the liquid remover 52, and small molecular compounds in the hot flue gas I are discharged into the atmosphere from the flue gas discharge port at the upper part of the liquid remover 52 along with the hot flue gas I because the small molecular compounds decomposed by dioxin are nontoxic and harmless and reach the discharge standard.
The metal chloride and the micromolecule compound are discharged from a hot smoke outlet of the chlorination roasting furnace 2 along with hot smoke I and enter a heat exchanger 8, hot smoke II generated by combustion in the melting furnace 3 is high-temperature smoke without the metal chloride and the micromolecule compound, the hot smoke II is discharged from a hot smoke outlet of the melting furnace 3 and enters a heating chamber through a pipeline and a heat source gas inlet of the heating chamber of the low-temperature pyrolyzer 1 to be used as a heat source for indirectly heating the fly ash in the pyrolysis chamber of the low-temperature pyrolyzer 1, the temperature of the hot smoke II is reduced after heat exchange in the heating chamber of the low-temperature pyrolyzer 1, and the cooled hot smoke II is discharged to the atmosphere from a heat source gas outlet of the heating chamber of the low-temperature pyrolyzer 1.
In the utility model, the heat of hot flue gas II discharged by a melting furnace 3 is recovered as a heat source of a pyrolyzer 1 in the thermal decomposition stage, original fly ash is indirectly preheated to 200-500 ℃ to be thermally decomposed into hot ash, and then the hot ash at 200-500 ℃ is introduced into a chlorination roasting furnace 2 to be roasted; if the original fly ash is directly introduced into the chlorination roasting furnace, the fly ash needs to additionally consume fuels such as natural gas and the like from the normal temperature to 200-500 ℃; the utility model recovers the heat of the hot flue gas II exhausted by the melting furnace 3 to preheat the original fly ash, and reduces the fuel consumption in the chlorination roasting stage compared with the method of directly introducing the original fly ash into the chlorination roasting furnace.
The metal chloride is sprayed and washed by alkaline liquid in the chilling device 4 and washed by the alkaline liquid in the washing device 5, finally the metal chloride enters the water tank 6 containing the alkaline liquid along with the alkaline liquid through the third pipeline 11, the metal chloride and the alkali liquor are subjected to chemical reaction to realize the separation of the metal chloride, the metal is decomposed, the enrichment of the metal in the water tank 6 is further realized, and the metal chloride enriched to a certain concentration can be further recycled as a metallurgical raw material.
It should be noted that: while the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to one skilled in the art that various changes in the form and details may be made therein without departing from the spirit and scope of the utility model. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (6)
1. A waste incineration fly ash treatment system is characterized by comprising a pyrolyzer (1), a roasting furnace (2), a melting furnace (3), a metal recovery device and a heat exchanger (8);
the pyrolyzer (1) comprises a pyrolysis chamber and a heating chamber, wherein the pyrolysis chamber comprises a fly ash inlet, a pyrolysis gas outlet and a hot ash outlet, and the heating chamber comprises a heat source gas inlet and a heat source gas outlet; a heat source in the heating chamber heats the material in the pyrolysis chamber;
the roasting furnace (2) is provided with a fuel inlet, a material inlet, a hot slag outlet and a hot flue gas outlet;
the melting furnace (3) is provided with a material inlet, a molten slag outlet and a hot flue gas outlet;
a pyrolysis gas outlet of the pyrolyzer (1) is connected into a fuel inlet of the roasting furnace (2) through a pipeline; a hot ash outlet of the pyrolyzer (1) is connected with a material inlet of the roasting furnace (2);
a hot slag outlet of the roasting furnace (2) is connected with a material inlet of the melting furnace (3) through a pipeline;
a hot flue gas outlet of the melting furnace (3) is connected with a heat source gas inlet of a heating chamber of the pyrolyzer (1) through a pipeline;
the hot flue gas outlet of the roasting furnace (2) is connected with a heat exchanger (8), and the outlet of the heat exchanger (8) is connected with a metal recovery device.
2. The waste incineration fly ash treatment system according to claim 1, wherein the metal recovery device comprises a chilling device (4), a washing device (5), a water tank (6), a water pump (7) and a pipeline;
the outlet of the heat exchanger (8) is communicated with the chilling device (4) through a pipeline;
a flue gas outlet arranged at the upper end of the chilling device (4) is connected with a washing device (5) through a pipeline; the lower end of the chilling device (4) is connected with a second pipeline (10), and liquid in the chilling device (4) is discharged into the water tank (6) along the second pipeline (10);
the upper end of the washing device (5) is provided with a smoke outlet, the lower end of the washing device (5) is connected with a third pipeline (11), and liquid in the washing device (5) is discharged into the water tank (6) along the third pipeline (11);
one end of the water pump (7) is connected into the water tank (6), the other end of the water pump is connected with the washing device (5) through a first pipeline (9), the pipeline (9) comprises a branch pipeline (91), and the branch pipeline (91) is connected with the chilling device (4).
3. The system for treating fly ash from waste incineration according to claim 2, wherein the washing device (5) is a venturi washing device, and the washing device (5) comprises a venturi tube (51) and a liquid remover (52) connected to the venturi tube (51).
4. The system for treating fly ash from waste incineration of claim 2, wherein the liquid contained in the pool (6) is an alkaline liquid.
5. The system according to claim 1, wherein the pyrolyzer (1) is a low temperature pyrolyzer and the roaster (2) is a chlorinator.
6. The waste incineration fly ash treatment system according to claim 1, characterized in that the hot ash outlet of the pyrolyzer (1) is connected to the material inlet of the calciner (2) by means of a screw or a pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121800086.8U CN215745469U (en) | 2021-08-03 | 2021-08-03 | Waste incineration fly ash treatment system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121800086.8U CN215745469U (en) | 2021-08-03 | 2021-08-03 | Waste incineration fly ash treatment system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN215745469U true CN215745469U (en) | 2022-02-08 |
Family
ID=80109623
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202121800086.8U Active CN215745469U (en) | 2021-08-03 | 2021-08-03 | Waste incineration fly ash treatment system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN215745469U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113714246A (en) * | 2021-08-03 | 2021-11-30 | 武汉武锅能源工程有限公司 | Waste incineration fly ash treatment system and method |
-
2021
- 2021-08-03 CN CN202121800086.8U patent/CN215745469U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113714246A (en) * | 2021-08-03 | 2021-11-30 | 武汉武锅能源工程有限公司 | Waste incineration fly ash treatment system and method |
| CN113714246B (en) * | 2021-08-03 | 2022-12-23 | 武汉武锅能源工程有限公司 | Waste incineration fly ash treatment system and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109539272A (en) | The high-temperature plasma recycling recovery process of waste containing chlorine and system | |
| CN108480360B (en) | Method for recycling fly ash resources and discharging tail gas in ultra-clean mode by melting method of rotary kiln | |
| CN211247720U (en) | Plasma fusion vitrification device and waste incineration fly ash treatment system | |
| CN113714246B (en) | Waste incineration fly ash treatment system and method | |
| CN112795776B (en) | Method for co-processing waste incineration fly ash and copper-containing sludge | |
| CN106987275A (en) | The high-temperature plasma gasification and melting processing system and method for trade waste | |
| CA2118003A1 (en) | Plasma torch processing of spent aluminum smelter potliner | |
| CN112808746B (en) | Resource treatment method for incineration slag and fly ash | |
| CN110479734B (en) | Method and device for innocent treatment of industrial waste salt by using alkaline melt | |
| CN206385096U (en) | The high-temperature plasma gasification and melting processing system of trade waste | |
| CN106984633A (en) | Utilize the method for plasma torch recycling treatment incineration of refuse flyash | |
| CN215745469U (en) | Waste incineration fly ash treatment system | |
| CN109737430A (en) | A kind of hazardous waste processing system and method | |
| CN107746066A (en) | Ammonium chloride preparation system and method for lime-ash plasma melting processing system | |
| CN105502543A (en) | Method for recycling coal chemical industry high-salt wastewater by blind coal oxygen-rich combustion process | |
| CN209309994U (en) | The high-temperature plasma resource utilization system of waste containing chlorine | |
| JP3361517B2 (en) | Waste treatment method by oxygen combustion | |
| CN113667827A (en) | Method for co-processing waste incineration fly ash and copper-containing sludge | |
| CN211204070U (en) | High organic waste liquid incineration disposal system that contains salt | |
| CN211232880U (en) | High, low calorific value hazardous waste burns melting innocent treatment system in coordination | |
| JP3878994B2 (en) | Method and apparatus for producing useful gas from halogen-containing combustible material and alkali-containing material | |
| CN113441536A (en) | Fly ash treatment system and fly ash treatment method | |
| CN112676315A (en) | Harmless resource treatment improvement method for waste incineration fly ash | |
| JP3774994B2 (en) | Resource separation method and equipment | |
| JPH11300157A (en) | Dry type removing method of hydrogen chloride in exhaust gas, and dry type removing device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |