CN110762537A - Method and device for co-processing incineration fly ash and gasification fly ash - Google Patents
Method and device for co-processing incineration fly ash and gasification fly ash Download PDFInfo
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- CN110762537A CN110762537A CN201911118121.5A CN201911118121A CN110762537A CN 110762537 A CN110762537 A CN 110762537A CN 201911118121 A CN201911118121 A CN 201911118121A CN 110762537 A CN110762537 A CN 110762537A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
Abstract
The invention provides a method and a device for co-processing incineration fly ash and gasification fly ash, belonging to the technical field of fly ash processing. The incineration fly ash and the gasification fly ash are mixed and undergo gasification-melting reaction or combustion-melting reaction in an oxygen-containing atmosphere to obtain liquid slag and a mixed gas product, wherein the mixed gas product is combustible gas or flue gas; the liquid slag forms glassy state slag after first cooling treatment; and the mixed gas product is subjected to secondary cooling treatment, gas dedusting treatment and gas purification treatment in sequence to obtain purified combustible gas or purified flue gas, the purified combustible gas is collected and recycled, and the purified flue gas is discharged up to the standard. The method provided by the invention utilizes the self heat value of the gasified fly ash in the gasification or combustion process without adding auxiliary fuel; and by utilizing the inorganic salt components in the two fly ashes, the ash content of the gasified fly ashes and the incineration fly ashes form an auxiliary material with a glass component without adding extra materials in the melting process, so the production cost is low, and the method is suitable for large-scale production.
Description
Technical Field
The invention relates to the technical field of fly ash disposal, in particular to a method and a device for co-disposal of incineration fly ash and gasification fly ash.
Background
The incineration fly ash comprises waste incineration fly ash and hazardous waste incineration fly ash, and the two types of fly ash are listed in 2016 edition of national hazardous waste records and belong to hazardous waste (HW18) due to the enrichment of various heavy metals and dioxin pollutants.
The waste incineration fly ash is a residue collected by a flue gas purification system of a domestic waste incineration plant, and the waste incineration fly ash has a large production amount and is one of the key points and difficulties in hazardous waste management in China. At present, more than 300 urban domestic garbage incineration plants in China have been produced, the annual incineration treatment capacity reaches 7000 ten thousand tons, the yield of the waste incineration fly ash is related to the types of the waste, the incineration conditions, the type of the incinerator and the flue gas treatment process, and 350-560 ten thousand tons of waste incineration fly ash are produced every year according to the proportion of 5-8% of the fly ash. The waste incineration fly ash is dark gray or grey white, the average particle size is generally 40-60 mu m, the content of soluble salt taking chlorides of K, Na and Ca as main bodies is 15-25%, and the waste incineration fly ash contains various heavy metals, dioxin and other hazardous substances.
The hazardous waste incineration fly ash is a residue collected by a flue gas purification system of a hazardous waste incineration plant, is large in production amount and strong in harmfulness, and is also one of the key points and difficulties in hazardous waste management in China. In 2018, the amount of hazardous waste in China is 400 ten thousand tons in an incineration mode, the amount of fly ash generated by incinerating the hazardous waste is 20-40 ten thousand tons according to the calculation of the fly ash generation proportion of 5-10%. The hazardous waste incineration fly ash and the waste incineration fly ash have the characteristics of low water content, irregular shape, high porosity, small particle size (average particle size is generally 40-60 mu m), large specific surface area and the like, and the main components are Na, Ca, K, Cl, S, Si and the like.
At present, incineration fly ash is mainly stabilized and solidified for safe landfill, but the storage capacity of a landfill site is limited, and the solidification mode needs to be improved, for example, the incineration fly ash is solidified by adopting a chelating agent, so that the stability of the chelating agent needs to be improved. Based on this, expert scholars actively research and develop the harmless and resource treatment method of incineration fly ash, most typically is the fly ash high-temperature melting vitrification technique, the technique can stably solidify heavy metals in incineration fly ash through heat treatment processes such as electricity, fuel melting vitrification and the like, but needs to consume more energy for realizing incineration fly ash melting; in addition, in order to reduce the ash melting point and facilitate the formation of a glass body, a certain amount of Ca, Al and Si inorganic salt is additionally added in the melting process, so that the material consumption is increased. Therefore, the technology needs to consume a large amount of energy and has higher treatment cost.
In recent years, coal gasification technology plays an extremely important role in economic development of China, but part of unreacted carbon and fine slag in the gasification process can be brought out by synthesis gas to generate a certain amount of gasification fly ash, and the annual output is preliminarily estimated to be 50-100 ten thousand tons. The gasification fly ash has a calorific value of 2500-4000 kCal/kg and an average particle size of 30-50 μm. At present, gasified fly ash is usually used for road engineering, mine backfilling or soil improvement, so that the calorific value of the gasified fly ash and the contained unburned carbon cannot be directly utilized, and resource waste is caused.
Disclosure of Invention
The invention aims to provide a method and a device for co-processing incineration fly ash and gasification fly ash, the method provided by the invention can realize harmless treatment and resource utilization of the incineration fly ash and the gasification fly ash, does not need to adopt additional auxiliary materials, has low production cost and is suitable for large-scale production.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides a method for co-processing incineration fly ash and gasification fly ash, which comprises the following steps:
mixing incineration fly ash and gasification fly ash, and carrying out gasification-melting reaction or combustion-melting reaction in an oxygen-containing atmosphere to obtain liquid slag and a mixed gas product, wherein the mixed gas product is combustible gas or flue gas;
the liquid slag forms glassy state slag after first cooling treatment;
and the mixed gas product is subjected to secondary cooling treatment, gas dedusting treatment and gas purification treatment in sequence to obtain purified combustible gas or purified flue gas, the purified combustible gas is collected and recycled, and the purified flue gas is discharged up to the standard.
Preferably, the incineration fly ash comprises waste incineration fly ash and/or hazardous waste incineration fly ash.
Preferably, when the gasification-fusion reaction is carried out, the mass of the incineration fly ash is 5-15% of that of the gasification fly ash; and the mixed gas product obtained after the gasification-melting reaction is combustible gas.
Preferably, the temperature of the system in the gasification-melting reaction process is 1350-1550 ℃.
Preferably, when the combustion-melting reaction is carried out, the mass of the incineration fly ash is 20-50% of that of the gasification fly ash; and the mixed gas product obtained after the combustion-melting reaction is flue gas.
Preferably, the temperature of the system in the combustion-melting reaction process is 1400-1600 ℃.
Preferably, the first cooling treatment is to cool the material to be less than or equal to 100 ℃; the second cooling treatment is to cool the materials to be less than or equal to 160 ℃.
The invention provides a device for co-processing incineration fly ash and gasification fly ash, which comprises a storage tank, a feeding bin and an entrained flow bed which are sequentially communicated, wherein the top of the entrained flow bed is connected with an ignition system and a primary air pipeline in parallel, the bottom of the entrained flow bed is provided with a slag discharging-cooling system, and an exhaust port of the entrained flow bed is sequentially communicated with a gas cooling system, a gas dedusting system and a gas purification system.
Preferably, the device further comprises a nitrogen production system, and two air outlets of the nitrogen production system are respectively communicated with the feeding bin and the gas dedusting system.
Preferably, the slag discharging-cooling system comprises a slag discharging valve and a slag discharging tank, the slag discharging tank is connected with the entrained flow bed through the slag discharging valve, and the cooling medium in the slag discharging tank is water.
The invention provides a method for co-processing incineration fly ash and gasification fly ash, which comprises the following steps: mixing incineration fly ash and gasification fly ash, mixing the incineration fly ash and the gasification fly ash, and carrying out gasification-melting reaction or combustion-melting reaction in an oxygen-containing atmosphere to obtain liquid slag and a mixed gas product, wherein the mixed gas productThe substance is combustible gas or flue gas; the liquid slag forms glassy state slag after first cooling treatment; and the mixed gas product is subjected to secondary cooling treatment, gas dedusting treatment and gas purification treatment in sequence to obtain purified combustible gas or purified flue gas, the purified combustible gas is collected and recycled, and the purified flue gas is discharged up to the standard. The incineration fly ash and the gasification fly ash are co-treated, the ash content of the gasification fly ash and the incineration fly ash are co-melted by utilizing the high temperature generated by gasification or combustion of the gasification fly ash in an oxygen-containing atmosphere, and glassy slag is formed after cooling, can be used as building materials, and realizes harmless treatment and resource utilization. Therefore, the method provided by the invention utilizes the self heat value of the gasified fly ash in the gasification or combustion process without adding auxiliary fuel; and utilizes the self inorganic salt components (CaO, SiO) in the two fly ashes2、Al2O3) And in the melting process, the ash content of the gasified fly ash and the incineration fly ash do not need to be additionally added to form an auxiliary material with a glass component, so that the production cost is low, and the method is suitable for large-scale production.
The invention provides a device for co-processing incineration fly ash and gasification fly ash, which comprises a storage tank, a feeding bin and an entrained flow bed which are sequentially communicated, wherein the top of the entrained flow bed is connected with an ignition system and a primary air pipeline in parallel, the bottom of the entrained flow bed is provided with a slag discharging-cooling system, and an exhaust port of the entrained flow bed is sequentially communicated with a gas cooling system, a gas dedusting system and a gas purification system. The device provided by the invention has a reasonable structure, does not need special or expensive components, is simple to operate, and can realize the co-treatment of incineration fly ash and gasification fly ash.
Drawings
FIG. 1 is a schematic structural view of an apparatus for co-processing incineration fly ash and gasification fly ash in the present invention;
FIG. 2 is another schematic view of the apparatus for co-processing incineration fly ash and gasification fly ash in the present invention;
FIG. 3 is a flow chart of a gasification-melting process in co-disposal of incineration fly ash and gasification fly ash in the present invention;
FIG. 4 is a flow chart of the combustion-melting process in the co-disposal of incineration fly ash and gasification fly ash in the present invention;
in the figure, 1-1 is an incineration fly ash storage tank, 1-1-1 is a waste incineration fly ash storage tank, 1-1-2 is a hazardous waste incineration fly ash storage tank, 1-2 is a gasification fly ash storage tank, 2 is a feeding bin, 3 is an entrained flow bed, 4 is an ignition system, 5 is a primary air pipeline, 6 is a slag discharge-cooling system, 7 is a gas cooling system, 8 is a gas dedusting system, 9 is a gas purification system, and 10 is a nitrogen production system.
Detailed Description
The invention provides a method for co-processing incineration fly ash and gasification fly ash, which comprises the following steps:
mixing incineration fly ash and gasification fly ash, and carrying out gasification-melting reaction or combustion-melting reaction in an oxygen-containing atmosphere to obtain liquid slag and a mixed gas product, wherein the mixed gas product is combustible gas or flue gas;
the liquid slag forms glassy state slag after first cooling treatment;
and the mixed gas product is subjected to secondary cooling treatment, gas dedusting treatment and gas purification treatment in sequence to obtain purified combustible gas or purified flue gas, the purified combustible gas is collected and recycled, and the purified flue gas is discharged up to the standard.
The incineration fly ash and the gasification fly ash are mixed and undergo gasification-melting reaction or combustion-melting reaction in an oxygen-containing atmosphere to obtain liquid slag and a mixed gas product, wherein the mixed gas product is combustible gas or flue gas. In the invention, the incineration fly ash and the gasification fly ash are mixed and ignited in an oxygen-containing atmosphere, carbon contained in the gasification fly ash is subjected to gasification reaction or sufficient combustion under the action of oxygen, and the correspondingly obtained mixed gas product is combustible gas (the calorific value is 1500-2000 kCal/kg, and the contained combustible components comprise CO and H2) Or the flue gas releases a large amount of heat simultaneously, so that the ash content of the incineration fly ash and the gasification fly ash can be fully melted to form liquid slag.
In the present invention, the incineration fly ash preferably includes waste incineration fly ash and/or hazardous waste incineration fly ash, the waste incineration fly ash specifically refers to a residue collected by a flue gas purification system of a domestic waste incineration plant, and the hazardous waste incineration fly ash specifically refers to a residue collected by a flue gas purification system of a hazardous waste incineration plant. The specific sources of the waste incineration fly ash and the hazardous waste incineration fly ash are not specially limited, and any source can be used. In the invention, the average particle size of the incineration fly ash is preferably 40-60 μm.
In the invention, the gasification fly ash is formed by taking out part of unreacted carbon and fine slag from synthesis gas in the coal gasification process, and the average particle size is preferably 30-50 μm; the specific source of the gasified fly ash is not particularly limited, and any source can be used.
In the invention, the proportion of the incineration fly ash and the gasification fly ash and the oxygen consumption can influence the chemical reaction process of the system after ignition, and the specific steps are as follows: the mass of the incineration fly ash is 5-15% of that of the gasification fly ash, when the system is in an oxygen-poor state (namely the oxygen content is relatively insufficient), gasification-melting reaction mainly occurs in the system, the temperature of the system can reach 1350-1550 ℃ by utilizing the heat released by gasification of the gasification fly ash (carbon is generated into CO through gasification reaction), and the ash content of the incineration fly ash and the gasification fly ash is fully melted; the mass of the incineration fly ash is 20-50% of that of the gasification fly ash, when the system is in an oxygen-rich state (namely the oxygen content is relatively excessive), combustion-melting reaction mainly occurs in the system, and the heat released by full combustion of the gasification fly ash (carbon is fully combusted to generate CO)2) The temperature of the system can reach 1400-1600 ℃, and the ash contents of the incineration fly ash and the gasification fly ash are fully melted.
The invention has no special limit to the type of the gasification agent for providing the oxygen-containing atmosphere and the oxygen content, and can select a proper gasification agent according to the actual requirement, specifically air, pure oxygen or oxygen-enriched gas; the amount of the gasifying agent to be introduced is determined according to actual needs so as to ensure the above-mentioned gasification-melting reaction or combustion-melting reaction to proceed smoothly, and the present invention is not particularly limited thereto.
In the present invention, the gasification-melting reaction or the combustion-melting reaction may be specifically initiated by ignition, and the present invention is not particularly limited thereto.
In the invention, after the liquid slag is obtained, the liquid slag forms glassy state slag after the first cooling treatment. In the present invention, the first cooling treatment is preferably to cool the material to 100 ℃ or less. In the present invention, the mode used for the first cooling treatment is not particularly limited, and it is preferable to perform the cooling treatment on the liquid slag using water at normal temperature as a cooling medium. In the invention, the glassy slag can be used as a building material, and the full utilization of waste resources is realized.
According to the invention, after the mixed gas product is obtained, the mixed gas product is sequentially subjected to second cooling treatment, gas dedusting treatment and gas purification treatment to obtain purified combustible gas or purified flue gas, the purified combustible gas is collected for reuse, and the purified flue gas is discharged after reaching the standard. In the invention, the second cooling treatment is preferably to cool the material to 160 ℃ or less, and more preferably to 145-155 ℃. In the present invention, the mode used for the second cooling treatment is not particularly limited, and the requirement of the cooling temperature may be satisfied. The gas dedusting treatment is not particularly limited, and the technical scheme of the gas dedusting treatment known to those skilled in the art can be adopted. The gas purification treatment of the present invention is not particularly limited, and a method known to those skilled in the art may be used. In the invention, after gas purification treatment, the purified combustible gas is collected for reuse so as to realize the full utilization of resources; the obtained purified flue gas is discharged up to the standard, and the environment is not influenced.
The invention provides a device for co-processing incineration fly ash and gasification fly ash, which comprises a storage tank, a feeding bin and an entrained flow bed which are sequentially communicated, wherein the top of the entrained flow bed is connected with an ignition system and a primary air pipeline in parallel, the bottom of the entrained flow bed is provided with a slag discharging-cooling system, and an exhaust port of the entrained flow bed is sequentially communicated with a gas cooling system, a gas dedusting system and a gas purification system.
The device for co-processing the incineration fly ash and the gasification fly ash comprises a storage tank, a gasification device and a control device, wherein the storage tank is used for storing raw materials; the material, size and the like of the storage tank are not particularly limited.
As an embodiment of the present invention, when the incineration fly ash used is hazardous waste incineration fly ash or waste incineration fly ash, the storage tank includes an incineration fly ash storage tank and a gasification fly ash storage tank, and both the incineration fly ash storage tank and the gasification fly ash storage tank are communicated with the feed inlet of the feed bin. As an embodiment of the present invention, when the incineration fly ash used is hazardous waste incineration fly ash and waste incineration fly ash, the storage tanks include a hazardous waste incineration fly ash storage tank, a waste incineration fly ash storage tank and a gasification fly ash storage tank, and the hazardous waste incineration fly ash storage tank, the waste incineration fly ash storage tank and the gasification fly ash storage tank are all communicated with the feed inlet of the feed bin.
The device for co-processing the incineration fly ash and the gasification fly ash comprises a feeding bin, a material feeding bin and a material discharging bin, wherein the feeding bin is used for uniformly mixing raw materials from a storage tank and then conveying the raw materials to an entrained flow bed for gasification-melting reaction or combustion-melting reaction; the material, size and the like of the feeding bin are not specially limited. As an embodiment of the invention, the device for co-processing incineration fly ash and gasification fly ash also comprises a nitrogen making system, wherein one gas outlet of the nitrogen making system is communicated with the feeding bin, so that raw materials are conveyed from the feeding bin to the entrained flow bed through nitrogen.
The device for co-processing incineration fly ash and gasification fly ash provided by the invention comprises an entrained flow bed, wherein gasification-melting reaction or combustion-melting reaction occurs in the entrained flow bed; the entrained flow is preferably a steel, cylindrical reactor, the dimensions of which are not particularly limited by the present invention.
In the invention, the top of the entrained flow is provided with an ignition system and a primary air pipeline in parallel, which are respectively used for ignition and gasification agent introduction, so that the incineration fly ash and the gasification fly ash carry out gasification-melting reaction or combustion-melting reaction in the entrained flow.
As an embodiment of the invention, the ignition system is an ignition combustor and consists of an ignition oil gun, a high-energy igniter and a flame detection device; the ignition oil gun is an air pressure atomization type ignition oil gun, and fuel required by the ignition oil gun is 0# light diesel oil.
The primary air duct of the present invention is not particularly limited, and a primary air duct known to those skilled in the art may be used.
In the invention, the bottom of the entrained flow is provided with a slag discharging-cooling system for discharging liquid slag from the entrained flow and cooling the liquid slag into glassy slag.
As an embodiment of the present invention, the slag discharging-cooling system includes a slag discharging valve and a slag discharging tank, the slag discharging tank is connected with the entrained flow bed through the slag discharging valve, and a cooling medium in the slag discharging tank is water; the slag discharging valve can control the discharging rate and the discharging amount of the liquid slag, and if the liquid slag can be intermittently discharged to the slag discharging tank for cooling, the cooling effect is ensured, and the glassy state slag meeting the use requirement of building materials is formed.
In the invention, the exhaust port of the entrained flow is sequentially communicated with a gas cooling system, a gas dedusting system and a gas purification system so as to realize cooling, dedusting and purification of a mixed gas product.
As an embodiment of the present invention, the gas cooling system is a water cooler; the high-temperature mixed gas product discharged from the exhaust port of the entrained flow bed is cooled to be less than or equal to 160 ℃ after passing through a water cooler, and then enters a subsequent gas dust removal system.
As an embodiment of the invention, the gas dust removal system comprises a bag-type dust remover and an ash bucket, has a nitrogen back-blowing function, and is used for performing gas dust removal treatment on a cooled mixed gas product. As an embodiment of the invention, the other air outlet of the nitrogen making system is communicated with the gas dust removal system, so that nitrogen can be conveniently provided to realize the back flushing of the nitrogen.
As an embodiment of the invention, the gas purification system comprises a desulfurization tower or a washing tower, in particular, when the mixed gas product is combustible gas, the gas purification system adopts the desulfurization tower to remove sulfide in the combustible gas; when the mixed gas product is flue gas, the gas purification system adopts a washing tower which has a deacidification function and can remove NO in the flue gasxAnd SO2。
The method of using the apparatus for co-processing incineration fly ash and gasification fly ash of the present invention is described below with reference to fig. 1 to 4: gasified fly ash and incineration fly ash (including garbage incineration fly ash and/or hazardous waste incineration fly ash) enter a material inlet bin according to a certain proportion from respective storage tanks, then are conveyed to an entrained flow bed from the material inlet bin through nitrogen, gasification agent is introduced from a primary air pipe at the top of the entrained flow bed to provide oxygen-containing atmosphere for the entrained flow bed, and ignition is carried out through an ignition system arranged at the top of the entrained flow bed to initiate reaction, when the oxygen supply is insufficient, the gasified fly ash is gasified in the entrained flow bed, the temperature of a hearth of the entrained flow bed can reach 1350-1550 ℃, ash content of the gasified fly ash and the incineration fly ash are fully melted under the high temperature condition to form liquid slag, the liquid slag is discharged and cooled from a slag discharge-cooling system at the bottom of the entrained flow bed to form glassy slag which can be used as building materials, and simultaneously a certain amount of combustible gas is generated in the gasification process, and is discharged, The gas dust removal system and the gas purification system can be conveyed to a user for reuse after treatment; when the oxygen supply is excessive, the gasified fly ash is fully combusted in the hearth, the temperature of the hearth of the entrained flow bed can reach 1400-1600 ℃, the ash content of the gasified fly ash and the incineration fly ash are fully melted under the high-temperature condition to form liquid slag, the liquid slag is discharged from a slag discharge-cooling system at the bottom of the entrained flow bed and is cooled to form glassy slag which can be used as building materials, and a certain amount of flue gas is generated in the combustion process, is discharged from an exhaust port of the entrained flow bed, and is treated by a gas cooling system, a gas dedusting system and a gas purification system in sequence and then is discharged after reaching the standard.
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. 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.
The following examples used the following raw materials with the specific ingredients:
the average particle size of the waste incineration fly ash produced by a certain waste incineration plant is 40-60 μm, and the main chemical components and the heavy metal content are respectively shown in tables 1 and 2:
table 1 main component of refuse incineration fly ash (%)
| Fe2O3 | MgO | Na2O | SiO2 | CaO | K2O | Al2O3 | Cl | S |
| 1.14 | 1.23 | 2.88 | 8.16 | 29.11 | 2.97 | 2.80 | 18.21 | 0.97 |
TABLE 2 heavy metal content (ppm) in the fly ash from waste incineration
| Pb | Zn | Cu | Ni | Mn | Cr |
| 3039.8 | 22670.5 | 1480.1 | 181.7 | 76 | 609.6 |
The average particle size of the hazardous waste incineration fly ash generated by a hazardous waste incineration plant is 40-60 mu m, and the analysis of the main chemical components is shown in Table 3:
table 3 analysis of part of chemical composition in fly ash from incineration of hazardous wastes (%)
| Fly ash type | Na | Ca | K | Cl | S | Si | Al | Fe |
| Bag collector | 13.1 | 20.1 | 2.1 | 9.8 | 8.48 | 0.8 | 0.2 | 0.2 |
| Collecting by quenching | 1.4 | 36.9 | 0.1 | 3.3 | 1.0 | 0.3 | 0.3 | 0.2 |
The average particle size of gasification fly ash produced by a certain coal gasification plant is 30-50 μm, and the analysis of main chemical components is shown in tables 4-6:
TABLE 4 gasification fly ash Industrial analysis (air dry basis)
| Item | Unit of | Numerical value |
| Moisture content | ％ | 0.48 |
| Volatile component | ％ | 2.68 |
| Fixed carbon | ％ | 46.25 |
| Ash content | ％ | 50.59 |
TABLE 5 gasification fly ash elemental analysis (air dry basis)
| Item | Unit of | Numerical value |
| C | ％ | 47.86 |
| H | ％ | 0.43 |
| O | ％ | - |
| N | ％ | 0.44 |
| S | ％ | 0.52 |
TABLE 6 gasification fly ash major ash component
Example 1
The co-disposal of gasification fly ash and waste incineration fly ash using the apparatus shown in fig. 1 and according to the flow scheme shown in fig. 3 comprises the following steps:
inputting gasification fly ash and waste incineration fly ash into a feeding bin according to a certain proportion, wherein the adding amount of the waste incineration fly ash is 5% of the mass of the gasification fly ash, and the two materials are fully mixed in the feeding bin and then are conveyed to an entrained flow bed through nitrogen; introducing air from the primary air pipe at the top of the entrained flow bed (controlling the air introduction amount to make the entrained flow bed in oxygen-deficient state), igniting by the ignition system arranged at the top of the entrained flow bed, gasifying fly ash in the entrained flow bed, wherein the hearth temperature of the entrained flow bed is about 1350 ℃, and gasifying fly ash and waste incineration fly ash under the high temperature conditionThe ash is fully melted to form liquid slag, the liquid slag is discharged from a slag discharge-cooling system at the bottom of the entrained flow bed and is cooled to 100 ℃ with normal-temperature water to form glassy slag which can be used as building materials; the gasification process also produces a certain amount of combustible gas (with a calorific value of about 1780kCal/kg and combustible components including CO and H2) After being discharged from an exhaust port of the entrained flow bed, the gas is cooled to about 150 ℃ by a gas cooling system, and then is treated by a gas dedusting system and a gas purification system to obtain purified combustible gas which can be conveyed to a user for reuse.
Example 2
The device shown in figure 1 is used for co-processing gasified fly ash and hazardous waste incineration fly ash according to the flow shown in figure 4, and comprises the following steps:
the gasification fly ash and the waste incineration fly ash are input into a feed bin according to a certain proportion, the adding amount of the hazardous waste incineration fly ash is 50 percent of the mass of the gasification fly ash, and the two materials are fully mixed in the feed bin and then are conveyed to an entrained flow bed through nitrogen; introducing pure oxygen from a primary air pipe at the top of the entrained flow bed (controlling the introduction amount of the pure oxygen to enable the entrained flow bed to be in an oxygen-enriched state), igniting by an ignition system arranged at the top of the entrained flow bed, fully burning gasified fly ash in the entrained flow bed, wherein the temperature of a hearth of the entrained flow bed is about 1500 ℃, the ash content of the gasified fly ash and hazardous waste incineration fly ash are fully melted to form liquid slag under the high-temperature condition, and the liquid slag is discharged from a slag discharge-cooling system at the bottom of the entrained flow bed and is cooled to 100 ℃ with normal temperature water to form glassy slag which can be used as building materials; and simultaneously, a certain amount of flue gas is generated in the gasification process, and is cooled to about 150 ℃ by a gas cooling system after being discharged from an exhaust port of the entrained flow bed, and then is treated by a gas dust removal system and a gas purification system to obtain purified flue gas which reaches the standard and is discharged.
Example 3
The co-disposal of the gasification fly ash, the waste incineration fly ash and the hazardous waste incineration fly ash by using the device shown in FIG. 2 and referring to the flow chart shown in FIG. 4 comprises the following steps:
inputting gasification fly ash, waste incineration fly ash and hazardous waste incineration fly ash into a feeding bin according to a certain proportion, wherein the addition amount of the waste incineration fly ash is 30% of the mass of the gasification fly ash, the addition amount of the hazardous waste incineration fly ash is 20% of the mass of the gasification fly ash, and the three materials are fully mixed in the feeding bin and then are conveyed to an entrained flow bed through nitrogen; introducing pure oxygen from a primary air pipe at the top of the entrained flow bed (controlling the introduction amount of the pure oxygen to enable the entrained flow bed to be in an oxygen-enriched state), igniting by an ignition system arranged at the top of the entrained flow bed, fully burning the gasified fly ash in the entrained flow bed, wherein the temperature of a hearth of the entrained flow bed is about 1600 ℃, the fly ash of the gasified fly ash, the waste incineration fly ash and the hazardous waste incineration fly ash are fully melted under the high-temperature condition to form liquid slag, and the liquid slag is discharged from a slag discharge-cooling system at the bottom of the entrained flow bed and is cooled to 100 ℃ with normal temperature to form glassy slag which can be used as building materials; and simultaneously, a certain amount of flue gas is generated in the gasification process, and is cooled to about 150 ℃ by a gas cooling system after being discharged from an exhaust port of the entrained flow bed, and then is treated by a gas dust removal system and a gas purification system to obtain purified flue gas which reaches the standard and is discharged.
From the above embodiments, the method provided by the present invention has the following beneficial effects:
1) the gasified fly ash is gasified or combusted through the entrained flow bed, and finally formed glassy slag can be used as building materials, so that resource utilization is realized;
2) the particle size of the incineration fly ash is similar to that of the gasification fly ash, the ash content of the gasification fly ash and the incineration fly ash are melted by using the high temperature generated during gasification or combustion of the gasification fly ash, and the obtained liquid slag is cooled to form a glassy substance, so that harmless treatment is realized;
3) by using elements such as Na, K and the like in the incineration fly ash, the ash content of the gasification fly ash and the ash melting point of the incineration fly ash can be reduced, and the full melting of the gasification fly ash and the incineration fly ash is facilitated to form liquid slag;
3) the self heat value of the gasified fly ash is fully utilized in the gasification-melting and combustion-melting processes, no external energy source, additional auxiliary fuel and the like are needed, and the cost is reduced;
4) the system temperature can reach 1350-1600 ℃ in the gasification-melting and combustion-melting processes, so that the incineration of dioxin in the incineration fly ash is realized;
5) the combustible gas generated in the gasification-melting reaction process can be used as secondary energy;
6) when the incineration fly ash is treated by the conventional method, SiO is added into the incineration fly ash2The fluxing agent is beneficial to the formation of the molten slag vitreous body, and the viscosity of the vitreous body is reduced; because of SiO in the gasified fly ash2The content can reach 50%, and also contains Al2O3And the inorganic salt components such as CaO and the like are utilized, and the two fly ashes do not need to be additionally added in the melting process to form an auxiliary material with a glass component, so that the production cost is further reduced, and the method is suitable for large-scale production.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (10)
1. A method for co-processing incineration fly ash and gasification fly ash is characterized by comprising the following steps:
mixing incineration fly ash and gasification fly ash, and carrying out gasification-melting reaction or combustion-melting reaction in an oxygen-containing atmosphere to obtain liquid slag and a mixed gas product, wherein the mixed gas product is combustible gas or flue gas;
the liquid slag forms glassy state slag after first cooling treatment;
and the mixed gas product is subjected to secondary cooling treatment, gas dedusting treatment and gas purification treatment in sequence to obtain purified combustible gas or purified flue gas, the purified combustible gas is collected and recycled, and the purified flue gas is discharged up to the standard.
2. The method according to claim 1, wherein the fly ash incineration comprises waste fly ash and/or hazardous waste fly ash incineration.
3. The method according to claim 1 or 2, wherein the gasification-fusion reaction is carried out with incineration fly ash mass being 5-15% of gasification fly ash mass; and the mixed gas product obtained after the gasification-melting reaction is combustible gas.
4. The method according to claim 3, wherein the temperature of the system during the gasification-melting reaction is 1350-1550 ℃.
5. The method according to claim 1 or 2, wherein the combustion-melting reaction is performed with the mass of incineration fly ash being 20 to 50% of the mass of gasification fly ash; and the mixed gas product obtained after the combustion-melting reaction is flue gas.
6. The method according to claim 5, wherein the temperature of the system during the combustion-melting reaction is 1400-1600 ℃.
7. The method according to claim 4 or 6, characterized in that the first cooling treatment is cooling the material to 100 ℃ or less; the second cooling treatment is to cool the materials to be less than or equal to 160 ℃.
8. The device for co-processing the incineration fly ash and the gasification fly ash is characterized by comprising a storage tank, a feeding bin and an entrained flow bed which are sequentially communicated, wherein the top of the entrained flow bed is connected with an ignition system and a primary air pipeline in parallel, the bottom of the entrained flow bed is provided with a slag discharging-cooling system, and an exhaust port of the entrained flow bed is sequentially communicated with a gas cooling system, a gas dedusting system and a gas purification system.
9. The apparatus of claim 8, further comprising a nitrogen generation system, wherein two gas outlets of the nitrogen generation system are respectively communicated with the feed bin and the gas dust removal system.
10. The apparatus of claim 8 or 9, wherein the slag tapping-cooling system comprises a slag tapping valve and a slag tapping tank, the slag tapping tank is connected with the entrained flow bed through the slag tapping valve, and the cooling medium in the slag tapping tank is water.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113280345A (en) * | 2021-06-25 | 2021-08-20 | 中国科学院山西煤炭化学研究所 | Method for generating electricity by coupling high-temperature melting and harmless treatment of waste fly ash with incineration |
| CN113549472A (en) * | 2021-08-31 | 2021-10-26 | 宁夏大学 | Novel process and device for treating miscellaneous salt |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113280345A (en) * | 2021-06-25 | 2021-08-20 | 中国科学院山西煤炭化学研究所 | Method for generating electricity by coupling high-temperature melting and harmless treatment of waste fly ash with incineration |
| CN113280345B (en) * | 2021-06-25 | 2022-09-09 | 中国科学院山西煤炭化学研究所 | Method for generating electricity by coupling high-temperature melting and harmless treatment of waste fly ash with incineration |
| CN113549472A (en) * | 2021-08-31 | 2021-10-26 | 宁夏大学 | Novel process and device for treating miscellaneous salt |
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