Method and device for co-disposing incineration fly ash and gasification fly ash

Abstract

The present invention provides a method and device for co-disposing incineration fly ash and gasification fly ash, belonging to the technical field of fly ash disposal. In the present invention, incineration fly ash and gasification fly ash are mixed and undergo a gasification-melting reaction or a combustion-melting reaction in an oxygen-containing atmosphere to obtain a liquid slag and a mixed gas product, and the mixed gas product is combustible gas or flue gas; the liquid slag forms a vitreous slag after the first cooling treatment; the mixed gas product is successively subjected to a second cooling treatment, a gas dust removal treatment and a 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 up to standard. The method provided by the present invention utilizes the self-heat value of the gasification fly ash during the gasification or combustion process without adding additional auxiliary fuel; and utilizes the self-inorganic salt components in the two fly ashes, and no additional auxiliary materials are required to make the ash of the gasification fly ash and the incineration fly ash form glass components during the melting process, with low production cost and being suitable for large-scale production.

Description

Technical Field

[0001] The present invention relates to the technical field of fly ash disposal, and particularly relates to a method and device for co-disposing incineration fly ash and gasification fly ash. Background Art

[0002] Incineration fly ash includes municipal solid waste incineration fly ash and hazardous waste incineration fly ash. Since these two types of fly ash are enriched with various heavy metals and dioxin-like pollutants, they are listed in the "National Hazardous Waste List" in 2016 and belong to hazardous waste (HW18).

[0003] Municipal solid waste incineration fly ash is the residue collected from the flue gas purification system of municipal solid waste incineration plants. The production volume of municipal solid waste incineration fly ash is huge, which is one of the key points and difficulties in the management of hazardous waste in China. At present, there are more than 300 municipal solid waste incineration plants in China, with an annual incineration treatment capacity reaching 70 million tons. The production of municipal solid waste incineration fly ash is related to the types of waste, incineration conditions, incinerator types, and flue gas treatment processes. Calculated according to the fly ash production ratio of 5-8%, 3.5-5.6 million tons of municipal solid waste incineration fly ash are produced annually. Municipal solid waste incineration fly ash is dark gray or grayish white, with an average particle size generally of 40-60 μm. The content of soluble salts mainly composed of chlorides of K, Na, and Ca is 15-25%, and it contains various heavy metals and harmful substances such as dioxins.

[0004] Hazardous waste incineration fly ash is the residue collected from the flue gas purification system of hazardous waste incineration plants. The production volume of hazardous waste incineration fly ash is large and its harmfulness is strong, which is also one of the key points and difficulties in the management of hazardous waste in China. In 2018, the incineration disposal volume of hazardous waste in China was 4 million tons. Calculated according to the fly ash production ratio of 5-10%, the production volume of hazardous waste incineration fly ash is 200,000-400,000 tons. Hazardous waste incineration fly ash and municipal solid waste incineration fly ash also have the characteristics of low moisture content, irregular shape, high porosity, small particle size (average particle size generally of 40-60 μm), and large specific surface area, and the main components are Na, Ca, K, Cl, S, Si, etc.

[0005] At present, the main treatment method for incineration fly ash is safe landfill after stabilization and solidification. However, due to the limited capacity of landfills and the need to improve the solidification method, for example, when using chelating agents to solidify incineration fly ash, the stability of chelating agents needs to be improved. Based on this, experts and scholars have actively studied and developed harmless and resource-based treatment methods for incineration fly ash. The most representative one is the fly ash high-temperature melting vitrification technology. This technology can stably solidify heavy metals in incineration fly ash through heat treatment processes such as electric and fuel melting vitrification. However, to achieve the melting of incineration fly ash, a large amount of energy is required; in addition, to reduce the ash melting point and facilitate the formation of glass bodies, a certain amount of Ca, Al, and Si inorganic salts need to be added additionally during the melting process, increasing the material consumption. Therefore, this technology requires a large amount of energy and has a high treatment cost.

[0006] In recent years, coal gasification technology has played an extremely important role in China's economic development. However, during the gasification process, some unreacted carbon and fine slag will be carried out by the syngas, generating a certain amount of gasification fly ash. The preliminary estimate of the annual output is 500,000 - 1,000,000 tons. The calorific value of the gasification fly ash is 2,500 - 4,000 kCal / kg, and the average particle size is 30 - 50 μm. Currently, the gasification fly ash is usually used in road engineering, mine backfilling or soil improvement, resulting in the calorific value of the gasification fly ash and the unburned carbon it contains not being directly utilized, causing waste of resources. Summary of the Invention

[0007] The purpose of the present invention is to provide a method and device for co-disposing incineration fly ash and gasification fly ash. The method provided by the present invention can achieve harmless treatment and resource utilization of incineration fly ash and gasification fly ash, and does not require the use of additional auxiliary materials, with low production costs and being suitable for large-scale production.

[0008] In order to achieve the above-mentioned invention purpose, the present invention provides the following technical solutions:

[0009] The present invention provides a method for co-disposing incineration fly ash and gasification fly ash, including the following steps:

[0010] Mix the incineration fly ash and gasification fly ash, and carry out a gasification-melting reaction or a combustion-melting reaction in an oxygen-containing atmosphere to obtain a liquid slag and a mixed gas product, and the mixed gas product is combustible gas or flue gas;

[0011] The liquid slag forms a vitreous slag after the first cooling treatment;

[0012] The mixed gas product is sequentially subjected to a second cooling treatment, a gas dust removal treatment and a gas purification treatment to obtain purified combustible gas or purified flue gas, collect the purified combustible gas for reuse, and the purified flue gas is discharged up to standard.

[0013] Preferably, the incineration fly ash includes waste incineration fly ash and / or hazardous waste incineration fly ash.

[0014] Preferably, when carrying out the gasification-melting reaction, the mass of the incineration fly ash is 5 - 15% of the mass of the gasification fly ash; the mixed gas product obtained after the gasification-melting reaction is combustible gas.

[0015] Preferably, the temperature of the system during the gasification-melting reaction is 1,350 - 1,550 °C.

[0016] Preferably, when carrying out the combustion-melting reaction, the mass of the incineration fly ash is 20 - 50% of the mass of the gasification fly ash; the mixed gas product obtained after the combustion-melting reaction is flue gas.

[0017] Preferably, the temperature of the system during the combustion-melting reaction is 1,400 - 1,600 °C.

[0018] Preferably, the first cooling treatment is to cool the material to ≤100°C; the second cooling treatment is to cool the material to ≤160°C.

[0019] The present invention provides a device for co-disposing incineration fly ash and gasification fly ash, which includes a storage tank, a feed bin, and a entrained flow bed connected in sequence. The top of the entrained flow bed is provided with an ignition system and a primary air duct in parallel. The bottom of the entrained flow bed is provided with a slag discharge-cooling system. The exhaust port of the entrained flow bed is connected to a gas cooling system, a gas dust removal system, and a gas purification system in sequence.

[0020] Preferably, it further includes a nitrogen generation system, and two air outlets of the nitrogen generation system are respectively connected to the feed bin and the gas dust removal system.

[0021] Preferably, the slag discharge-cooling system includes a slag discharge valve and a slag discharge tank. The slag discharge tank is connected to the entrained flow bed through the slag discharge valve, and the cooling medium in the slag discharge tank is water.

[0022] The present invention provides a method for co-disposing incineration fly ash and gasification fly ash, which includes the following steps: mixing incineration fly ash and gasification fly ash, and carrying out a gasification-melting reaction or a combustion-melting reaction in an oxygen-containing atmosphere to obtain a liquid slag and a mixed gas product. The mixed gas product is combustible gas or flue gas; the liquid slag forms a vitreous slag after the first cooling treatment; the mixed gas product is sequentially subjected to a second cooling treatment, a gas dust removal treatment, and a 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 up to standard. The present invention co-disposes incineration fly ash and gasification fly ash. In an oxygen-containing atmosphere, using the high temperature generated by the gasification or combustion of gasification fly ash, the ash of gasification fly ash and incineration fly ash are melted together, and after cooling, a vitreous slag is formed, which can be used as building materials, realizing harmless treatment and resource utilization. Therefore, the method provided by the present invention utilizes the self-heat value of gasification fly ash during the gasification or combustion process without adding auxiliary fuel; and utilizes the self-inorganic salt components (CaO, SiO2, Al2O3) in the two fly ashes, and no additional auxiliary materials are required to form a glass component during the melting process, resulting in low production costs and being suitable for large-scale production.

[0023] The present invention provides a device for co-disposing incineration fly ash and gasification fly ash, which includes a storage tank, a feed bin, and a entrained flow bed connected in sequence. The top of the entrained flow bed is provided with an ignition system and a primary air duct in parallel. The bottom of the entrained flow bed is provided with a slag discharge-cooling system. The exhaust port of the entrained flow bed is connected to a gas cooling system, a gas dust removal system, and a gas purification system in sequence. The device provided by the present invention has a reasonable structure, does not require special or expensive components, is easy to operate, and can realize the co-disposal of incineration fly ash and gasification fly ash. Description of the Drawings

[0024] Figure 1 It is a schematic structural diagram of the device for co-disposing incineration fly ash and gasification fly ash in the present invention;

[0025] Figure 2 It is another schematic structural diagram of the device for co-disposing incineration fly ash and gasification fly ash in the present invention;

[0026] Figure 3 It is a process flow diagram of the gasification-melting process when co-disposing incineration fly ash and gasification fly ash in the present invention;

[0027] Figure 4 It is a process flow diagram of the combustion-melting process when co-disposing incineration fly ash and gasification fly ash in the present invention;

[0028] In the figure, 1-1 is an incineration fly ash storage tank, 1-1-1 is a municipal solid 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 feed bin, 3 is a entrained flow bed, 4 is an ignition system, 5 is a primary air duct, 6 is a slag discharge-cooling system, 7 is a gas cooling system, 8 is a gas dust removal system, 9 is a gas purification system, 10 is a nitrogen production system. Detailed Description of the Invention

[0029] The present invention provides a method for co-disposing incineration fly ash and gasification fly ash, comprising the following steps:

[0030] Mix the incineration fly ash and the gasification fly ash, and carry out a gasification-melting reaction or a combustion-melting reaction in an oxygen-containing atmosphere to obtain a liquid slag and a mixed gas product, wherein the mixed gas product is combustible gas or flue gas;

[0031] The liquid slag forms a vitreous slag after the first cooling treatment;

[0032] The mixed gas product is successively subjected to a second cooling treatment, a gas dust removal treatment and a gas purification treatment to obtain purified combustible gas or purified flue gas, collect the purified combustible gas for reuse, and discharge the purified flue gas up to the standard.

[0033] In the present invention, the incineration fly ash and the gasification fly ash are mixed, and a gasification-melting reaction or a combustion-melting reaction occurs in an oxygen-containing atmosphere to obtain a liquid slag and a mixed gas product, wherein the mixed gas product is combustible gas or flue gas. In the present invention, after the incineration fly ash and the gasification fly ash are mixed, ignition is carried out in an oxygen-containing atmosphere, and the carbon contained in the gasification fly ash undergoes a gasification reaction or sufficient combustion under the action of oxygen, and the corresponding mixed gas product obtained is combustible gas (with a calorific value of 1500-2000 kCal / kg, and the combustible components contained include CO and H2) or flue gas, and at the same time, a large amount of heat is released, which can cause the ash components of the incineration fly ash and the gasification fly ash to be fully melted to form a liquid slag.

[0034] 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 the residue collected from the flue gas purification system of a domestic waste incineration plant, and the hazardous waste incineration fly ash specifically refers to the residue collected from the flue gas purification system of a hazardous waste incineration plant. The present invention has no special limitation on the specific sources of the waste incineration fly ash and the hazardous waste incineration fly ash, and any source is acceptable. In the present invention, the average particle size of the incineration fly ash is preferably 40 - 60 μm.

[0035] In the present invention, the gasification fly ash specifically refers to the fly ash formed by unreacted carbon and fine slag being carried out by syngas during the coal gasification process, and the average particle size is preferably 30 - 50 μm; the present invention has no special limitation on the specific source of the gasification fly ash, and any source is acceptable.

[0036] In the present invention, the ratio of the incineration fly ash to the gasification fly ash and the oxygen consumption will affect the chemical reaction process occurring in the system after ignition. Specifically: when the mass of the incineration fly ash is 5 - 15% of the mass of the gasification fly ash, when the system is in an oxygen-deficient state (i.e., the oxygen content is relatively insufficient), the main reaction occurring in the system is the gasification-melting reaction. By using the heat released by the gasification of the gasification fly ash (carbon generates CO through the gasification reaction), the temperature of the system can reach 1350 - 1550 °C, and the ash of the incineration fly ash and the gasification fly ash is fully melted; when the mass of the incineration fly ash is 20 - 50% of the mass of the gasification fly ash, when the system is in an oxygen-rich state (i.e., the oxygen content is relatively excessive), the main reaction occurring in the system is the combustion-melting reaction. By using the heat released by the full combustion of the gasification fly ash (carbon generates CO2 through full combustion), the temperature of the system can reach 1400 - 1600 °C, and the ash of the incineration fly ash and the gasification fly ash is fully melted.

[0037] The present invention has no special limitation on the type of the gasifying agent providing the oxygen-containing atmosphere and the oxygen content. It is only necessary to select a suitable gasifying agent according to actual needs. Specifically, it can be air, pure oxygen or oxygen-rich gas. The present invention has no special limitation on the oxygen-rich gas, and the oxygen-rich gas well-known to those skilled in the art can be used; the feeding amount of the gasifying agent is determined according to actual needs, and it is advisable to ensure the smooth progress of the above gasification-melting reaction or combustion-melting reaction. The present invention does not make a special limitation on this.

[0038] In the present invention, the gasification-melting reaction or combustion-melting reaction can specifically be initiated by ignition, and the present invention does not make a special limitation on this.

[0039] In the present invention, after obtaining the molten slag, the molten slag is subjected to a first cooling treatment to form a vitreous slag. In the present invention, the first cooling treatment preferably cools the material to ≤100 °C. The present invention has no special limitation on the manner of the first cooling treatment, and preferably uses water at normal temperature as the cooling medium to cool the molten slag. In the present invention, the vitreous slag can be used as a building material, realizing the full utilization of waste resources.

[0040] In the present invention, after obtaining the mixed gas product, the mixed gas product is successively subjected to a second cooling treatment, a gas dust removal treatment and a gas purification treatment to obtain purified combustible gas or purified flue gas. The purified combustible gas is collected and reused, and the purified flue gas is discharged up to the standard. In the present invention, the second cooling treatment preferably cools the material to ≤160 °C, and more preferably cools it to 145 - 155 °C. The present invention has no special limitation on the manner of the second cooling treatment, and it is only necessary to meet the above cooling temperature requirements. The present invention has no special limitation on the gas dust removal treatment, and a gas dust removal treatment technical solution well-known to those skilled in the art can be adopted. The present invention has no special limitation on the gas purification treatment, and a method well-known to those skilled in the art can be adopted. In the present invention, after the gas purification treatment, the obtained purified combustible gas is collected and reused to realize the full utilization of resources; the obtained purified flue gas is discharged up to the standard and will not cause an impact on the environment.

[0041] The present invention provides a device for co-disposing incineration fly ash and gasification fly ash, including a storage tank, a feed bin and a entrained flow bed connected in sequence. A ignition system and a primary air duct are arranged in parallel at the top of the entrained flow bed. A slag discharge-cooling system is arranged at the bottom of the entrained flow bed. The exhaust port of the entrained flow bed is successively connected with a gas cooling system, a gas dust removal system and a gas purification system.

[0042] The device for co-disposing incineration fly ash and gasification fly ash provided by the present invention includes a storage tank for storing raw materials; the present invention has no special limitation on the material, size, etc. of the storage tank.

[0043] As an embodiment of the present invention, when the incineration fly ash used is hazardous waste incineration fly ash or municipal solid 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 connected to the feed port of the feed bin. As an embodiment of the present invention, when the incineration fly ash used is hazardous waste incineration fly ash and municipal solid waste incineration fly ash, the storage tank includes a hazardous waste incineration fly ash storage tank, a municipal solid waste incineration fly ash storage tank and a gasification fly ash storage tank, and the hazardous waste incineration fly ash storage tank, the municipal solid waste incineration fly ash storage tank and the gasification fly ash storage tank are all connected to the feed port of the feed bin.

[0044] The device for co-disposing incineration fly ash and gasification fly ash provided by the present invention includes a feed bin, which is used to evenly mix the raw materials from the storage tank and then transport them to the entrained flow bed for gasification-melting reaction or combustion-melting reaction; the present invention does not make special limitations on the material, size, etc. of the feed bin. As an embodiment of the present invention, the device for co-disposing incineration fly ash and gasification fly ash further includes a nitrogen generation system, and an air outlet of the nitrogen generation system is communicated with the feed bin, so as to facilitate the transportation of the raw materials from the feed bin to the entrained flow bed through nitrogen.

[0045] The device for co-disposing incineration fly ash and gasification fly ash provided by the present invention includes an entrained flow bed, in which a gasification-melting reaction or a combustion-melting reaction occurs; the entrained flow bed is preferably a steel-made, cylindrical reactor, and the present invention does not make special limitations on its size.

[0046] In the present invention, an ignition system and a primary air duct are arranged in parallel at the top of the entrained flow bed, which are respectively used for ignition and introducing a gasifying agent, so that the incineration fly ash and the gasification fly ash carry out a gasification-melting reaction or a combustion-melting reaction in the entrained flow bed.

[0047] As an embodiment of the present invention, the ignition system is an ignition burner, which is composed of an ignition oil gun, a high-energy igniter and a flame detection device; wherein, the ignition oil gun is an air pressure atomizing ignition oil gun, and the fuel required for the ignition oil gun is 0# light diesel.

[0048] The present invention does not have special limitations on the primary air duct, and a primary air duct well-known to those skilled in the art can be adopted.

[0049] In the present invention, a slag discharge-cooling system is arranged at the bottom of the entrained flow bed, which is used to discharge the liquid slag from the entrained flow bed and cool it to form vitreous slag.

[0050] As an embodiment of the present invention, the slag discharge-cooling system includes a slag discharge valve and a slag discharge tank. The slag discharge tank is connected to the entrained flow bed through the slag discharge valve, and the cooling medium in the slag discharge tank is water; wherein, the slag discharge valve can control the discharge rate and discharge amount of the liquid slag. For example, the liquid slag can be intermittently discharged into the slag discharge tank for cooling to ensure the cooling effect and form vitreous slag meeting the requirements for building materials use.

[0051] In the present invention, an exhaust port of the entrained flow bed is successively communicated with a gas cooling system, a gas dust removal system and a gas purification system to realize the cooling, dust removal and purification of the mixed gas product.

[0052] As an embodiment of the present invention, the gas cooling system is a water cooler; after the high-temperature mixed gas product discharged from the exhaust port of the entrained flow bed passes through the water cooler, the temperature drops to ≤160 °C, and then it enters the subsequent gas dust removal system.

[0053] As an embodiment of the present invention, the gas dust removal system includes a bag filter and a hopper, and has a nitrogen backwashing function for gas dust removal treatment of the cooled mixed gas product. As an embodiment of the present invention, another air outlet of the nitrogen generation system is connected to the gas dust removal system to facilitate the provision of nitrogen for nitrogen backwashing.

[0054] As an embodiment of the present invention, the gas purification system includes a desulfurization tower or a scrubber. Specifically, when the mixed gas product is combustible gas, the gas purification system uses a desulfurization tower to remove sulfides in the combustible gas; when the mixed gas product is flue gas, the gas purification system uses a scrubber, which has an acid removal function and can remove NO x and SO2.

[0055] The following will combine Figures 1 to 4 to illustrate the usage method of the device for co-disposing incineration fly ash and gasification fly ash in the present invention: Gasification fly ash and incineration fly ash (including municipal solid waste incineration fly ash and / or hazardous waste incineration fly ash) enter the feed bin in a certain proportion from their respective storage tanks, and then are transported to the entrained flow bed by nitrogen from the feed bin. The gasifying agent is introduced into the entrained flow bed through the primary air pipe at the top of the entrained flow bed to provide an oxygen-containing atmosphere for the entrained flow bed, and the reaction is initiated by ignition through the ignition system provided at the top of the entrained flow bed. When the oxygen supply is insufficient, the gasification fly ash undergoes gasification in the entrained flow bed. At this time, the furnace temperature of the entrained flow bed can reach 1350 - 1550 °C. Under this high-temperature condition, the ash of the gasification fly ash and the incineration fly ash are fully melted to form a liquid slag. The liquid slag is discharged and cooled from the slag discharge-cooling system at the bottom of the entrained flow bed to form a vitreous slag, which can be used as building materials. At the same time, a certain amount of combustible gas is generated during the gasification process. After being discharged from the exhaust port of the entrained flow bed, it is sequentially processed by the gas cooling system, the gas dust removal system, and the gas purification system and then can be transported to users for reuse; when the oxygen supply is excessive, the gasification fly ash burns fully in the furnace. At this time, the furnace temperature of the entrained flow bed can reach 1400 - 1600 °C. Under this high-temperature condition, the ash of the gasification fly ash and the incineration fly ash are fully melted to form a liquid slag. The liquid slag is discharged and cooled from the slag discharge-cooling system at the bottom of the entrained flow bed to form a vitreous slag, which can be used as building materials. At the same time, a certain amount of flue gas is generated during the combustion process. After being discharged from the exhaust port of the entrained flow bed, it is sequentially processed by the gas cooling system, the gas dust removal system, and the gas purification system and then discharged up to standard.

[0056] The following will clearly and completely describe the technical solutions in the present invention in combination with the embodiments in the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all of the embodiments. Based on the embodiments in the present invention, all other embodiments obtained by those of ordinary skill in the art without making creative efforts fall within the scope of protection of the present invention.

[0057] The specific components of the raw materials used in the following examples are as follows:

[0058] The fly ash from a waste incineration plant has an average particle size of 40 - 60 μm. The main chemical components and heavy metal contents are shown in Table 1 and Table 2 respectively:

[0059] Table 1 Main components of fly ash from waste incineration (%)

[0060] <![CDATA[Fe2O3]]> MgO <![CDATA[Na2O]]> <![CDATA[SiO2]]> CaO <![CDATA[K2O]]> <![CDATA[Al2O3]]> Cl S 1.14 1.23 2.88 8.16 29.11 2.97 2.80 18.21 0.97

[0061] Table 2 Heavy metal contents in fly ash from waste incineration (ppm)

[0062] Pb Zn Cu Ni Mn Cr 3039.8 22670.5 1480.1 181.7 76 609.6

[0063] The fly ash from a hazardous waste incineration plant has an average particle size of 40 - 60 μm. The analysis of main chemical components is shown in Table 3:

[0064] Table 3 Analysis of partial chemical components in fly ash from hazardous waste incineration (%)

[0065] Fly ash type Na Ca K Cl S Si Al Fe Fabric collection 13.1 20.1 2.1 9.8 8.48 0.8 0.2 0.2 Quench collection 1.4 36.9 0.1 3.3 1.0 0.3 0.3 0.2

[0066] The gasification fly ash produced by a coal gasification plant has an average particle size of 30 - 50 μm. The analysis of main chemical components is shown in Tables 4 - 6:

[0067] Table 4 Proximate analysis of gasification fly ash (air - dried basis)

[0068] Project Unit Value Moisture content ％ 0.48 Volatile matter ％ 2.68 Fixed carbon ％ 46.25 Ash content ％ 50.59

[0069] Table 5 Ultimate analysis of gasification fly ash (air - dried basis)

[0070] Project Unit Value C ％ 47.86 H ％ 0.43 O ％ - N ％ 0.44 S ％ 0.52

[0071] Table 6 Main ash components of gasification fly ash

[0072]

[0073]

[0074] Example 1

[0075] Using Figure 1 the device shown and according to Figure 3 the process shown to co - dispose of gasification fly ash and fly ash from waste incineration, including the following steps:

[0076] The gasified fly ash and the waste incineration fly ash are input into the feed bin at a certain ratio. The addition amount of the waste incineration fly ash is 5% of the mass of the gasified fly ash. After the two materials are fully mixed in the feed bin, they are transported to the entrained flow bed by nitrogen; air is introduced 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 an oxygen-deficient state), and ignition is carried out through the ignition system arranged at the top of the entrained flow bed. The gasified fly ash undergoes gasification in the entrained flow bed. At this time, the furnace temperature of the entrained flow bed is about 1350°C. Under this high-temperature condition, the ash of the gasified fly ash and the waste incineration fly ash are fully melted to form a liquid slag. The liquid slag is discharged from the slag discharge-cooling system at the bottom of the entrained flow bed and is cooled to 100°C by normal temperature water to form a vitreous slag, which can be used as building materials; at the same time, a certain amount of combustible gas (with a calorific value of about 1780 kCal / kg, and the combustible components including CO and H2) is generated during the gasification process. After being discharged from the exhaust port of the entrained flow bed, it is cooled to about 150°C by the gas cooling system, and then purified combustible gas is obtained after being treated by the gas dust removal system and the gas purification system, which can be transported to users for reuse.

[0077] Example 2

[0078] Utilize Figure 1 the device shown and according to Figure 4 the process shown to co-dispose the gasified fly ash and the hazardous waste incineration fly ash, including the following steps:

[0079] The gasified fly ash and the waste incineration fly ash are input into the feed bin at a certain ratio. The addition amount of the hazardous waste incineration fly ash is 50% of the mass of the gasified fly ash. After the two materials are fully mixed in the feed bin, they are transported to the entrained flow bed by nitrogen; pure oxygen is introduced from the primary air pipe at the top of the entrained flow bed (controlling the pure oxygen introduction amount to make the entrained flow bed in an oxygen-rich state), and ignition is carried out through the ignition system arranged at the top of the entrained flow bed. The gasified fly ash burns fully in the entrained flow bed. At this time, the furnace temperature of the entrained flow bed is about 1500°C. Under this high-temperature condition, the ash of the gasified fly ash and the hazardous waste incineration fly ash are fully melted to form a liquid slag. The liquid slag is discharged from the slag discharge-cooling system at the bottom of the entrained flow bed and is cooled to 100°C by normal temperature water to form a vitreous slag, which can be used as building materials; at the same time, a certain amount of flue gas is generated during the gasification process. After being discharged from the exhaust port of the entrained flow bed, it is cooled to about 150°C by the gas cooling system, and then purified flue gas is obtained after being treated by the gas dust removal system and the gas purification system, and is discharged up to standard.

[0080] Example 3

[0081] Utilize Figure 2 the device shown and refer to Figure 4 the process shown to co-dispose the gasified fly ash, the waste incineration fly ash and the hazardous waste incineration fly ash, including the following steps:

[0082] The gasified fly ash, municipal solid waste incineration fly ash, and hazardous waste incineration fly ash are fed into the feed bin in a certain proportion. The addition amount of municipal solid waste incineration fly ash is 30% of the mass of the gasified fly ash, and the addition amount of hazardous waste incineration fly ash is 20% of the mass of the gasified fly ash. After the three materials are fully mixed in the feed bin, they are transported to the entrained flow bed by nitrogen; pure oxygen is introduced from the primary air pipe at the top of the entrained flow bed (the introduction amount of pure oxygen is controlled to make the entrained flow bed in an oxygen-rich state), and ignition is carried out through the ignition system set at the top of the entrained flow bed. The gasified fly ash burns fully in the entrained flow bed. At this time, the furnace temperature of the entrained flow bed is about 1600 °C. Under this high-temperature condition, the fly ash of the gasified fly ash, municipal solid waste incineration fly ash, and hazardous waste incineration fly ash are fully melted to form a liquid slag. The liquid slag is discharged from the slag discharge-cooling system at the bottom of the entrained flow bed and cooled to 100 °C by normal temperature water to form a vitreous slag, which can be used as building materials; at the same time, a certain amount of flue gas is also generated during the gasification process. After being discharged from the exhaust port of the entrained flow bed, it is cooled to about 150 °C by the gas cooling system, and then the purified flue gas is obtained after being treated by the gas dust removal system and the gas purification system and is discharged up to standard.

[0083] As can be seen from the above embodiments, the method provided by the present invention has the following beneficial effects:

[0084] 1) The gasified fly ash is gasified or burned through the entrained flow bed, and the finally formed vitreous slag can be used as building materials, realizing resource utilization;

[0085] 2) The particle sizes of the incineration fly ash and the gasified fly ash are similar. The ash of the gasified fly ash and the incineration fly ash are melted by the high temperature generated during the gasification or combustion of the gasified fly ash, and the liquid slag obtained is cooled to form a vitreous substance, realizing harmless treatment;

[0086] 3) By using elements such as Na and K in the incineration fly ash, the ash melting point of the gasified fly ash and the incineration fly ash can be reduced, which is beneficial to their full melting to form a liquid slag;

[0087] 3) The self-heat value of the gasified fly ash is fully utilized during the gasification-melting and combustion-melting processes, without the need for external energy and additional auxiliary fuels, etc., which is beneficial to reducing costs;

[0088] 4) The system temperature during the gasification-melting and combustion-melting processes can reach 1350-1600 °C, realizing the destruction of dioxins in the incineration fly ash;

[0089] 5) The combustible gas generated during the gasification-melting reaction process can be used as secondary energy;

[0090] 6) When treating incineration fly ash by conventional methods, adding fluxes such as SiO2 to the incineration fly ash is beneficial to the formation of its molten slag glass body and reduces the viscosity of the glass body. Since the SiO2 content in gasification fly ash can reach 50%, and it also contains inorganic salt components such as Al2O3 and CaO, the present invention utilizes the inorganic salt components in the two fly ashes themselves, and no additional auxiliary materials for forming glass components need to be added during the melting process, which is beneficial to further reducing production costs and is suitable for large-scale production.

[0091] The above are only the preferred embodiments of the present invention. It should be noted that for those of ordinary skill in the art, without departing from the principle of the present invention, several improvements and refinements can be made, and these improvements and refinements should also be regarded as the protection scope of the present invention.

Claims

1. A method for co-disposing incineration fly ash and gasification fly ash, characterized in that It includes the following steps: Mix the incineration fly ash and the gasification fly ash, and carry out a gasification-melting reaction or a combustion-melting reaction in an oxygen-containing atmosphere to obtain a liquid slag and a mixed gas product, where the mixed gas product is combustible gas or flue gas; The liquid slag forms a vitreous slag after the first cooling treatment; The mixed gas product is successively subjected to a second cooling treatment, a gas dust removal treatment and a gas purification treatment to obtain purified combustible gas or purified flue gas. Collect the purified combustible gas for reuse, and discharge the purified flue gas up to the standard; When carrying out the gasification-melting reaction, the mass of the incineration fly ash is 5-15% of the mass of the gasification fly ash; the mixed gas product obtained after the gasification-melting reaction is combustible gas; the temperature of the system during the gasification-melting reaction is 1350-1550 °C; When carrying out the combustion-melting reaction, the mass of the incineration fly ash is 20-50% of the mass of the gasification fly ash; the mixed gas product obtained after the combustion-melting reaction is flue gas; the temperature of the system during the combustion-melting reaction is 1400-1600 °C.

2. The method according to claim 1, characterized in that, The incineration fly ash includes waste incineration fly ash and / or hazardous waste incineration fly ash.

3. The method according to claim 1, wherein The first cooling treatment is to cool the material to ≤100 °C; the second cooling treatment is to cool the material to ≤160 °C.

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