Multi-source solid waste collaborative incineration treatment method and system

Abstract

The invention provides a multi-source solid waste collaborative incineration treatment method and system, and belongs to the technical field of multi-source solid waste collaborative treatment. The multi-source solid waste collaborative incineration treatment method comprises the steps that water-containing gasified fly ash and a sludge conditioning agent are fed into an inner tank body of an integrated stirring device to be mixed, an obtained wall breaking agent overflows from the inner tank body and flows into an outer tank body of the integrated stirring device to be mixed with sludge entering the outer tank body, and a mixed material is obtained, the main components of the water-containing gasified fly ash comprise water, coal ash and part of unconverted carbon; dehydrating the mixed material by using a high-pressure mechanical filter pressing device to obtain a dehydrated material; and the dehydrated material is conveyed into a circulating fluidized bed incinerator of the circulating fluidized bed device, carbon contained in the water-containing gasified fly ash is used as fuel to achieve incineration of the sludge and the water-containing gasified fly ash, and slag and a gas-solid mixed material are generated. According to the invention, stable combustion and resource utilization of the low-calorific-value fuel are realized.

Description

Technical Field

[0001] The present invention relates to the field of co - processing of multi - source solid wastes, and particularly to a method and a system for co - incineration treatment of multi - source solid wastes. Background Art

[0002] In the process of sewage treatment, a large amount of sludge is generated. If not treated in time, it will cause pollution and harm to the environment. Therefore, the treatment of sludge has become an important issue in urban environmental management. For ordinary municipal solid waste sludge, dry - out incineration treatment is one of the relatively mature treatment methods at present. This technology mainly reduces the moisture content in the sludge through drying and heat treatment, and then sends it into an incinerator for incineration to achieve the harmlessness and reduction of the sludge. However, due to the high moisture content of the sludge, if it is dried by energy sources such as steam and heat - conducting oil, there are problems such as high energy consumption and high operating costs. Summary of the Invention

[0003] In view of the above - mentioned technical problems, the present invention provides a method and a system for co - incineration treatment of multi - source solid wastes, in order to at least partially solve the above - mentioned technical problems. For this purpose, the technical solutions provided by the present invention are as follows.

[0004] In the first aspect of the present invention, a method for co - incineration treatment of multi - source solid wastes is provided, including: feeding water - containing gasification fly ash and a sludge conditioner into the inner tank of an integrated stirring device for mixing, and the obtained wall - breaking agent overflows from the inner tank and flows into the outer tank of the integrated stirring device to be mixed with the sludge entering the outer tank to obtain a mixed material, wherein the main components of the water - containing gasification fly ash include water, coal ash, and some un - converted carbon; using a high - pressure mechanical pressure - filtration device to dehydrate the mixed material to obtain a dehydrated material; and transporting the dehydrated material to the circulating fluidized - bed incinerator of a circulating fluidized - bed device to incinerate the sludge and the water - containing gasification fly ash by using the carbon contained in the water - containing gasification fly ash as fuel, generating slag and a gas - solid mixed material.

[0005] As a second aspect of the present invention, a system for co-incineration treatment of multi-source solid waste is provided, which is suitable for implementing the method for co-incineration treatment of multi-source solid waste described above. The system includes: an integrated stirring device, a high-pressure mechanical pressure filtration device, and a circulating fluidized bed device. Among them, the integrated stirring device includes: an inner tank body, an outer tank body, and a stirring unit. The stirring unit includes a stirring motor fixed on the top of the outer tank body, a stirring shaft controlled by the stirring motor and extending through the inner tank body to the bottom of the outer tank body, and a plurality of stirring blades arranged on the stirring shaft. The inner tank body is suitable for mixing water-containing gasified fly ash and a sludge conditioner to obtain a wall-breaking agent. The outer tank body is connected through an overflow port provided on the top side wall of the inner tank body, so that the wall-breaking agent is mixed with the sludge entering the outer tank body to form a mixed material; the high-pressure mechanical pressure filtration device is connected to a mixed material outlet provided at the bottom of the outer tank body. The high-pressure mechanical pressure filtration device is composed of multiple layers of thin filter cloths to dehydrate the mixed material to obtain a dehydrated material; the circulating fluidized bed device includes a circulating fluidized bed incinerator. A raw material inlet connected to a filter cake outlet of the high-pressure mechanical pressure filtration device is provided on the side wall of the circulating fluidized bed incinerator, so as to send the dehydrated material into the circulating fluidized bed incinerator to realize the incineration of sludge and water-containing gasified fly ash by using the carbon contained in the water-containing gasified fly ash, and generate a gas-solid mixed material and slag.

[0006] Based on the above technical solutions, the method and system for co-incineration treatment of multi-source solid waste provided by the present invention have at least one of the following beneficial effects:

[0007] (1) In the present invention, the water-containing gasified fly ash and sludge are co-treated. Since the sludge has a high ash content and a low calorific value, external supplementary energy such as coal or diesel needs to be added during separate incineration, while the water-containing gasified fly ash contains carbon and is a high-calorific value fuel. Incinerating the dehydrated material obtained after mixing and dehydrating the two has the advantages of higher thermal efficiency, no need for external supplementary energy, and higher efficiency. Further, in the present invention, the dehydrated material obtained after mixing and dehydrating the water-containing gasified fly ash with a small particle size and the sludge with a high viscosity is incinerated, which can make the water-containing gasified fly ash adhere to the surface of the sludge and is not easily dispersed, ensuring the residence time of the water-containing gasified fly ash in the circulating fluidized bed incinerator and realizing the efficient incineration of the gasified fly ash and sludge.

[0008] (2) Since the traditional sludge dewatering system sets the sludge conditioner tank and the sludge tank separately, there are problems of large floor area and high equipment investment. To reduce the floor area and save equipment investment, this system adopts an integrated stirring device, and the inner tank and the outer tank are connected by setting an overflow port on the inner tank. The inner tank is suitable for mixing water-containing gasified fly ash and sludge conditioner. After being evenly mixed, it overflows to the outer tank as a sludge breaker, and the outer tank is used to mix the breaker and the sludge to achieve the purpose of sludge dewatering. Since the dehydration efficiency of the traditional horizontal plate and frame filter press device is low and can only reduce the moisture content of the material to about 70%, the high-pressure mechanical filter press device of the present invention adopts a vertical method, and the mixed material is pressed by a high-pressure hydraulic machine. The moisture content of the dehydrated material obtained after pressing can reach 30-50%, improving the dehydration efficiency. The circulating fluidized bed incinerator is responsible for incinerating the dehydrated material to realize the harmlessness and reduction of sludge. Description of the Drawings

[0009] Figure 1 It is a schematic structural diagram of the multi-waste co-incineration treatment system in the embodiment of the present invention;

[0010] Figure 2 It is a schematic structural diagram of the integrated stirring device in the embodiment of the present invention.

[0011]

Description of the Reference Numerals

[0012] 1 - Integrated stirring device, 101 - First fly ash inlet, 102 - First conditioner inlet, 103 - Sludge inlet, 104 - Inner tank, 105 - Outer tank, 106 - Stirring motor, 107 - Stirring shaft, 108 - First stirring blade, 109 - Second stirring blade, 110 - Third stirring blade, 111 - Fourth stirring blade, 112 - Reinforcement device, 113 - Overflow port, 114 - First support, 115 - Second support, 116 - Mixed material outlet, 117 - Emergency discharge port;

[0013] 2 - High-pressure mechanical filter press device, 21 - Filter cloth, 22 - Filter cake outlet;

[0014] 3 - Circulating fluidized bed incinerator, 31 - Raw material inlet, 32 - Gas-solid mixed material outlet, 33 - Return port, 34 - Slag discharge port, 35 - Oxidant inlet;

[0015] 4 - Gas-solid separator, 41 - Gas outlet, 42 - Solid outlet;

[0016] 5 - Return feeder, 51 - Solid inlet, 52 - Return outlet;

[0017] 6 - Air preheater, 61 - First flue gas inlet, 62 - Air outlet, 63 - Air inlet, 64 - First flue gas outlet;

[0018] 7 - Waste heat boiler, 71 - Cold water inlet, 72 - Second flue gas inlet, 73 - Steam outlet, 74 - Second flue gas outlet;

[0019] 8 - Flue gas purification unit;

[0020] A - Water - containing gasified fly ash, B - Sludge conditioner, C - Sludge, D - Mixed material, E - Dewatered material, F - Slag, G - Gas - solid mixed material, H - High - temperature flue gas, I - Solid material, J - Normal - temperature air, K - Pre - heated air, L - Medium - temperature flue gas, M - De - aerated water, N - Low - temperature flue gas, O - Water vapor. Detailed implementation manners

[0021] To make the objectives, technical solutions and advantages of the present invention more clear and understandable, the following further elaborates the present invention in detail with reference to specific embodiments and the accompanying drawings.

[0022] The water - containing gasified fly ash is a solid waste generated in the coal gasification section, mainly composed of coal ash, partially unreacted carbon, etc. Affected by the ash content of the raw coal and the system load, the water content of the water - containing gasified fly ash reaches more than 60%, which not only causes a large amount of waste of water resources, but also has disadvantages such as difficult water treatment in the slag yard and high transportation costs. In recent years, with the rapid development of the coal chemical industry, how to dispose of the large amount of water - containing gasified fly ash generated by the gasifier and eliminate the pollution of the waste residue has become a technical problem that needs to be solved urgently for sustainable development. For ordinary solid waste municipal sludge and industrial solid waste water - containing gasified fly ash, the water content in the sludge or water - containing gasified fly ash is mainly reduced through drying and heat treatment, and then sent to the incinerator for incineration to achieve the harmlessness and reduction of solid waste. However, due to the high water content of the sludge and water - containing gasified fly ash, if dried by energy such as steam and heat - conducting oil, there will be problems such as high energy consumption, high operating cost and low economic efficiency. If the microorganisms in the sludge are broken by adding flocculants such as polyacrylamide (PAM), the cost of the sludge conditioner will be too high and the dehydration efficiency will be low; moreover, the traditional sludge dehydration system sets the sludge conditioner tank and the sludge tank separately, which has a large floor area and high equipment investment.

[0023] In view of the existing problems, the present invention provides a method for co-incineration treatment of multi-source solid waste, which co-treats water-containing gasification fly ash and sludge. By utilizing the property of high calorific value of the water-containing gasification fly ash, it is mixed with sludge with low calorific value and then subjected to incineration treatment, solving the problems that sludge combustion requires external energy and high energy consumption, and enabling a relatively high thermal efficiency. Further, by utilizing the characteristic of high viscosity of the sludge, after mixing with the water-containing gasification fly ash, the gasification fly ash can adhere to the surface of the sludge and is not easily dispersed, ensuring that the gasification fly ash can smoothly enter the furnace, avoiding the explosion of the water-containing gasification fly ash in the feeding device, reducing the safety hazard; it also ensures the residence time of the gasification fly ash in the circulating fluidized bed incinerator, avoiding unreacted gasification fly ash from entering the backend waste heat boiler, reducing the abrasion of the gasification fly ash on the backend waste heat boiler, and having less ash accumulation, thus improving the system thermal efficiency. Moreover, the water-containing gasification fly ash can be used as a cell wall breaker, achieving a relatively high dehydration efficiency and solving the problem of excessively high cost caused by using flocculants or sludge conditioners such as PAM.

[0024] In terms of system improvement, to reduce the floor area and save equipment investment, the present system adopts an integrated stirring device. By designing the tank body and the stirring unit, the tank body is divided into an inner tank body and an outer tank body, and the inner tank body and the outer tank body are connected through an overflow port on the inner tank body to construct an integrated stirring device. When the liquid level of the cell wall breaker composed of the water-containing gasification fly ash and the sludge conditioner exceeds the overflow port on the inner tank body, it flows into the outer tank body and mixes with the sludge in the tank body to obtain a mixed material, achieving the purpose of removing the bound water in the sludge. The present invention uses a high-pressure mechanical pressure filtration device to press the mixed material vertically. The moisture content of the dehydrated material obtained after pressing can reach 30-50%. By adopting the high-pressure mechanical pressure filtration device of the present invention, the heat drying step in the traditional sludge and water-containing gasification fly ash dehydration system is omitted, greatly improving the dehydration efficiency.

[0025] Specifically, the present invention provides a method for co-incineration treatment of multi-source solid waste.

[0026] Figure 1 is a schematic structural diagram of the system for co-incineration treatment of multi-source solid waste in the embodiment of the present invention; Figure 2 is a schematic structural diagram of the integrated stirring device in the embodiment of the present invention.

[0027] As Figure 1 、 Figure 2As shown in the figure, the method for co-incineration treatment of multi-source solid waste provided by the present invention includes: feeding the water-containing gasification fly ash A and the sludge conditioner B into the inner tank 104 of the integrated stirring device 1 for mixing, and the obtained wall-breaking agent overflows from the inner tank 104 and flows into the outer tank 105 of the integrated stirring device 1, where it is mixed with the sludge C entering the outer tank 105 to obtain a mixed material D. Among them, the main components of the water-containing gasification fly ash A include water, coal ash, and part of the unreacted carbon; using the high-pressure mechanical pressure filtration device 2 to dehydrate the mixed material D to obtain a dehydrated material E; transporting the dehydrated material E to the circulating fluidized bed incinerator 3 of the circulating fluidized bed device to utilize the carbon contained in the water-containing gasification fly ash A as fuel to realize the incineration of the sludge C and the water-containing gasification fly ash A, generating furnace slag F and a gas-solid mixed material G.

[0028] In the embodiment of the present invention, since the traditional sludge dehydration and conditioning process directly mixes the sludge conditioner B with the sludge C, resulting in a low concentration and weak effect of the sludge conditioner B, the demand is large. In the present invention, the sludge conditioner B is mixed with the water-containing gasification fly ash A as a wall-breaking agent. The porous particles in the water-containing gasification fly ash in the wall-breaking agent can adsorb the water and organic matter in the sludge, destroy the colloidal structure, and at the same time convert part of the capillary water and adsorbed water in the sludge into void water that can be mechanically removed, thereby changing the sludge viscosity and improving the sludge fluidity and solid-liquid separation performance. Compared with the traditional method of additionally adding a wall-breaking agent, the present invention uses the water-containing gasification fly ash as part of the wall-breaking agent, reducing the consumption and cost of the sludge conditioner B while realizing sludge dehydration. Further, since the sludge C has a high water content and a low calorific value, the existing sludge independent incineration technology requires the addition of auxiliary fuels such as coal or diesel. The present invention uses the high-calorific value solid waste water-containing gasification fly ash A as an auxiliary fuel to realize the incineration of the sludge C and reduce the use of coal or diesel, not only recycling the solid waste generated in the coal gasification section but also reducing the consumption of non-renewable energy. In addition, the particle size of the water-containing gasification fly ash A generated by the existing circulating fluidized bed gasifier is relatively small, about 30-60 μm. When incinerating this type of water-containing gasification fly ash A alone, it is difficult for the water-containing gasification fly ash A to enter the furnace smoothly, and it is easy to have a combustion reaction in the feeding device, posing a safety hazard. The present invention adds the water-containing gasification fly ash A generated by the circulating fluidized bed gasifier to the sludge conditioner B for pre-stirring, then mixes it with the sludge C for stirring, and then uniformly conducts mechanical pressure filtration dehydration treatment, which can enable the material to smoothly enter the incinerator and avoid the risk of spontaneous combustion, ensuring the continuous and stable operation of the equipment.

[0029] In an embodiment of the present invention, the water content of sludge C is above 80%, for example, it can be 80%, 83%, 85%, 87%, 90%, 95%. Most of the existing sludge drying and incineration technologies use drying devices such as disk dryers, paddle dryers, and vacuum dryers, which require steam, heat transfer oil, etc. as heat sources for drying, resulting in high drying energy consumption and operating costs. In response to this, the present invention proposes to use a hierarchical mechanical dehydration device, which can reduce the water content of sludge with a high water content (above 80%) and water-vaporized fly ash without using steam, heat transfer oil, etc. as heat sources, reducing the dehydration energy consumption and operating costs. Specifically, the hierarchical mechanical dehydration device adopted in the present invention is a high-pressure mechanical filter press device 2, which is provided with multiple layers of thin filter cloths 21, and the mixed material D is evenly spread between the upper and lower filter cloths 21, with each layer having a thickness of 1-3 cm, which is beneficial to improving the dehydration efficiency. The high-pressure mechanical filter press device 2 adopts a vertical and hierarchical method, and the mixed material D is pressed by a high-pressure hydraulic machine, which can energy-efficiently press and dehydrate the mixed material D into dehydrated material E, with its thickness being 5-10 mm, and the water content is reduced to 30-50%. Among them, the filter press pressure is set to 20-28 MPa, and the filter press time is controlled to be 20-50 min. The thickness of the mixed material D between the multiple layers of thin filter cloths 21 can be, for example, 1 cm, 1.5 cm, 2 cm, 2.5 cm, 3 cm; the filter press pressure can be, for example, 20 MPa, 22 MPa, 25 MPa, 26 MPa, 28 MPa; the filter press time can be, for example, 20 min, 30 min, 40 min, 50 min; the thickness of the dehydrated material E can be, for example, 5 mm, 6 mm, 7 mm, 8 mm, 9 mm, 10 mm.

[0030] According to an embodiment of the present invention, the water content of the water-containing gasification fly ash A is 4% - 95%, for example, it can be 4%, 15%, 25%, 35%, 45%, 55%, 65%, 75%, 85%, 95%. It contains two kinds of water-containing gasification fly ash. One is the water-containing gasification fly ash produced by a entrained flow gasifier, with a relatively high water content (generally above 90%, such as 50% - 95%); the other is the water-containing gasification fly ash produced by a circulating fluidized bed gasifier, with a relatively low water content (4% - 49%). When the water content of the water-containing gasification fly ash A is 50% - 95%, the sludge conditioner B is added in solid form and can be dissolved by the water in the water-containing gasification fly ash A, which not only reduces the water content in the water-containing gasification fly ash and facilitates subsequent dehydration and incineration treatment, but also reduces the consumption of additional water. When the water content of the water-containing gasification fly ash A is 4% - 49%, it cannot meet the water content required for the dissolution of the sludge conditioner B. At this time, the sludge conditioner B needs to be added in the form of a solution with a concentration of 5% - 15wt%, for example, it can be added in the form of a solution with a concentration of 5wt%, 7wt%, 10wt%, 12wt%, 15wt%. If the concentration of the sludge conditioner B is lower than 5%, it will cause incomplete dehydration of the sludge C, which is not conducive to subsequent pressure filtration dehydration and incineration treatment; if the concentration of the sludge conditioner B is higher than 15%, it will cause waste. Therefore, the method for co-incineration treatment of multiple sources of solid waste of the present invention can treat the water-containing gasification fly ash A with a water content of 4% - 95%. Further, the sludge conditioner B in the present invention can be selected from polyferric sulfate, polyaluminum chloride, etc.

[0031] According to an embodiment of the present invention, the mass ratio of the water-containing gasification fly ash A to the sludge C is 1:5 - 2:1, for example, it can be 1:5, 1:4, 1:3, 1:2, 1:1, 2:1; the air-dried basis calorific value of the water-containing gasification fly ash A ≥ 3500 kcal / kg, for example, it can be 3500 kcal / kg, 3700 kcal / kg, 4000 kcal / kg, 4200 kcal / kg, 4500 kcal / kg, and the air-dried basis calorific value of the sludge C ≥ 1600 kcal / kg, for example, it can be 1600 kcal / kg, 2000 kcal / kg, 2300 kcal / kg, 2500 kcal / kg, 2600 kcal / kg.

[0032] In an embodiment of the present invention, controlling the mass ratio of the water-containing gasification fly ash A to the sludge C at 1:5 - 2:1, the air-dried basis calorific value of the water-containing gasification fly ash A ≥ 3500 kcal / kg, and the air-dried basis calorific value of the sludge C ≥ 1600 kcal / kg is to make the mixed material D of the two meet the calorific value required for subsequent combustion. If the proportion of the sludge C is higher, or the calorific values of the two are lower, the calorific value of the mixed material D cannot meet the incineration requirements, and the purpose of co-incineration treatment of multiple sources of solid waste cannot be achieved.

[0033] Continue as Figure 1 shown, the gas-solid mixed material G is separated by the centrifugal action of the gas-solid separator 4 to obtain high-temperature flue gas H and solid material I. The gas-solid separator 4 can be a high-efficiency cyclone separator or other high-efficiency gas-solid separators. The solid material I includes unreacted gasification fly ash and ash slag. The solid material I is returned to the circulating fluidized bed incinerator 3 through the return feeder 5 to realize the recycling of the solid material I and reduce the solid particles in the high-temperature flue gas H so as not to cause abrasion to the equipment at the back end.

[0034] Continue as Figure 1 shown, the high-temperature flue gas H exchanges heat with normal-temperature air J in the air preheater 6 to obtain preheated air K and medium-temperature flue gas L. The preheated air K participates in the incineration reaction in the circulating fluidized bed incinerator 3 as an oxidant. If the normal-temperature air J directly enters the circulating fluidized bed incinerator 3, the temperature in the circulating fluidized bed incinerator 3 will drop significantly, affecting the incineration efficiency of the circulating fluidized bed incinerator 3. By preheating through the air preheater 6 and using the waste heat of the high-temperature flue gas H to heat the normal-temperature air J to 450 - 600 °C, this adverse effect can be reduced and a relatively high incineration efficiency can be maintained; among them, the temperature in the circulating fluidized bed incinerator 3 is 900 - 1100 °C, for example, it can be 900 °C, 1000 °C, 1100 °C, the temperature of the high-temperature flue gas H is 850 - 1050 °C, for example, it can be 850 °C, 900 °C, 1000 °C, 1050 °C, the temperature of the preheated air K is 450 - 600 °C, for example, it can be 450 °C, 500 °C, 550 °C, 600 °C, and the temperature of the medium-temperature flue gas L is 500 - 650 °C, for example, it can be 500 °C, 550 °C, 600 °C, 650 °C.

[0035] Continue as Figure 1 shown, the medium-temperature flue gas L exchanges heat with deaerated water M in the waste heat boiler 7 as a heat source to obtain low-temperature flue gas N and water vapor O. The water vapor O can be sent out as product steam; the low-temperature flue gas N is introduced into the flue gas purification unit 8 for dust removal and purification in order to obtain up-to-standard flue gas and achieve up-to-standard discharge; among them, the temperature of the low-temperature flue gas N is 180 - 250 °C, for example, it can be 180 °C, 200 °C, 220 °C, 250 °C.

[0036] Thus, the present invention realizes the co-incineration treatment of multi-source solid wastes by mixing the water-containing gasification fly ash A and the sludge conditioner B to form a wall-breaking agent, then mixing with the sludge C, pressure filtering and dewatering, and co-incinerating in the circulating fluidized bed incinerator 3, solves the problem that the sludge C has a low calorific value and cannot be incinerated alone, and avoids the explosion of the small-particle-size water-containing gasification fly ash A in the feeding device.

[0037] As a second aspect of the present invention, a system for co-incineration treatment of multi-source solid waste is provided, which is suitable for implementing the method for co-incineration treatment of multi-source solid waste. The system includes: an integrated stirring device 1, comprising: an inner tank 104, an outer tank 105 and a stirring unit. The stirring unit includes a stirring motor 106 fixed on the top of the outer tank 105, a stirring shaft 107 controlled by the stirring motor 106 and extending through the inner tank 104 to the bottom of the outer tank 105, and a plurality of stirring blades arranged on the stirring shaft 107. The inner tank 104 is suitable for mixing the water-containing gasification fly ash A and the sludge conditioner B to obtain a wall-breaking agent. The outer tank 105 is connected through an overflow port 113 provided on the top side wall of the inner tank 104, so that the wall-breaking agent is mixed with the sludge C entering the outer tank 105 to form a mixed material D; a high-pressure mechanical pressure filtration device 2, connected to a mixed material outlet 116 provided at the bottom of the outer tank 105. The high-pressure mechanical pressure filtration device 2 is composed of multiple layers of thin filter cloths 21 to dehydrate the mixed material D to obtain a dehydrated material E; a circulating fluidized bed device, including a circulating fluidized bed incinerator 3. A raw material inlet 31 communicating with a filter cake outlet 22 of the high-pressure mechanical pressure filtration device 2 is provided on the side wall of the circulating fluidized bed incinerator 3, so as to feed the dehydrated material E into the circulating fluidized bed incinerator 3 to realize the incineration of the sludge C and the water-containing gasification fly ash A by using the carbon contained in the water-containing gasification fly ash A, and generate a gas-solid mixed material G and slag F.

[0038] In an embodiment of the present invention, an overflow port 113 arranged on the top side wall of the inner tank body 104 serves as a channel connecting the inner tank body 104 and the outer tank body 105. The stirring unit is fixed on the outer tank body 105. The stirring shaft 107 in the stirring unit is controlled by a stirring motor 106 and extends through the inner tank body 104 to the bottom of the outer tank body 105. The stirring blades on the stirring shaft 107 can be used to stir and mix the water-containing gasified fly ash A and the sludge conditioner B in the inner tank body 104 to obtain a wall-breaking agent. When the liquid level of the wall-breaking agent is higher than the overflow port 113, it overflows and enters the outer tank body 105, and is stirred and mixed with the sludge C in the outer tank body 105. The porous particles in the water-containing gasified fly ash A in the wall-breaking agent can adsorb the water and organic matter in the sludge C, destroy the colloidal structure, and at the same time convert part of the capillary water and adsorbed water in the sludge C into void water that can be mechanically removed, thereby changing the viscosity of the sludge C and improving the fluidity and solid-liquid separation performance of the sludge C. After the wall-breaking agent and the sludge C are uniformly mixed in the outer tank body 105, they can be discharged from the mixture outlet 116 at the bottom of the outer tank body 105 and enter the downstream high-pressure mechanical filter press device 2 for dehydration treatment. The dehydration efficiency of the traditional horizontal plate and frame filter press device is relatively low, and it can only reduce the moisture content of the mixture to about 70%. The dehydrated material with such a high moisture content entering the circulating fluidized bed incinerator will significantly affect the operation stability and reduce the incineration efficiency. In response, the present invention uses a high-pressure mechanical filter press device 2 with vertical and staged pressing for dehydration treatment. A plurality of layers of thin filter cloths 21 are arranged in the high-pressure mechanical filter press device 2, and the mixed material D is evenly spread between the upper and lower filter cloths 21 with a thickness of 1-3 cm, which is beneficial to improving the dehydration efficiency. The moisture content of the dehydrated material E obtained after pressing can reach 30-50%, and no subsequent heat drying treatment is required, which simplifies the dehydration treatment process, improves the dehydration efficiency, reduces the energy consumption of traditional drying, and reduces the drying cost. Finally, the dehydrated material E is sent into the circulating fluidized bed incinerator 3 for incineration, and the carbon contained in the water-containing gasified fly ash A is used to realize the incineration of the sludge C and the water-containing gasified fly ash A, and multi-source solid waste co-incineration treatment is realized through the system of the present invention.

[0039] In an embodiment of the present invention, the sludge conditioner B can be selected from polyferric sulfate, polyaluminum chloride, etc., which belong to acidic or alkaline polymers and have corrosiveness; and the water-containing gasified fly ash A has a small particle size and will cause wear to the inner tank body 104, the outer tank body 105 and the pipeline; and the sludge C has a high ash content and contains acid-base substances, which will also cause wear and corrosion to the inner tank body 104, the outer tank body 105 and the pipeline. Therefore, both the inner tank body 104 and the outer tank body 105 in the integrated stirring device 1 are made of stainless steel.

[0040] Continue as Figure 2As shown in the figure, in the integrated stirring device 1 of the present invention: at the top of the outer tank body 105, a first fly ash inlet 101 for the entry of water-containing gasified fly ash A, a first regulator inlet 102 for the entry of sludge regulator B are provided, a sludge inlet 103 is provided on the side wall, and a material outlet 116 for discharging the mixed material formed by the wall-breaking agent and the sludge is provided at the bottom. The sludge inlet 103 is located on the side wall of the outer tank body 105 below the bottom of the inner tank body 104. The height H of the outer tank body 105 is greater than the height h of the inner tank body 104. The height of the outer tank body is H, and the distance from the sludge inlet 103 to the bottom of the outer tank body is 1 / 2 - 1 / 3H. This structural design is, on the one hand, to prevent the sludge from entering the inner tank body 104 during the stirring process and to avoid affecting the outer wall of the inner tank body 104; on the other hand, it is to ensure the volume of the sludge in the outer tank body 105 and to guarantee the working efficiency of the integrated stirring device. The height of the inner tank body 104 is h, and both the fly ash pipeline and the regulator pipeline are located at 1 / 4h - 1 / 2h below the overflow port; the overflow port 113 is provided at 1 / 9 - 1 / 15h from the top of the inner tank body 104, and the distance from the inner wall of the outer tank body 105 is 1 / 10 - 1 / 7d. The overflow port can be one, two or more, and multiple overflow ports 113 are arranged in a circle around the inner tank body 104. If the position of the overflow port 113 is lower, the capacity of the inner tank body 104 will be smaller, which is not conducive to uniform mixing and the mixing efficiency is lower; if the distance between the overflow port 113 and the inner wall of the outer tank body 105 is smaller, it may hinder the smooth entry of the wall-breaking agent into the outer tank body 105, and at the same time, the wall-breaking agent will also scour the inner wall of the outer tank body 105. If the distance is larger, the capacity of the inner tank body 104 will be reduced, and the mixing efficiency of the integrated stirring device cannot be guaranteed.

[0041] In an embodiment of the present invention, when the water content of the water-containing gasified fly ash A is 4% - 49%, at this time, the sludge regulator B can be a liquid (such as polyferric sulfate liquid), and a flow meter and a delivery pump can be provided between the sludge regulator storage tank and the first regulator inlet 102 to pump the liquid sludge regulator B into the first regulator inlet 102.

[0042] Continue as Figure 2As shown in the figure, at the top of the inner tank body 104, there are provided a second fly ash inlet connected to the first fly ash inlet 101 through a fly ash pipeline, and a second regulator inlet connected to the first regulator inlet 102 through a regulator pipeline. The inner tank body 104 is located inside the outer tank body 105, and the water-containing gasified fly ash A and the sludge regulator B can be completely introduced into the inner tank body 104. Further, the diameter of the outer tank body 105 is d, and the fly ash pipeline and the regulator pipeline are arranged at a position of 1 / 3 - 1 / 6d from the edge of the outer tank body 105, so as to ensure that the fly ash pipeline and the regulator pipeline are located inside the inner tank body 104, and further ensure that the water-containing gasified fly ash A and the sludge regulator B both enter the inner tank body 104. Furthermore, the fly ash pipeline and the regulator pipeline are symmetrically arranged. The diameters of the fly ash pipeline and the regulator pipeline are d1, and the transverse distance between the overflow port 113 and the inlets of the fly ash pipeline and the regulator pipeline is d1 - 3d1. The inner tank body 104 is fixed to the inner wall of the outer tank body 105 through the first support 114, and a plurality of second supports 115 are further provided at the bottom of the outer tank body 105 for supporting the integrated stirring device 1. The plurality of second supports 115 can support the integrated stirring device 1 in the form of a triangle or surrounding a base to ensure stability. An emergency discharge port 117 can also be provided at the bottom of the outer tank body 105. When the materials in the tank reach the threshold or exceed the maximum capacity (more than 90% and above of the volume of the outer tank body 105), the emergency discharge port 117 can be opened for discharging materials to ensure the safety and normal use of the device. Furthermore, the volume ratio of the inner tank body 104 to the outer tank body 105 is 1:3 - 1:8

[0043] Continue as Figure 2 As shown in the figure, in the inner tank body 104, at least one stirring blade, such as the first stirring blade 108, is provided on the stirring shaft 107; in the outer tank body 105, at least two stirring blades, such as the second stirring blade 109, the third stirring blade 110, and the fourth stirring blade 111, are provided on the stirring shaft 107, and the distances between the stirring blades are the same or different; among them, the stirring blades have a cross-shaped or fan-shaped structure. For example: the first stirring blade 108, the second stirring blade 109, and the third stirring blade 110 have a cross-shaped structure, and the fourth stirring blade 111 has a fan-shaped structure.

[0044] In an embodiment of the present invention, to achieve an integrated stirring effect, facilitate control, save electricity, and reduce the occupation of the space of the inner tank 104 and the outer tank 105, only one stirring shaft 107 is provided for the integrated stirring device 1. The stirring speed of the stirring shaft 107 can be controlled within 15 - 50 r / min to achieve uniform stirring of the water-containing gasified fly ash A, the sludge conditioner B, the wall-breaking agent, and the sludge C. Among them, the stirring speed of the stirring shaft 107 can be 15 r / min, 25 r / min, 35 r / min, 45 r / min, or 50 r / min. Since the inner tank 104 is used to mix the water-containing gasified fly ash A and the sludge conditioner B, and the mixture of the two has a small mass and is easy to disperse, at least one stirring blade is provided; while the outer tank 105 is used to mix the wall-breaking agent and the sludge C, and the mixture of the two has a large volume, mass, and stirring resistance, and at least two stirring blades need to be provided to ensure sufficient and uniform stirring. Among them, the spacing between the stirring blades in the inner tank 104 and the outer tank 105 can be the same or different, and is specifically set according to the actual stirring situation. Setting the stirring blade as a cross-shaped or fan-shaped structure can meet the requirements of shear force or large-flow stirring, and make the wall-breaking agent and the sludge C mix more evenly.

[0045] In an embodiment of the present invention, since the depth of the outer tank 105 is large and the torque during stirring is large, it is easy to damage the stirring shaft 107. Therefore, as continued in Figure 2 shown, a plurality of reinforcement devices 112 are provided on the stirring shaft 107. Among them, at least one reinforcement device 112 is provided at the torque threshold (such as the place where the torque is the largest), which can effectively avoid damage to the stirring shaft 107.

[0046] As continued in Figure 1As shown in the figure, the circulating fluidized bed incinerator 3 is further provided with: a gas-solid mixed material outlet 32 at the top, a return port 33 in the dense phase region, a slag discharge port 34 at the bottom, and an oxidant inlet 35. Further, the height of the circulating fluidized bed incinerator 3 is h1, and the distance from the raw material inlet 31 to the bottom of the circulating fluidized bed incinerator 3 is 1 / 4h1 to 1 / 10h1. Setting the raw material inlet 31 here can reduce the energy consumption of mechanically pushing the dehydrated material E into the circulating fluidized bed incinerator 3; and if the raw material inlet 31 is too high, the dehydrated material E may be directly blown out by the airflow or enter the downstream device without being fully burned, affecting the incineration efficiency. The gas-solid mixed material G is discharged from the circulating fluidized bed incinerator 3 through the gas-solid mixed material outlet 32 and enters the gas-solid separator 4 for gas-solid separation to obtain high-temperature flue gas H and solid material I. The dense phase region is a region in the circulating fluidized bed incinerator 3 where the concentration of materials or combustion medium is relatively high and the flow characteristics are relatively dense, and it is the core region for efficient and stable operation. Setting the return port 33 in the dense phase region can enable the returned material to be directly incinerated. The slag F generated by the incineration of the circulating fluidized bed incinerator 3 is discharged through the slag discharge port 34 at the bottom of the incinerator to prevent the accumulation of slag F and affect the incineration efficiency in the furnace. The oxidant enters the circulating fluidized bed incinerator 3 through the oxidant inlet 35 to provide oxygen for incineration. Among them, the oxidant can be preheated air K, and the oxygen concentration in the preheated air K is 21%.

[0047] The circulating fluidized bed device further includes: a gas-solid separator 4 and a return feeder 5 that are connected in sequence downstream of the gas-solid mixed material outlet 32; wherein, the gas-solid separator 4 uses centrifugal force to perform gas-solid separation on the gas-solid mixed material G to obtain high-temperature flue gas H and solid material I, and the solid material I includes unreacted water-containing gasified fly ash A and reacted ash slag. The gas-solid separator 4 is provided with a gas outlet 41 for discharging the high-temperature flue gas H and a solid outlet 42 for discharging the solid material I. The return feeder 5 is provided with a solid inlet 51 connected to the solid outlet 42 and a return outlet 52 connected to the return port 33, and is suitable for returning the solid material I to the dense phase region of the circulating fluidized bed incinerator 3 for recycling.

[0048] The air preheater 6 is applicable to heat exchange between high-temperature flue gas H and normal-temperature air J to obtain preheated air K and medium-temperature flue gas L. The temperature of the high-temperature flue gas H is 850 - 1050 °C, for example, it can be 850 °C, 900 °C, 1000 °C, 1050 °C; the temperature of the preheated air K is 450 - 600 °C, for example, it can be 450 °C, 500 °C, 550 °C, 600 °C. The air preheater 6 is provided with a first flue gas inlet 61 connected to the gas outlet 41 for the high-temperature flue gas H to enter, an air outlet 62 connected to the oxidant inlet 35 for discharging the preheated air K, an air inlet 63 for the normal-temperature air J to enter, and a first flue gas outlet 64 for discharging the medium-temperature flue gas L. The preheated air K participates in the combustion reaction in the circulating fluidized bed incinerator 3 as an oxidant, and at the same time, it can reduce the temperature fluctuation in the circulating fluidized bed incinerator 3 and maintain a high combustion efficiency. The medium-temperature flue gas L is discharged through the first flue gas outlet 64 and enters the downstream waste heat boiler 7.

[0049] The waste heat boiler 7 is located downstream of the air preheater 6 and is applicable to heat exchange between the medium-temperature flue gas L and deaerated water M to obtain low-temperature flue gas N and water vapor O. The temperature of the medium-temperature flue gas L is 500 - 650 °C, for example, it can be 500 °C, 550 °C, 600 °C, 650 °C; the temperature of the low-temperature flue gas N is 180 - 250 °C, for example, it can be 180 °C, 200 °C, 220 °C, 250 °C. The waste heat boiler 7 is provided with a cold water inlet 71 for the deaerated water M to enter, a second flue gas inlet 72 connected to the first flue gas outlet 64, a steam outlet 73 for discharging the water vapor O, and a second flue gas outlet 74 for discharging the low-temperature flue gas N. The medium-temperature flue gas L undergoes heat exchange with the deaerated water M in the waste heat boiler 7, and the temperature reduction to obtain the low-temperature flue gas N can reduce the corrosion or damage of the subsequent flue gas purification unit 8 by high temperature and maintain the normal service life of the flue gas purification unit 8; at the same time, the deaerated water M is heated to become water vapor O, which can be sent out as a product to provide steam or heat source. Through the step-by-step heat exchange of the air preheater 6 and the waste heat boiler 7, local thermal stress or acid dew point corrosion caused by quenching can be avoided, and the heat exchange efficiency can be improved. At the same time, the thermal energy of the high-temperature flue gas H is converted into preheated air K or water vapor O, which can be used for power generation, heating or process requirements, improving the system energy efficiency; and reducing the temperature of the final discharged flue gas to meet the environmental protection emission standards.

[0050] The flue gas purification unit 8 is connected to the second flue gas outlet 74 and is applicable to dust removal and purification of the low-temperature flue gas N. The flue gas purification unit 8 also includes a cyclone separator, a bag filter and a desulfurization device to make the low-temperature flue gas N meet the emission standards and reduce the pollution of the low-temperature flue gas N to the environment.

[0051] In an embodiment of the present invention, a system for co-incineration treatment of multi-source solid wastes can achieve co-treatment of water-containing gasification fly ash A and sludge C, solving the problems existing in traditional sludge and water-containing gasification fly ash drying and incineration technologies, such as high moisture content and low calorific value of raw materials, and difficult stable combustion. The integrated stirring device 1 solves the problems of large floor area and high equipment investment of traditional sludge dewatering systems. The high-pressure mechanical filter press device 2 adopts a vertical method to reduce the moisture content of the dewatered material E to 30-50%, which can eliminate the subsequent thermal drying treatment, simplify the drying and incineration system, and improve the dewatering efficiency of traditional horizontal plate and frame filter press devices.

[0052] The following will specifically describe the method and system for co-incineration treatment of multi-source solid wastes of the present invention in conjunction with specific embodiments. It should be noted that the embodiments provided by the present invention are only for illustrative purposes and are not limited thereto.

[0053] Example 1

[0054] The water-containing gasification fly ash A generated by a certain entrained flow bed and the sludge C generated by a sewage treatment plant are treated using the system for co-incineration treatment of multi-source solid wastes of the present invention. Their proximate analysis and ultimate analysis are shown in Table 1. The schematic structural diagram of the system for co-incineration treatment of multi-source solid wastes is as Figure 1 shown, and the schematic diagram of the integrated stirring device used is as Figure 2 shown. The specific treatment process is as follows:

[0055] Table 1 Proximate analysis and ultimate analysis of raw materials (air-dried basis)

[0056]

[0057] (1) The water-containing gasification fly ash A with a moisture content of 90% generated by a certain entrained flow bed is transported through the first fly ash inlet 101 and the solid polyferric sulfate is transported through the first regulator inlet 102 into the inner tank 104 of the integrated stirring device 1, and the concentration of polyferric sulfate in the mixture is controlled to be 15%. The water-containing gasification fly ash A and polyferric sulfate are fully mixed evenly to obtain a wall-breaking agent. When the high material level is reached in the inner tank 104, the wall-breaking agent is discharged into the outer tank 105 through the overflow port 113 on the side wall of the inner tank 104.

[0058] (2) The sludge C with a moisture content of 80% produced by the sewage treatment plant is transported to the outer tank 105 of the integrated stirring device 1 through the sludge inlet 103, and the stirring speed of the stirring shaft 107 is set to 50r / min, so as to be mixed with the wall-breaking agent to obtain the mixed material D. The air-dry basis calorific value of the water-containing gasified fly ash A and the sludge C is detected by the detection device, wherein the air-dry basis calorific value of the water-containing gasified fly ash A is 5250kcal / kg, and the air-dry basis calorific value of the sludge C is 2000kcal / kg, and the air-dry basis mass ratio of the water-containing gasified fly ash A to the sludge C is controlled at 2:1. Finally, the mixed material D is sent to the high-pressure mechanical filter press 2 through the mixed material outlet 116 for dehydration treatment.

[0059] (3) To improve the dehydration efficiency, a thin layer of filter cloth 21 is provided in the high-pressure mechanical filter press device 2, and the mixed material D is evenly spread between the upper and lower filter cloths 21. The thickness of the mixed material D between each layer of filter cloth 21 is about 2 cm. The pressure of the high-pressure mechanical filter press device 2 is set to 20 MPa, and the filtration time is 30 min. The high-pressure mechanical filter press device 2 adopts a vertical graded dehydration method, and the mixed material D is squeezed by a high-pressure hydraulic machine. After squeezing, a dehydrated material E with a moisture content of 30% and a thickness of 7 mm is obtained.

[0060] (4) The dehydrated material E is transported to a circulating fluidized bed incinerator 3 for incineration to obtain high-temperature flue gas H and slag F, wherein the furnace temperature of the circulating fluidized bed incinerator 3 is 900°C.

[0061] (5) The high-temperature flue gas H is sent to the air preheater 6 for heat exchange treatment to obtain medium-temperature flue gas L and preheated air K. The temperature of the high-temperature flue gas H is 850°C, and the temperature of the preheated air K is 450°C.

[0062] (6) The medium-temperature flue gas L is introduced into the waste heat boiler 7 for waste heat recovery and utilization to obtain low-temperature flue gas N and water vapor O. The temperature of the medium-temperature flue gas L is 500° C., and the temperature of the low-temperature flue gas N is 210° C.

[0063] (7) The low-temperature flue gas N is introduced into the flue gas purification unit 8 for dust removal and purification to obtain flue gas that meets the standards and achieves standard emissions. The flue gas purification unit 8 includes a cyclone separator, a bag filter and a desulfurization device.

[0064] After treatment by the system in the above-mentioned embodiment 1, the carbon content in the slag discharged from the circulating fluidized bed incinerator 3 is 0.8wt%, and the pressure of the water vapor in the waste heat boiler 7 is 1.3MPaG and the temperature is 194°C.

[0065] Example 2

[0066] The system for co-incineration treatment of multi-source solid waste of the present invention is used to treat the water-containing gasification fly ash A generated by a certain factory and the sludge C generated by a sewage treatment plant. The proximate analysis and ultimate analysis are shown in Table 2. The schematic structural diagram of the system for co-incineration treatment of multi-source solid waste is as shown in Figure 1 shown, and the integrated stirring device used is as shown in Figure 2 shown. The specific treatment process is as follows:

[0067] Table 2 Proximate Analysis and Ultimate Analysis of Raw Materials (air-dried basis)

[0068]

[0069] (1) The water-containing gasification fly ash A with a moisture content of 65% generated by a certain entrained flow bed is fed through the first fly ash inlet 101 and the polymeric ferric sulfate solid is fed through the polymeric ferric sulfate inlet 102 into the inner tank 104 of the integrated stirring device 1, and the concentration of polymeric ferric sulfate in the mixture is controlled to be 11%. The water-containing gasification fly ash A and the polymeric ferric sulfate are fully mixed evenly to obtain a wall-breaking agent. When the high material level is reached in the inner tank 104, the wall-breaking agent is discharged into the outer tank 105 through the overflow port 113 on the side wall of the inner tank 104.

[0070] (2) The sludge C with a moisture content of 83% generated by the sewage treatment plant is fed through the sludge inlet 103 into the outer tank 105 of the integrated stirring device 1, and the stirring speed of the stirring shaft 107 is set to 15 r / min to mix with the wall-breaking agent to obtain a mixed material D. The air-dried basis calorific values of the water-containing gasification fly ash A and the sludge C are detected by a detection device. The air-dried basis calorific value of the water-containing gasification fly ash A is 3500 kcal / kg, and the air-dried basis calorific value of the sludge C is 3109 kcal / kg. The air-dried basis mass ratio of the water-containing gasification fly ash A to the sludge C is controlled at 1:1. Finally, the mixed material D is sent to the high-pressure mechanical pressure filtration device 2 through the mixed material outlet 116 for dehydration treatment.

[0071] (3) To improve the dehydration efficiency, the high-pressure mechanical pressure filtration device 2 is provided with a thin-layer filter cloth 21. The mixed material D is evenly spread between the upper and lower filter cloths 21, and the thickness of the mixed material D between each layer of filter cloth 21 is about 3 cm. The pressure of the high-pressure mechanical pressure filtration device 2 is set to 28 MPa, and the pressure filtration time is 50 min. The high-pressure mechanical pressure filtration device 2 adopts a vertical grading dehydration method to press the mixed material D through a high-pressure hydraulic machine. After pressing, a dehydrated material E with a moisture content of 50% and a thickness of 10 mm is obtained.

[0072] (4) The dehydrated material E is transported to the circulating fluidized bed incinerator 3 for incineration treatment to obtain high-temperature flue gas H and furnace slag F, where the furnace temperature of the circulating fluidized bed incinerator 3 is 1000 °C.

[0073] (5) The high-temperature flue gas H is sent to the air preheater 6 for heat exchange treatment to obtain medium-temperature flue gas L and preheated air K. The temperature of the high-temperature flue gas H is 950°C, and the temperature of the preheated air is 520°C.

[0074] (6) The medium-temperature flue gas L is introduced into the waste heat boiler 7 for waste heat recovery and utilization to obtain low-temperature flue gas N and water vapor O. The temperature of the medium-temperature flue gas is 600°C and the temperature of the low-temperature flue gas N is 180°C.

[0075] (7) The low-temperature flue gas N is introduced into the flue gas purification unit 8 for dust removal and purification to obtain flue gas that meets the standards and achieves standard emissions. The flue gas purification unit 8 includes a bag filter and a desulfurization device.

[0076] After treatment by the system in the above-mentioned embodiment 2, the carbon content in the slag discharged from the circulating fluidized bed incinerator 3 is 1.3wt%, and the pressure of the water vapor in the waste heat boiler 7 is 1.3MPaG and the temperature is 194°C.

[0077] Example 3

[0078] The system for the coordinated incineration of multi-source solid wastes of the present invention was used to treat the water-containing gasified fly ash A produced by a circulating fluidized bed of a certain factory and the sludge C produced by a sewage treatment plant. The industrial analysis and elemental analysis thereof are shown in Table 1. The schematic diagram of the system structure for the coordinated incineration of multi-source solid wastes is shown in Figure 1 As shown, the integrated stirring device used is as follows Figure 2 The specific processing flow is as follows:

[0079] Table 3 Industrial analysis and elemental analysis of raw materials (air-dried basis)

[0080]

[0081] (1) The water-containing gasified fly ash A with a moisture content of 4% produced by a circulating fluidized bed in a certain factory is transported to the inner tank body 104 of the integrated stirring device 1 through the first fly ash inlet 101 and the polyferric sulfate solid through the first conditioning agent inlet 102, and the concentration of the polyferric sulfate in the mixture is controlled to be 5%. The water-containing gasified fly ash A and the polyferric sulfate are fully mixed to obtain a wall-breaking agent. When the inner tank body 104 reaches a high material level, the wall-breaking agent is discharged into the outer tank body 105 through the overflow port 113 on the side wall of the inner tank body 104.

[0082] (2) Sludge C with a water content of 85% generated by the sewage treatment plant is transported through the sludge inlet 103 into the outer tank 105 of the integrated stirring device 1, and the stirring speed of the stirring shaft 107 is set to 30 r / min to be mixed with the wall-breaking agent to obtain the mixed material D. The air-dried basis calorific values of the water-containing gasification fly ash A and sludge C are detected by the detection device. The air-dried basis calorific value of the water-containing gasification fly ash A is 4380 kcal / kg, and the air-dried basis calorific value of the sludge C is 1600 kcal / kg. The air-dried basis mass ratio of the water-containing gasification fly ash A to the sludge C is controlled at 1:5. Finally, the mixed material D is sent through the mixed material outlet 116 to the high-pressure mechanical filter press device 2 for dehydration treatment.

[0083] (3) To improve the dehydration efficiency, the high-pressure mechanical filter press device 2 is provided with a thin-layer filter cloth 21. The mixed material D is evenly spread between the upper and lower filter cloths 21, and the thickness of the mixed material D between each layer of filter cloth 21 is about 1 cm. The pressure of the high-pressure mechanical filter press device 2 is set to 24 MPa, and the filter press time is 20 min. The high-pressure mechanical filter press device 2 adopts a vertical grading dehydration method to press the mixed material D through a high-pressure hydraulic machine. After pressing, the dehydrated material E with a water content of 40% and a thickness of 5 mm is obtained.

[0084] (4) The dehydrated material E is transported to the circulating fluidized bed incinerator 3 for incineration treatment to obtain high-temperature flue gas H and furnace slag F, where the furnace temperature of the circulating fluidized bed incinerator 3 is 1100 °C.

[0085] (5) The high-temperature flue gas H is sent to the air preheater 6 for heat exchange treatment to obtain medium-temperature flue gas L and preheated air K. The temperature of the high-temperature flue gas H is 1050 °C, and the temperature of the preheated air is 600 °C.

[0086] (6) The medium-temperature flue gas L is introduced into the waste heat boiler 7 for waste heat recovery and utilization to obtain low-temperature flue gas N and water vapor O. The temperature of the medium-temperature flue gas is 650 °C, and the temperature of the low-temperature flue gas N is 250 °C.

[0087] (7) The low-temperature flue gas N is introduced into the flue gas purification unit 8 for dust removal and purification treatment to obtain qualified flue gas for achieving qualified discharge. The flue gas purification unit 8 includes a cyclone separator, a bag filter, and a desulfurization device.

[0088] After being processed by the system in the above-mentioned Embodiment 3, the carbon content in the furnace slag discharged from the circulating fluidized bed incinerator 3 is 1.0 wt%, and the pressure of the water vapor in the waste heat boiler 7 is 3.82 MPaG, and the temperature is 450 °C.

[0089] In summary, by co-incinerating sludge C and water-containing gasification fly ash A, the present invention solves the problem that sludge C with low calorific value cannot be burned alone, and at the same time solves the problem that water-containing gasification fly ash A with small particle size is difficult to smoothly enter the furnace. Using the mixture of polyferric sulfate and water-containing gasification fly ash A as a wall-breaking agent can improve the sludge dehydration efficiency and reduce the dehydration cost. The high-pressure mechanical pressure filtration device 2 uses the method of vertical pressure filtration to uniformly perform mechanical dehydration treatment on water-containing gasification fly ash A and sludge C with high water content, improving the dehydration efficiency, simplifying the dehydration steps, and reducing the sludge drying cost.

[0090] The specific embodiments described above further elaborate on the object, technical solution and beneficial effects of the present invention. It should be understood that the above are only specific embodiments of the present invention and are not used to limit the present invention. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention shall be included within the protection scope of the present invention.

Claims

1. A method for co-incineration treatment of multi-source solid waste, characterized in that, The method includes: Feeding the water-containing gasified fly ash and the sludge conditioner into the inner tank of the integrated stirring device for mixing. The obtained breaker flows out of the inner tank and into the outer tank of the integrated stirring device, where it is mixed with the sludge entering the outer tank to obtain a mixed material. Among them, the main components of the water-containing gasified fly ash include water, coal ash, and partially unreacted carbon; Using a high-pressure mechanical pressure filtration device to dehydrate the mixed material to obtain a dehydrated material; Conveying the dehydrated material to the circulating fluidized bed incinerator of the circulating fluidized bed device to incinerate the sludge and the water-containing gasified fly ash by using the carbon contained in the water-containing gasified fly ash as fuel, generating slag and a gas-solid mixed material.

2. The method according to claim 1, wherein The water content of the water-containing gasified fly ash is 4%-95%, the water content of the sludge is more than 80%, and the water content of the dehydrated material is 30-50%; The sludge conditioner is selected from polyferric sulfate, and the concentration is 5-15wt%; Among them, when the water content of the water-containing gasified fly ash is 50-95%, the sludge conditioner is added in solid form. When the water content of the water-containing gasified fly ash is 4%-49%, the sludge conditioner is added in the form of a solution with a concentration of 5-15%.

3. The method according to claim 2, wherein The mass ratio of the water-containing gasified fly ash to the sludge is 1:5-2:1; The air-dried basis calorific value of the water-containing gasified fly ash is ≥3500 kcal / kg, and the air-dried basis calorific value of the sludge is ≥1600 kcal / kg.

4. The method according to claim 1, characterized in that, The high-pressure mechanical pressure filtration device is composed of multiple layers of thin filter cloths. The thickness of the mixed material between adjacent two layers of filter cloths is 1-3 cm, the pressure of pressure filtration is 20-28 MPa, the pressure filtration time is 20-50 min, and the thickness of the dehydrated material is 5-10 mm.

5. The method according to any one of claims 1-4, characterized in that The method further includes: The gas-solid mixed material is separated by a gas-solid separator to obtain high-temperature flue gas and solid materials. The solid materials include unreacted gasified fly ash and ash slag, and the solid materials are returned to the circulating fluidized bed incinerator through a return feeder; The high-temperature flue gas exchanges heat with normal-temperature air in an air preheater to obtain preheated air and medium-temperature flue gas. The preheated air participates in the incineration reaction in the circulating fluidized bed incinerator as an oxidant; Among them, the temperature in the circulating fluidized bed incinerator is 900-1100 °C, the temperature of the high-temperature flue gas is 850-1050 °C, the temperature of the preheated air is 450-600 °C, and the temperature of the medium-temperature flue gas is 500-650 °C.

6. The method according to claim 5, wherein The method further includes: The medium-temperature flue gas is used as a heat source to exchange heat with deaerated water in a waste heat boiler to obtain low-temperature flue gas and water vapor; The low-temperature flue gas is introduced into a flue gas purification unit for dust removal and purification; Among them, the temperature of the low-temperature flue gas is 180-250 °C.

7. A system for co-incineration treatment of multi-source solid waste, which is applicable to implementing the method described in any one of claims 1-6, and is characterized in that, The system includes: Integrated stirring device, comprising: an inner tank, an outer tank, and a stirring unit. The stirring unit includes a stirring motor fixed to the top of the outer tank, a stirring shaft controlled by the stirring motor and extending through the inner tank to the bottom of the outer tank, and a plurality of stirring blades provided on the stirring shaft. The inner tank is adapted to mix water-containing gasified fly ash and a sludge conditioner to obtain a wall-breaking agent. The outer tank is connected through an overflow port provided on the top side wall of the inner tank so that the wall-breaking agent is mixed with the sludge entering the outer tank to form a mixed material; High-pressure mechanical pressure filtration device, connected to a mixed material outlet provided at the bottom of the outer tank. The high-pressure mechanical pressure filtration device is composed of multiple layers of thin filter cloths to dehydrate the mixed material to obtain a dehydrated material; Circulating fluidized bed device, including a circulating fluidized bed incinerator. A raw material inlet communicating with a filter cake outlet of the high-pressure mechanical pressure filtration device is provided on the side wall of the circulating fluidized bed incinerator so as to feed the dehydrated material into the circulating fluidized bed incinerator to realize the incineration of the sludge and the water-containing gasified fly ash by using the carbon contained in the water-containing gasified fly ash, generating a gas-solid mixed material and slag.

8. The system according to claim 7, wherein The circulating fluidized bed incinerator is further provided with: a gas-solid mixed material outlet located at the top, a return port located in the dense phase zone, a slag discharge port and an oxidant inlet located at the bottom; The circulating fluidized bed device further includes: a gas-solid separator and a return feeder connected in sequence downstream of the gas-solid mixed material outlet; Wherein, the gas-solid separator is adapted to perform gas-solid separation on the gas-solid mixed material to obtain high-temperature flue gas and solid materials. The gas-solid separator is provided with a gas outlet for discharging the high-temperature flue gas and a solid outlet for discharging the solid materials; Return feeder, provided with a solid inlet connected to the solid outlet and a return outlet connected to the return port, and is adapted to return the solid materials to the circulating fluidized bed incinerator.

9. The system according to claim 8, wherein The system further includes: Air preheater, adapted to exchange heat between the high-temperature flue gas and normal-temperature air to obtain preheated air and medium-temperature flue gas. It is provided with a first flue gas inlet connected to the gas outlet for the high-temperature flue gas to enter, an air outlet connected to the oxidant inlet for discharging the preheated air, an air inlet for the normal-temperature air to enter, and a first flue gas outlet for discharging the medium-temperature flue gas; Optionally, it further includes: Waste heat boiler, located downstream of the air preheater, adapted to exchange heat between the medium-temperature flue gas and deaerated water to obtain low-temperature flue gas and steam. It is provided with a cold water inlet for deaerated water to enter, a second flue gas inlet connected to the first flue gas outlet, a steam outlet for discharging the steam, and a second flue gas outlet for discharging the low-temperature flue gas; Optionally, it further includes: Flue gas purification unit, connected to the second flue gas outlet, and adapted to perform dust removal and purification on the low-temperature flue gas.

10. The system according to claim 7, wherein The height of the circulating fluidized bed incinerator is h1, and the distance from the raw material inlet to the bottom of the circulating fluidized bed incinerator is 1 / 4h1 to 1 / 10h1.

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