CN112791554A - Flue gas treatment method and system - Google Patents
Flue gas treatment method and system Download PDFInfo
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- CN112791554A CN112791554A CN202011620564.7A CN202011620564A CN112791554A CN 112791554 A CN112791554 A CN 112791554A CN 202011620564 A CN202011620564 A CN 202011620564A CN 112791554 A CN112791554 A CN 112791554A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/005—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by heat treatment
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
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- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2257/302—Sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
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Abstract
The invention provides a flue gas treatment method and a flue gas treatment system. The flue gas treatment method comprises the following steps: A. burning the first sintering flue gas by using a fluidized bed combustion device, so that the temperature of fluidized bed exhaust gas discharged by the fluidized bed combustion device is more than or equal to 900 ℃; B. and mixing the gas discharged by the fluidized bed with a second part of sintering flue gas. The invention can be widely applied to the purification treatment of the flue gas in the industries of steel and iron and the like, and has the advantages of low cost, less emission and high efficiency.
Description
Technical Field
The invention relates to an environment-friendly technology, in particular to a flue gas harmless treatment technology.
Background
In many industrial production, flue gas discharged after combustion contains a large amount of pollutants, and needs to be subjected to harmless treatment and then dischargedOtherwise, the environment is seriously polluted. For example, steel production is a highly polluting industry, while the sintering process in steel production is an important source of pollution. The sintering flue gas generated by the sintering process contains a large amount of sulfur dioxide (SO)2) Nitrogen oxides, dioxins, and carbon monoxide (CO). Along with the increasing environmental protection requirement of the whole society, the harmless treatment of the sintering flue gas is increasingly urgent.
In order to reduce the pollution level of the sintering flue gas, a plurality of sintering flue gas treatment technologies are developed. For example, chinese patent application No. 201810331212.6 discloses a sintering flue gas purification system. The system introduces sintering flue gas as an oxidant and a fluidizing medium into a combustion device, and performs mixed combustion with fuel in the combustion device. The purposes of desulfurization and dioxin removal are realized in the combustion process.
The sintering flue gas purification system has certain problems. The combustion device needs a larger furnace chamber volume to process the sintering flue gas, and simultaneously needs more fuel to assist combustion, so that the equipment cost and the operation cost for processing the sintering flue gas are higher.
Disclosure of Invention
In order to reduce the cost required by purifying the sintering flue gas and improve the efficiency, the invention provides a sintering flue gas treatment method. The invention also provides a sintering flue gas treatment system for realizing the method.
The technical scheme of the invention is as follows.
A flue gas treatment method, wherein the flue gas comprises sintering flue gas, and comprises the following steps:
A. burning the first sintering flue gas by using a fluidized bed combustion device, so that the temperature of fluidized bed exhaust gas discharged by the fluidized bed combustion device is more than or equal to 900 ℃;
B. and mixing the gas discharged by the fluidized bed with a second part of sintering flue gas.
Optionally, the mixing of the fluidized bed exhaust gas and the second portion of sintering flue gas is performed in a separator of the fluidized bed combustion apparatus.
Optionally, the ratio of the volume ratio of the second portion of sintering flue gas to the first portion of sintering flue gas under the same condition is in a range of 1/9 to 1/4.
Optionally, the temperature of the fluidized bed exhaust gas after mixing with the second portion of sintering flue gas is greater than 850 ℃.
Optionally, the second portion of sintering flue gas is preheated to a minimum of 500 ℃ before the fluidized bed exhaust gas is mixed with the second portion of sintering flue gas.
A flue gas treatment system comprises a fluidized bed combustion device, a separator communicated with a discharge channel of the fluidized bed combustion device; the fluidized bed combustion device is provided with a hearth, the flue gas comprises sintering flue gas, a first sintering flue gas inlet channel communicated with the fluidized bed combustion device is arranged, and a second sintering flue gas inlet channel communicated with the gas inlet of the separator is also arranged; the temperature of the fluidized bed exhaust gas discharged from the fluidized bed combustion device and entering the separator is greater than or equal to 900 ℃.
Optionally, a primary air port is arranged at the bottom of the fluidized bed combustion device, and an air distribution plate is arranged at the bottom of the hearth of the fluidized bed combustion device; the primary air port is communicated with the first sintering flue gas inlet channel; a secondary air port is also arranged on the fluidized bed combustion device and is communicated with the first sintering flue gas inlet channel; the distance between the air distribution plate and the top of the hearth of the fluidized bed combustion device is H, and the secondary air port is arranged at a position which is far from the air distribution plate 1/6H to 1/5H.
Optionally, a plurality of secondary tuyeres are arranged around the hearth of the fluidized bed combustion device; the secondary air opening distance is the same as the size of the wind distribution plate.
Optionally, in unit time, the flow rate of the primary tuyere accounts for 35% -55% of the flow rate of the first sintering flue gas inlet channel.
Optionally, the flue gas treatment system is characterized in that: a flue gas preheater is also arranged; and preheating the gas in the first sintering flue gas inlet channel and the gas in the second sintering flue gas inlet channel by the flue gas preheater.
Optionally, the furnace of the fluidized bed combustion unit comprises an insulated furnace.
Optionally, the flue gas treatment system is further provided with a denitration device communicated with the separator; and the denitration device conveys the denitration material into the separator.
Optionally, a feed back port of the separator is communicated with the fluidized bed combustion device; and a desulfurizer feeding port is arranged on a communication channel between the feed back port of the separator and the fluidized bed combustion device.
The invention has the technical effects that:
according to the flue gas treatment method and system, the second part of sintering flue gas is mixed with the product (the fluidized bed exhaust gas) obtained after the first part of sintering flue gas is combusted and treated by the fluidized bed combustion device. Because the gas discharged by the fluidized bed has the characteristics of high temperature (more than or equal to 900 ℃) and high speed, the temperature after the gas is mixed with the second part of sintering flue gas can also exceed 850 ℃, and the dioxin in the second part of sintering flue gas can be effectively removed to burn carbon monoxide (CO). Meanwhile, desulfurizer such as calcium oxide (CaO) and the like is remained in the gas discharged from the fluidized bed, and sulfur dioxide (SO) in the second sintering flue gas can be effectively removed2). As can be seen from the above description, the second part of sintering flue gas can be mixed with the gas discharged from the fluidized bed to achieve harmless treatment, so that when treating the same amount of sintering flue gas, the total amount of sintering flue gas to be treated by the fluidized bed combustion device is reduced, and the volume of the fluidized bed combustion device can be reduced, thereby effectively reducing the construction cost and the fuel use cost of the fluidized bed combustion device, reducing the emission, improving the efficiency of treating sintering flue gas, and achieving the purpose of the present invention.
Further effects of the above alternatives will be described below in conjunction with the detailed description.
Drawings
FIG. 1 is a flow chart of an embodiment of a sintering flue gas treatment method of the present invention.
FIG. 2 is a schematic structural diagram of an embodiment of a sintering flue gas treatment system according to the present invention.
The designations in the figures illustrate the following:
201. a first sintering flue gas inlet channel; 202. a fluidized bed combustion unit; 203. a secondary tuyere; 204. a primary tuyere; 205. a wind distribution plate; 206. a desulfurizer feed port; 207. an air inlet; 208. a denitration device; 209. a second sintering flue gas inlet channel; 210. a separator; 211. a heated surface; 212. a flue gas preheater; 213. sintering flue gas enters the channel; 214. a desulfurization unit; 215. a dust remover; 216. a material returning pipeline.
Detailed Description
In the description of this section, the terms bottom, upper and lower have the expressions indicating orientation meaning relative orientation in the direction of gravity, unless otherwise specified.
The technical solution of the present invention will be described in detail below with reference to the accompanying drawings.
FIG. 1 shows one embodiment of a flue gas treatment process of the present invention. This example will be described in detail below.
Firstly, the sintering flue gas is divided into two parts: the first part of sintering flue gas and the second part of sintering flue gas. Under the same conditions, the ratio of the volume ratio of the second sintering flue gas to the first sintering flue gas ranges from 1/9 to 1/4. Or, 80-90% of the total amount of the sintering flue gas is divided into a first part of sintering flue gas; 10-20% of the total amount of the sintering flue gas is divided into a second portion of sintering flue gas.
Secondly, the first part of sintering flue gas is guided to enter a fluidized bed combustion device for combustion treatment, and the temperature of the fluidized bed exhaust gas discharged by the fluidized bed combustion device is larger than or equal to 900 ℃ through modes such as enhanced combustion, heat insulation treatment of a hearth of the fluidized bed combustion device and the like. Preheating the second part of sintering flue gas to over 500 ℃.
Thirdly, mixing the gas discharged by the fluidized bed combustion device after the first part of sintering flue gas is combusted (fluidized bed discharge gas) with the second part of sintering flue gas. Temperature after mixingGreater than 850 ℃. In the step, dioxin in the second part of sintering flue gas can be effectively removed, and carbon monoxide (CO) is combusted. Meanwhile, the residual calcium oxide (CaO) in the gas discharged from the fluidized bed can effectively remove sulfur dioxide (SO) in the second sintering flue gas2) And the aim of desulfurizing the second sintering flue gas is fulfilled. In the step, even when the gas discharged from the fluidized bed is mixed with the second sintering flue gas, the denitration treatment can be performed, so that the purpose of denitration of the second sintering flue gas is realized, and finally, the harmless treatment of the sintering flue gas is realized. Of course, the denitration treatment may be performed in a subsequent step.
FIG. 2 shows an embodiment of a flue gas treatment system implementing the flue gas treatment method of FIG. 1. The flue gas treatment system comprises a fluidized bed combustion unit 202, a separator 210, a heating surface 211, and a flue gas preheater 212. In this embodiment, the fluidized bed combustion apparatus 202 is a circulating fluidized bed combustion apparatus, and the hearth of the fluidized bed combustion apparatus 202 is an adiabatic hearth, and in this embodiment, the wall of the adiabatic hearth is made of an adiabatic material. The sintering flue gas inlet channel 213 is communicated with the flue gas preheater 212 and then branches into two channels: a first part sintering flue gas inlet channel 201 and a second part sintering flue gas inlet channel 209. Wherein, the first part sintering flue gas inlet channel 201 is further communicated with a primary tuyere 204 at the bottom of the fluidized bed combustion device 202 and a secondary tuyere 203 on the side wall of the fluidized bed combustion device 202. The air distribution plate 205 is arranged at the bottom of the fluidized bed combustion device 202, and if the air distribution plate 205 is at a distance H from the top of the hearth of the fluidized bed combustion device 202, the secondary air port 203 is arranged at a distance H from the air distribution plate 1/6. A plurality of secondary air ports 203 (not shown in the figure) are arranged around the hearth of the fluidized bed combustion device 202, and the plurality of secondary air ports 203 are uniformly distributed around the hearth. The distances between the plurality of secondary air ports 203 (namely all the secondary air ports 203) and the air distribution plate 205 are the same, namely, the arranged secondary air ports 203 are only distributed at the same height and are arranged in a single layer.
The second sintering flue gas inlet channel 209 is connected to the gas inlet 207 of the separator 210. The discharge channel of the fluidized bed combustion apparatus 202 is communicated with the gas inlet 207 of the separator 210, and a denitration apparatus 208(SNCR apparatus, hereinafter, referred to as Selective Non-Catalytic Reduction) is provided on the channel where the discharge channel of the fluidized bed combustion apparatus 202 is communicated with the gas inlet 207 of the separator 210, and the denitration apparatus 208 feeds the denitration material into the separator 210 through the gas inlet 207. The lower part of the separator 210 is provided with a feed back port (the lower end of the separator 210, not shown by a label in the figure), which is connected (communicated) with one end of the feed back pipe 216. The other end of the return pipe 216 is communicated with the fluidized bed combustion device. A desulfurizer feeding port 206 is provided on the return pipe 216. A separator discharge port is provided at an upper portion of the separator 210. The pipeline from the discharge port of the separator passes through the heating surface 211 and the flue gas preheater 212, and then is communicated with the desulfurizer 214 and the dust remover 215.
On the basis of the embodiment shown in fig. 2, the following second and third embodiments are derived.
The second embodiment differs from the embodiment shown in fig. 2 in that: if the air distribution plate 205 is at a distance H from the top of the hearth of the fluidized bed combustion apparatus 202, the secondary air port 203 is disposed at a distance H from the air distribution plate 9/50H.
The third embodiment differs from the embodiment shown in fig. 2 in that: if the air distribution plate 205 is at a distance H from the top of the hearth of the fluidized bed combustion apparatus 202, the secondary air port 203 is disposed at a distance H from the air distribution plate 1/5H.
The working process of the embodiment shown in fig. 2 is explained below to further illustrate the technical solution of the present invention. The black arrows in fig. 2 indicate the flow direction of the sintering fumes.
Firstly, the sintering flue gas to be treated enters along the sintering flue gas inlet channel 213 and is subjected to heat exchange by the flue gas preheater 212, so that the temperature of the sintering flue gas is raised to be higher than 500 ℃.
Second, the sintering flue gas preheated by the flue gas preheater 212 continues to flow along two paths: a first part sintering flue gas inlet channel 201 and a second part sintering flue gas inlet channel 209. 80% of the sintering flue gas enters the first sintering flue gas inlet channel 201, and 20% of the sintering flue gas enters the second sintering flue gas inlet channel 209. In other embodiments, the following two ways of distributing the sintering fumes are possible: 1. 85% of sintering flue gas enters the first sintering flue gas inlet channel 201, and 15% of sintering flue gas enters the second sintering flue gas inlet channel 209; 2. 90% of the sintering flue gas enters the first sintering flue gas inlet channel 201, and 10% of the sintering flue gas enters the second sintering flue gas inlet channel 209. The proportion of the sintering flue gas entering the first sintering flue gas inlet channel 201 and the second sintering flue gas inlet channel 209 can be adjusted by more prior art. As exemplified herein. A flow meter is arranged in the second sintering flue gas inlet channel 209 for flow monitoring, a movable flue gas baffle (equivalent to a flow valve for controlling the flow of sintering flue gas) is arranged in the second sintering flue gas inlet channel 209, and the movable flue gas baffle is timely adjusted according to the monitoring result of the flow meter. The process can be manually operated, and can also be realized by setting a control module to acquire the measurement data of the flowmeter and sending a control instruction to control the movement of the movable smoke baffle.
Thirdly, the sintering flue gas in the first sintering flue gas channel 201 (the first sintering flue gas) is further divided into two parts. A part of the air enters from a primary air port 204 at the bottom of the fluidized bed combustion device 202, passes through an air distribution plate 205 and then enters a hearth of the fluidized bed combustion device 202. The part of the sintering flue gas entering from the primary tuyere 204 is used as combustion improver and fluidizing medium, and the function of the part is to fluidize bed material in a dense-phase zone at the lower part of the hearth after passing through the air distribution plate 205 and provide oxygen for combustion reaction. The fuel required for combustion is fed from the lower part of the fluidized bed combustion device 202 above the air distribution plate 205 (the fuel inlet is not shown in the figure), and is subjected to anoxic combustion under the reducing atmosphere in the dense phase zone part. Another part of the sintering flue gas in the first part of the sintering flue gas channel 201 enters the hearth from the secondary tuyere 203. The secondary tuyere 203 is arranged in a single layer and has a small number, so that the speed of the sintering flue gas entering from the secondary tuyere 203 is increased under the condition that the total amount of the sintering flue gas entering the secondary tuyere 203 is not changed. At the position of the secondary tuyere 203, the hearth back pressure is low, so that the sintering flue gas entering from the secondary tuyere 203 can penetrate through the bed layer more easily and enter the center of the hearth. The sintering flue gas contains oxygen, and the oxygen in the sintering flue gas entering from the secondary tuyere 203 is beneficial to more fully burning and more fully consuming CO. Because the first part of sintering flue gas entering the hearth is preheated and the hearth is a heat-insulating hearth, the temperature in the hearth can be higher than 850 ℃, and the condition of decomposing dioxin is met. The amount of sintering fumes entering the primary tuyere 204 (e.g., the volume under the same conditions) is 35-55% of the amount of the first portion of sintering fumes. The proportion of the sintering flue gas entering the primary tuyere 204 is within a range, and the amount of the sintering flue gas entering the primary tuyere 204 in the embodiment accounts for 35% of the amount of the first sintering flue gas. In the other two embodiments, the amount of the sintering flue gas entering the primary tuyere 204 is 40% and 55% of the first portion of the sintering flue gas, respectively. By adjusting the ratio of the amount of the sintering flue gas entering the primary tuyere 204 to the amount of the sintering flue gas entering the secondary tuyere 203, the staged combustion of the fuel is realized, i.e., the fuel is subjected to anoxic combustion in a reducing atmosphere in a region below the secondary tuyere 203, so that the generation of nitrogen oxides is reduced. The secondary tuyere 203 is arranged at a higher position, so that the area of anoxic combustion is larger, and the generation of nitrogen oxides is more effectively reduced. The adjustment of the ratio between the amount of the sintering flue gas entering the primary tuyere 204 and the amount of the sintering flue gas entering the secondary tuyere 203 can be performed according to the properties of the fuel. For example, if the fuel is a highly volatile fuel, the proportion of sintering fumes entering the primary tuyere 204 should be small; if the fuel is a low volatility fuel, the proportion of sintering fumes entering the primary tuyere 204 should be greater.
Fourth, the gas (fluidized bed exhaust gas) generated after the combustion in the fluidized bed combustion apparatus 202 enters the separator 210 through the exhaust passage of the fluidized bed combustion apparatus 202. Because the hearth of the fluidized bed combustion device 202 is an adiabatic hearth, the temperature of the fluidized bed exhaust gas is greater than or equal to 900 ℃.
Fifth, the preheated sintering flue gas (second sintering flue gas) in the second sintering flue gas inlet channel 209 enters the separator 210. Due to the second sintering flue gas, the gas flow speed in the inlet flue 207 of the separator 210 is greatly increased and can be increased from the conventional 20-22m/s to 27-29m/s, so that the separation efficiency and the heat and mass transfer rate of the separator 210 are further improved. Meanwhile, the addition of the second sintering flue gas also produces the following effects:
1. the preheated second sintering flue gas is mixed with the fluidized bed exhaust gas (the temperature is more than or equal to 900 ℃) so that the temperature in the separator 210 is higher than 850 ℃, namely higher than the decomposition temperature of dioxin. This allows the dioxin in the second sintering flue gas to be removed.
2. And the residual CO in the gas discharged by the fluidized bed is further reacted with the oxygen in the second sintering flue gas under the high-temperature condition, so that the CO is fully consumed.
3. And the residual calcium oxide in the gas discharged by the fluidized bed can react with sulfur dioxide and oxygen in the second sintering flue gas to desulfurize the second sintering flue gas.
Sixthly, the denitration device 208 is communicated with the separator 210, urea solution or ammonia solution and other denitration materials are sprayed into the separator 201, and the fluidized bed exhaust gas and the second sintering flue gas are subjected to denitration in the separator 201.
Seventhly, limestone added through the desulfurizer feeding port 206 on the return pipe 216 is mixed with the circulating material separated by the separator 210 in the return pipe 216, and before entering the fluidized bed combustion device 202, part of the limestone can be subjected to a calcination reaction to generate calcium oxide, so that after entering the hearth, the newly generated calcium oxide can directly enter the combustion zone for a desulfurization reaction, and the desulfurization efficiency is improved.
Eighth, the gas discharged from above the separator 210 is heat-exchanged at a heated surface (e.g., an evaporation heated surface, a superheater, a reheater, an economizer, etc.), so that the waste heat is effectively utilized. And then preheated by the flue gas preheater 212.
Ninth, the gas passing through the flue gas preheater 212 (the gas obtained by preheating the sintering flue gas) enters the desulfurization device 214, and sulfur dioxide in the gas is continuously removed by a semi-dry method. Then, the desulfurized gas is introduced into the dust collector 215 to be subjected to deep dust collection, and the fly ash is captured and simultaneously the dioxin remaining in the gas is removed. To this end, an operation of the embodiment shown in fig. 2 is completed.
As can be seen from the above description of the process, the method and the system for treating sintering flue gas of the present invention can reduce the total amount of sintering flue gas to be treated by the fluidized bed combustion apparatus and the volume of the fluidized bed combustion apparatus, when treating the same amount of sintering flue gas, thereby effectively reducing the construction cost and the fuel use cost of the fluidized bed combustion apparatus, reducing the emission, and simultaneously improving the efficiency of treating sintering flue gas.
It should be noted that the above-mentioned embodiments are only preferred embodiments of the present invention, and do not limit the scope of the present invention, and the present invention may be replaced by other equivalent techniques. Therefore, all equivalent changes, direct or indirect applications, made by using the description and drawings of the present invention, or other related technical fields are all included in the scope of the present invention.
Claims (13)
1. A flue gas treatment method is characterized in that the flue gas comprises sintering flue gas, and the method comprises the following steps: the method comprises the following steps:
A. burning the first sintering flue gas by using a fluidized bed combustion device, so that the temperature of fluidized bed exhaust gas discharged by the fluidized bed combustion device is more than or equal to 900 ℃;
B. and mixing the gas discharged by the fluidized bed with a second part of sintering flue gas.
2. The flue gas treatment method according to claim 1, wherein: the fluidized bed exhaust gas and the second sintering flue gas are mixed in a separator of the fluidized bed combustion device.
3. The flue gas treatment method according to claim 1, wherein: the ratio of the volume ratio of the second part of sintering flue gas to the first part of sintering flue gas under the same conditions ranges from 1/9 to 1/4.
4. The flue gas treatment method according to claim 1, wherein: the temperature of the mixture of the fluidized bed exhaust gas and the second sintering flue gas is more than 850 ℃.
5. The flue gas treatment method according to claim 1, wherein: the second portion of sintering flue gas is preheated to a minimum of 500 ℃ before the fluidized bed exhaust gas is mixed with the second portion of sintering flue gas.
6. A flue gas treatment system comprises a fluidized bed combustion device, a separator communicated with a discharge channel of the fluidized bed combustion device; fluidized bed combustion apparatus is provided with furnace, the flue gas includes sintering flue gas, its characterized in that: a first part of sintering flue gas inlet channel communicated with the fluidized bed combustion device is arranged, and a second part of sintering flue gas inlet channel communicated with the gas inlet of the separator is also arranged; the temperature of the fluidized bed exhaust gas discharged from the fluidized bed combustion device and entering the separator is greater than or equal to 900 ℃.
7. The flue gas treatment system of claim 6, wherein: a primary air port is arranged at the bottom of the fluidized bed combustion device, and an air distribution plate is arranged at the bottom of the hearth of the fluidized bed combustion device; the primary air port is communicated with the first sintering flue gas inlet channel; a secondary air port is also arranged on the fluidized bed combustion device and is communicated with the first sintering flue gas inlet channel; the distance between the air distribution plate and the top of the hearth of the fluidized bed combustion device is H, and the secondary air port is arranged at a position which is far from the air distribution plate 1/6H to 1/5H.
8. The flue gas treatment system of claim 7, wherein: a plurality of secondary air ports are arranged around the hearth of the fluidized bed combustion device; the secondary air opening distance is the same as the size of the wind distribution plate.
9. The flue gas treatment system of claim 7, wherein: in unit time, the flow of the primary air port accounts for 35% -55% of the flow of the first sintering flue gas inlet channel.
10. The flue gas treatment system of claim 6, wherein: a flue gas preheater is also arranged; and preheating the gas in the first sintering flue gas inlet channel and the gas in the second sintering flue gas inlet channel by the flue gas preheater.
11. The flue gas treatment system of claim 6, wherein: the furnace of the fluidized bed combustion unit comprises an insulated furnace.
12. The flue gas treatment system of claim 6, wherein: a denitration device communicated with the separator is also arranged; and the denitration device conveys the denitration material into the separator.
13. The flue gas treatment system of claim 6, wherein: the feed back port of the separator is communicated with the fluidized bed combustion device; and a desulfurizer feeding port is arranged on a communication channel between the feed back port of the separator and the fluidized bed combustion device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011620564.7A CN112791554A (en) | 2020-12-31 | 2020-12-31 | Flue gas treatment method and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202011620564.7A CN112791554A (en) | 2020-12-31 | 2020-12-31 | Flue gas treatment method and system |
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