A sulfite dry desulfurization and denitration integrated system

Abstract

The present application relates to a kind of ammonium sulfite dry desulfurization and denitrification integrated system, including reaction tower, ammonium sulfate removal device, cooling cooler, ammonium sulfite particle trapping device and ammonium sulfite separation and precipitation system and drying system, the flue gas outlet of reaction tower is connected by pipeline the flue gas import of ammonium sulfate removal device, the flue gas outlet of ammonium sulfate removal device is connected by pipeline the import of cooling cooler, the import of cooling cooler is connected the import of ammonium sulfite particle trapping device, the condensate outlet of cooling cooler and the ammonium bisulfite discharge port of ammonium sulfite particle trapping device are respectively connected by pipeline the import of ammonium sulfite separation and precipitation system, the bottom of reaction tower is equipped with raw material inlet.Advantages: using ammonium sulfite and ammonia as raw material, not only can realize the efficient collaborative removal of sulfur dioxide and nitrogen oxides, reaction raw material ammonium sulfite can be recycled and reused, reduce the cost of reaction material.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of flue gas treatment equipment, in particular to a sulfite ammonium dry desulfurization and denitrification integrated system. BACKGROUND

[0002] Flue gas desulfurization and denitrification treatment refers to removing SO2 and NOx in flue gas, because these two gaseous pollutants will form acid rain after entering the atmosphere, which has a great impact on the natural environment and human living environment.

[0003] At present, there are mature technologies for separate desulfurization and denitrification in the industry, such as limestone-gypsum desulfurization, SCR, SNCR denitrification, etc., but these technologies also have some shortcomings, such as high wastewater treatment cost and difficult disposal of by-product gypsum for limestone-gypsum method, catalyst plugging, poisoning and failure for SCR, and ammonia injection point limited by furnace and heating surface arrangement for SNCR due to reaction temperature window. These problems have not been perfectly solved, and two sets of equipment are separately arranged for desulfurization and denitrification, which not only occupies a large area, but also has high investment, management and operation cost. Therefore, the industry is seeking new processes for simultaneous flue gas desulfurization and denitrification technology, and these processes are basically in the research and development stage. The sulfite ammonium desulfurization and denitrification integrated technology developed by Beijing Qingxin Environmental Technology Co., Ltd. mainly uses sulfite ammonium and liquid ammonia (ammonia water) as raw materials, which can realize the functions of desulfurization and denitrification in one system. However, sulfite ammonium is easy to decompose under heat, which leads to large material loss.

[0004] Therefore, it is necessary to develop a sulfite ammonium dry desulfurization and denitrification integrated system to solve the above technical problems. SUMMARY

[0005] The technical problem to be solved by the present application is to provide a sulfite ammonium dry desulfurization and denitrification integrated system, which effectively overcomes the defects of the prior art.

[0006] The technical solution of the present application to solve the above technical problems is as follows:

[0007] An integrated ammonium sulfite dry desulfurization and denitrification system comprises a reaction tower, an ammonium sulfate removal device, a cooling cooler, an ammonium sulfite particle capture device, an ammonium sulfite separation and precipitation system, and a drying system. The flue gas outlet of the reaction tower is connected to the flue gas inlet of the ammonium sulfate removal device via a pipeline, the flue gas outlet of the ammonium sulfate removal device is connected to the inlet of the cooling cooler via a pipeline, the outlet of the cooling cooler is connected to the inlet of the ammonium sulfite particle capture device, the outlet of the ammonium sulfite particle capture device is connected to a smoke exhaust pipeline, the condensate outlet of the cooling cooler and the ammonium bisulfite discharge outlet of the ammonium sulfite particle capture device are respectively connected to the inlet of the ammonium sulfite separation and precipitation system via pipelines, the ammonium sulfite separation and precipitation system is used to precipitate ammonium sulfite crystals, the drying and grinding system is used to dry the ammonium sulfite crystals and grind them into loose powder, and a raw material inlet is provided at the bottom of the reaction tower.

[0008] On the basis of the above technical solution, the present invention can also be improved as follows.

[0009] Furthermore, the ammonium sulfate removal device is a bag dust collector, and the lower end ash outlet of the bag dust collector is connected to an ammonium sulfate storage bin.

[0010] Furthermore, the above-mentioned ammonium sulfite particle collection device is a wet electrostatic precipitator, and its liquid phase outlet constitutes its ammonium bisulfite discharge outlet.

[0011] Furthermore, the ammonium sulfite separation and precipitation system includes a liquid collecting tank, a low-temperature evaporator, a cooling crystallizer and a filtering device connected in sequence through pipelines. The liquid collecting tank is provided with a liquid inlet, which constitutes the inlet of the ammonium sulfite separation and precipitation system.

[0012] Furthermore, an ammonia adding pipeline with a valve is provided at the bottom of the liquid collecting tank, and the ammonia adding pipeline is connected to an ammonia source.

[0013] Furthermore, the filtering device is a vacuum belt or plate and frame filter press.

[0014] Furthermore, the above-mentioned drying system includes an anaerobic drying device and a grinding device. The discharge end of the above-mentioned anaerobic drying device is connected to the feed end of the above-mentioned grinding device through a material feeding device. The discharge end of the above-mentioned grinding device is connected to the ammonium sulfite storage bin. The above-mentioned ammonium sulfite storage bin is provided with a discharge port, and the above-mentioned discharge port is connected to the raw material inlet of the above-mentioned reaction tower through a loader.

[0015] Furthermore, the above-mentioned oxygen-free drying device is an oxygen-free drying machine.

[0016] The beneficial effects of the present invention are: using ammonium sulfite and ammonia as raw materials, not only can efficient synergistic removal of sulfur dioxide and nitrogen oxides be achieved, but the reaction raw material ammonium sulfite can be recycled and reused, greatly reducing the cost of reaction materials. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 It is a structural schematic diagram of the integrated system for dry desulfurization and denitrification using ammonium sulfite according to the present invention.

[0018] In the accompanying drawings, the components represented by the reference numerals are as follows:

[0019] 1. Reaction tower; 2. Ammonium sulfate removal device; 3. Cooling cooler; 4. Ammonium sulfite particle collection device; 6. Liquid ammonia storage tank; 21. Ammonium sulfate storage silo; 51. Liquid collecting tank; 52. Low-temperature evaporator; 53. Cooling crystallizer; 54. Filtering device; 55. Anaerobic drying device; 56. Grinding device; 57. Ammonium sulfite storage silo; 58. Loading machine. DETAILED DESCRIPTION

[0020] The principles and features of the present invention are described below with reference to the accompanying drawings. The examples given are only used to explain the present invention and are not used to limit the scope of the present invention.

[0021] Example: Figure 1 As shown, the integrated system for dry desulfurization and denitrification of ammonium sulfite in this embodiment includes a reaction tower 1, an ammonium sulfate removal device 2, a cooling cooler 3, an ammonium sulfite particle capture device 4, and an ammonium sulfite separation and precipitation system and a drying system. The flue gas outlet of the above-mentioned reaction tower 1 is connected to the flue gas inlet of the above-mentioned ammonium sulfate removal device 2 through a pipeline, the flue gas outlet of the above-mentioned ammonium sulfate removal device 2 is connected to the inlet of the above-mentioned cooling cooler 3 through a pipeline, the outlet of the above-mentioned cooling cooler 3 is connected to the inlet of the above-mentioned ammonium sulfite particle capture device 4, the outlet of the above-mentioned ammonium sulfite particle capture device 4 is connected to the exhaust pipeline, the condensate outlet of the above-mentioned cooling cooler 3 and the ammonium bisulfite discharge port of the above-mentioned ammonium sulfite particle capture device 4 are respectively connected to the inlet of the above-mentioned ammonium sulfite separation and precipitation system through pipelines, the above-mentioned ammonium sulfite separation and precipitation system is used to precipitate ammonium sulfite crystals, the above-mentioned drying and grinding system is used to dry the above-mentioned ammonium sulfite crystals and grind them into loose powder, and a raw material inlet is provided at the bottom of the above-mentioned reaction tower 1.

[0022] The ammonium sulfite dry desulfurization and denitrification integrated system of this embodiment is applicable to the treatment of flue gas emissions from coal-fired boilers, steelmaking, aluminum smelting, ships, and other chemical and non-electrical plants. The specific treatment process is as follows:

[0023] The original flue gas enters from the lower part of the reaction tower 1. The SO2 and NOx in the flue gas first react with the ammonium sulfite (ammonium sulfite powder obtained by the drying and grinding system) and NH3 (ammonia gas additionally introduced into the reaction tower 1) input into the system to generate ammonium sulfite, ammonium bisulfite, ammonium sulfate and nitrogen respectively. The reaction equations are as follows:

[0024] 1) SO2 reacts with NH3 to produce (NH4)2SO4. The reaction equation is as follows:

[0025] SO2+2NH3+H2O=(NH4)2SO3

[0026] 2) (NH4)2SO3 further reacts with SO2:

[0027] (NH4)2SO3+SO2+H2O=2(NH4)HSO3

[0028] 3) Part of (NH4)2SO3 is oxidized by O2 in the flue gas:

[0029] 2(NH4)2SO3+O2=2(NH4)2SO4

[0030] 4) Part of (NH4)HSO3 is oxidized by O2 in the flue gas:

[0031] 2NH4HSO3+O2=2NH4HSO4

[0032] The denitrification part uses ammonium sulfite to react with NOx to generate N2. The reaction is designed in the following reaction stages:

[0033] 1) NO is oxidized to NO2 by O2 in the flue gas

[0034] 2NO+O2=2NO2

[0035] 3)(NH4)2SO3 reacts with NO in the presence of a catalyst to produce N2

[0036] 2(NH4)2SO3+2NO=(NH4)2SO4+N2

[0037] 4) (NH4) 2SO3 reacts with NO2 in the presence of a catalyst to produce N2

[0038] 4(NH4)2SO3+2NO2=4(NH4)2SO4+N2

[0039] 5) (NH4)2SO3 high temperature decomposition

[0040] (NH4)2SO3.H2SO=2NH3+SO2S+H2SO

[0041] In addition, since the temperature in the reaction tower 1 is generally higher than the decomposition temperature of ammonium sulfite, part of the ammonium sulfite directly decomposes into SO2 and NH3 and mixes into the flue gas. The mixed flue gas from the reaction tower 1 then enters the ammonium sulfate removal device 2, and the flue gas can still meet the denitration condition in the ammonium sulfate removal device 2, and the denitration continues to proceed, and since the ammonium sulfate removal device 2 intercepts part of the undecomposed ammonium sulfite material, and contacts the flue gas passing through it, the ammonium sulfite intercepted in the ammonium sulfate removal device 2 has a very high denitration efficiency. The particulate matter finally collected by the ammonium sulfate removal device 2 is mainly the product (ammonium sulfate) of complete reaction, which can be used as an economic byproduct for other industrial purposes. The flue gas from the ammonium sulfate removal device 2 generally achieves the predetermined removal efficiency of NOx, and still has a large amount of SO2 and NH3 mixed in the flue gas. From the reaction principle, the reaction of SO2 and NH3 is extremely easy to proceed, but the reaction temperature cannot be higher than 70°C, otherwise the generated ammonium sulfite directly decomposes into SO2 and NH3, which is equivalent to the reaction not being able to proceed. Therefore, the flue gas from the ammonium sulfate removal device 2 is cooled by the cooling cooler 3 to reduce the temperature to below 60°C, and SO2 and NH3 can rapidly react to generate ammonium sulfite (when SO2 is excessive, part of ammonium bisulfite will also be generated, which exists in the flue gas in the form of fine particles). In addition, since the flue gas is cooled, the cooling cooler 3 will have condensed water precipitated, and this part of the condensed water often dissolves a large amount of ammonium sulfite and ammonium bisulfite, so it needs to be collected to the ammonium sulfite separation and precipitation system for processing and recycling. Specifically, ammonium sulfite crystals are separated from the ammonium sulfite separation and precipitation system, and then the ammonium sulfite crystals are dried in a drying system and ground into loose powder, and then the powder (ammonium sulfite) is used as raw material and sent into the inside of the reaction tower 1 through the raw material inlet.

[0042] Specifically, the low-temperature flue gas from the cooling cooler 3 carries a large amount of ammonium sulfite particles and a small amount of ammonium bisulfite, which can be adsorbed and transported to the ammonium sulfite separation and precipitation system for collection and recycling when passing through the ammonium sulfite particle trapping device 4. At this time, SO2, NOx in the flue gas, and ammonium sulfite particles re-generated by material decomposition are all removed, and the exhaust gas at the outlet of the ammonium sulfite particle trapping device 4 generally meets the predetermined emission requirements.

[0043] It should be noted that since the reaction tower 1 needs to ensure that the gas-solid mixture in the tower is uniform, the ammonium sulfite material is preferably blown into the reaction tower 1 by pneumatic conveying. The temperature in the reaction tower 1 needs to be controlled between 60-110°C, otherwise the reaction cannot proceed if the temperature is too low, and the reaction efficiency is low if the temperature is too high.

[0044] In this embodiment, the ammonium sulfate removal device 2 utilizes a conventional bag filter. The specific model can be flexibly and reasonably selected based on actual usage requirements. The lower ash outlet of the bag filter is connected to an ammonium sulfate storage bin 21. During operation, the internal temperature of the bag filter must be maintained above 60°C. This prevents bag sticking due to condensation and also allows the bag filter's large surface area to serve as a secondary site for desulfurization and denitrification reactions.

[0045] Of course, the ammonium sulfate removal device 2 of this embodiment can also be replaced by a dust collector with filtering properties such as a ceramic filter tube dust collector and a plastic sintered plate dust collector, and the use of an electrostatic precipitator and a cyclone dust collector should be avoided as much as possible.

[0046] The ammonium sulfite particle collection device 4 is a wet electrostatic precipitator, and its liquid phase outlet constitutes its ammonium bisulfite discharge outlet.

[0047] As a preferred embodiment, the ammonium sulfite separation and precipitation system includes a liquid collecting tank 51, a low-temperature evaporator 52, a cooling crystallizer 53 and a filter device 54 connected in sequence by pipelines. The liquid collecting tank 51 is provided with a liquid inlet, which constitutes the inlet of the ammonium sulfite separation and precipitation system.

[0048] In the above embodiment, the ammonium sulfite-rich liquid collected by the cooling cooler 3 and the ammonium sulfite particle capture device 4 (i.e., a wet electrostatic precipitator) is stored in a liquid collection tank 51. When the liquid level in the liquid collection tank 51 reaches a high level, the subsequent processing units are activated. First, the liquid in the liquid collection tank 51 enters the low-temperature evaporator 52 (enters the shell side of the low-temperature evaporator 52). Under vacuum, the interior of the low-temperature evaporator 52 begins to boil at 50-70°C (generally, the vacuum level of the low-temperature evaporator 52 needs to be controlled between 75 kPa and 88 kPa to maintain the internal boiling temperature between 50-70°C), thereby concentrating the ammonium sulfite liquid. Subsequently, this portion of the relatively high-temperature concentrated liquid enters the cooling crystallizer 53 (a device belonging to the prior art, which causes the saturated solution to precipitate crystals by cooling (specifically, the saturated liquid or supersaturated mixed liquid above 50°C from the low-temperature evaporator 52 is cooled to reduce the solubility of ammonium sulfite, thereby allowing more ammonium sulfite to precipitate in the form of crystals). The specific model is flexibly and reasonably selected according to actual use requirements). The temperature reduction causes the solubility of ammonium sulfite to decrease, and ammonium sulfite precipitates in the form of crystals. The slurry is then filtered and dehydrated through the filtration device 54. The filtrate obtained after dehydration is sent to the drying system for drying and grinding, and the filtered liquid is sent back to the low-temperature evaporator 52.

[0049] It should be noted that due to the cooling of the flue gas, condensed water will be precipitated on the coil surface of the cooling cooler 3. This condensed water often dissolves a large amount of ammonium sulfite and ammonium bisulfite, so it needs to be collected in the subsequent collecting tank 51 for processing and reuse.

[0050] In this embodiment, the liquid collecting tank 51 is preferably designed to have a volume that can collect 4 hours or more of collected liquid, so as to avoid continuous low load operation or frequent intermittent start-stop of the subsequent processing unit.

[0051] As a preferred embodiment, the bottom of the liquid collecting tank 51 is provided with an ammonia feeding pipe with a valve, which is connected to an ammonia source.

[0052] In the above embodiment, when the proportion of ammonium bisulfite in the solution ions is more than 10% (which can be set by oneself), ammonia gas can be introduced through the ammonia feeding pipe at the bottom of the liquid collecting tank 51, and the ammonia gas will react with the ammonium bisulfite to form ammonium sulfite.

[0053] In this embodiment, the filter device 54 uses a vacuum belt or plate-and-frame filter press of existing technology, and the specific model can be flexibly and reasonably selected according to actual use requirements. The obtained filtrate is sent back to the low-temperature evaporator 52 through a pipeline, and the filtered cake enters the subsequent drying system.

[0054] As a preferred embodiment, the drying system includes an oxygen-free drying device 55 and a grinding device 56, the discharge end of the oxygen-free drying device 55 is connected to the feed end of the grinding device 56 through a material feeding device, the discharge end of the grinding device 56 is connected to an ammonium sulfite storage bin 57, the ammonium sulfite storage bin 57 is provided with a discharge port, and the discharge port is connected to the raw material inlet of the reaction tower 1 through a feeding machine 58.

[0055] In the above embodiment, the ammonium sulfite crystals are sent to the oxygen-free drying device 55 for drying, and then sent to the grinding device 56 for grinding into loose powder and stored in the ammonium sulfite storage bin 57, and when needed, the ammonium sulfite powder in the ammonium sulfite storage bin 57 is sent to the reaction tower 1 through the feeding machine 58 (which can be continuous feeding or intermittent feeding of ammonium sulfite powder), so that the complete process of drying, grinding and feeding of the crystals can be realized.

[0056] It should be emphasized that in the case of high SO2 content in flue gas, the ammonium sulfite generated by inputting ammonia is sufficient to support the amount of ammonium sulfite required for denitrification, and even has a surplus, so it is necessary to supplement part of the ammonium sulfite material in the ammonium sulfite storage bin 57 or output part of the high-value by-product of ammonium sulfite according to different flue gas conditions.

[0057] In the embodiment, the oxygen-free drying device 55 adopts an oxygen-free drying machine of the prior art, and the specific model can be selected flexibly and reasonably according to actual use requirements. The oxygen-free drying machine is used to dry the filtered ammonium sulfite crystals, and the drying is performed in an oxygen-free environment below 60 DEG C, so that decomposition of the ammonium sulfite is avoided, and oxidation of the ammonium sulfite by oxygen in the air is also avoided. The oxygen-free drying machine does not need to dry the material to a completely water-free state, but only needs to ensure that the attached water of the material is less than 5%, and the material is in a loose and non-bulky state.

[0058] In the embodiment, the grinding device 56 can adopt an existing Raymond mill or a fan mill or other existing powder grinding equipment suitable for the properties of ammonium sulfite, and the specific model can be selected flexibly and reasonably according to actual use requirements. Meanwhile, the feeding machine 58 can adopt a suction feeding machine to suction and feed the ammonium sulfite powder in the ammonium sulfite storage bin 57 to the reaction tower 1.

[0059] The liquid ammonia storage tank 6 is further included, which is connected to the inside of the reaction tower 1 through a pipeline, so as to conveniently deliver ammonia gas raw material to the reaction tower 1.

[0060] In the description of the present application, it should be understood that the terms "center", "longitudinal", "transverse", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential" and the like indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present application and simplifying the description, and do not indicate or imply that the devices or elements indicated must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as a limitation on the present application.

[0061] In addition, the terms "first" and "second" are only for descriptive purposes, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined with "first" and "second" can explicitly or implicitly include at least one of the features. In the description of the present application, the meaning of "a plurality of" is at least two, such as two, three, etc., unless otherwise specifically limited.

[0062] In the present invention, unless otherwise specified or limited, the terms "installed," "connected," "connect," "fixed," etc. should be understood in a broad sense. For example, they can refer to fixed connection, detachable connection, or integration; mechanical connection, electrical connection; direct connection, or indirect connection through an intermediate medium; internal communication between two components, or interaction between two components, unless otherwise specified. Those skilled in the art will understand the specific meanings of the above terms in the present invention based on specific circumstances.

[0063] In the present invention, unless otherwise expressly specified or limited, when a first feature is "above" or "below" a second feature, it may mean that the first and second features are in direct contact, or that the first and second features are in indirect contact through an intermediary. Furthermore, when a first feature is "above," "above," or "above" a second feature, it may mean that the first feature is directly above or diagonally above the second feature, or simply means that the first feature is at a higher level than the second feature. When a first feature is "below," "below," or "below" a second feature, it may mean that the first feature is directly below or diagonally below the second feature, or simply means that the first feature is at a lower level than the second feature.

[0064] In the description of this specification, the reference terms "one embodiment", "some embodiments", "example", "specific example", or "some examples" mean that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described can be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art can combine and combine different embodiments or examples described in this specification and features of different embodiments or examples without contradiction.

[0065] Although the embodiments of the present invention have been shown and described above, it will be understood that the above embodiments are illustrative and are not to be construed as limitations on the present invention. A person skilled in the art may change, modify, replace and modify the above embodiments within the scope of the present invention.

Claims

1. An integrated system for dry desulfurization and denitrification using ammonium sulfite, characterized by: The invention comprises a reaction tower (1), an ammonium sulfate removal device (2), a cooling cooler (3), an ammonium sulfite particle capture device (4), an ammonium sulfite separation and precipitation system and a drying system. The flue gas outlet of the reaction tower (1) is connected to the flue gas inlet of the ammonium sulfate removal device (2) through a pipeline, the flue gas outlet of the ammonium sulfate removal device (2) is connected to the inlet of the cooling cooler (3) through a pipeline, the outlet of the cooling cooler (3) is connected to the inlet of the ammonium sulfite particle capture device (4), the outlet of the ammonium sulfite particle capture device (4) is connected to a smoke exhaust pipeline, the condensate outlet of the cooling cooler (3) and the ammonium bisulfite discharge port of the ammonium sulfite particle capture device (4) are respectively connected to the inlet of the ammonium sulfite separation and precipitation system through pipelines, the ammonium sulfite separation and precipitation system is used to precipitate ammonium sulfite crystals, the drying and grinding system is used to dry the ammonium sulfite crystals and grind them into loose powder, and a raw material inlet is provided at the bottom of the reaction tower (1).

2. The integrated system for dry desulfurization and denitrification using ammonium sulfite according to claim 1, characterized in that: The ammonium sulfate removal device (2) is a bag dust collector, and the lower end ash outlet of the bag dust collector is connected to an ammonium sulfate storage bin (21).

3. The integrated system for dry desulfurization and denitrification using ammonium sulfite according to claim 1, characterized in that: The ammonium sulfite particle capturing device (4) is a wet electrostatic precipitator, and its liquid phase outlet constitutes its ammonium bisulfite discharge outlet.

4. The integrated system for dry desulfurization and denitrification using ammonium sulfite according to claim 1, characterized in that: The ammonium sulfite separation and precipitation system comprises a liquid collecting tank (51), a low-temperature evaporator (52), a cooling crystallizer (53) and a filtering device (54) which are sequentially connected through pipelines. The liquid collecting tank (51) is provided with a liquid inlet, which constitutes the inlet of the ammonium sulfite separation and precipitation system.

5. The integrated system for dry desulfurization and denitrification using ammonium sulfite according to claim 4, characterized in that: An ammonia adding pipeline with a valve is provided at the bottom of the liquid collecting tank (51), and the ammonia adding pipeline is connected to an ammonia source.

6. The integrated system for dry desulfurization and denitrification using ammonium sulfite according to claim 4, characterized in that: The filtering device (54) is a vacuum belt or plate and frame filter press.

7. The integrated system for dry desulfurization and denitrification using ammonium sulfite according to any one of claims 1 to 6, characterized in that: The drying system comprises an anaerobic drying device (55) and a grinding device (56), wherein the discharge end of the anaerobic drying device (55) is connected to the feed end of the grinding device (56) via a material feeding device, and the discharge end of the grinding device (56) is connected to an ammonium sulfite storage bin (57), and the ammonium sulfite storage bin (57) is provided with a discharge port, and the discharge port is connected to the raw material inlet of the reaction tower (1) via a feeder (58).

8. The integrated system for dry desulfurization and denitrification using ammonium sulfite according to claim 7, characterized in that: The oxygen-free drying device (55) is an oxygen-free drying machine.

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