CN213408210U - Flue gas treatment system based on calcium-based absorbent - Google Patents
Flue gas treatment system based on calcium-based absorbent Download PDFInfo
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- CN213408210U CN213408210U CN202022020767.4U CN202022020767U CN213408210U CN 213408210 U CN213408210 U CN 213408210U CN 202022020767 U CN202022020767 U CN 202022020767U CN 213408210 U CN213408210 U CN 213408210U
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Abstract
The utility model discloses a flue gas processing system based on calcium-based absorbent. The flue gas treatment system comprises calcium-based absorbent supply equipment, chlorine dioxide supply equipment, pre-dedusting equipment, a moving bed absorption tower and a flue; the calcium-based absorbent supply equipment comprises a calcium oxide storage tank, a fly ash storage tank, a bentonite storage tank, a process water storage tank, a kneading machine, a granulating machine and a drying machine; the calcium oxide storage tank, the fly ash storage tank, the bentonite storage tank and the process water storage tank are respectively connected with a kneading machine, and the kneading machine, the granulator and the dryer are sequentially connected; the pre-dedusting equipment is connected with the flue; the flue is connected with the chlorine dioxide supply equipment; and the flue and the dryer are respectively connected with the moving bed absorption tower. The utility model discloses a flue gas processing system can reduce equipment investment running cost, and the absorbent is easily recycle.
Description
Technical Field
The utility model relates to a flue gas processing system based on calcium-based absorbent.
Background
Sulfur dioxide and nitrogen oxides are the main components of acid rain, which is one of the major environmental problems in the world today. Boilers, hot blast furnaces, coal-fired thermal power plants and the like are main emission bodies of sulfur dioxide and nitrogen oxides. In order to reduce the emission of harmful substances such as sulfur dioxide, nitrogen oxide and the like, a boiler, a hot blast stove, a coal-fired thermal power plant and the like need to be provided with a matched flue gas treatment system to treat polluted atmosphere.
The moving bed desulfurization technology generally uses active coke as an adsorbent. The desulfurization and denitrification of the active coke can be realized by only one system, the process is simple, the flow is smooth, the layout is compact, and a large amount of water resources can be saved as a dry process. However, due to the abrasion between the activated coke and the equipment and between the activated coke particles, when the activated carbon moves in the moving bed desulfurization and denitrification equipment, a considerable amount of the activated coke is crushed and becomes waste activated coke powder which cannot be recycled, so that the consumption of the activated coke is increased, the resource waste is caused, and the operation cost is increased. CN204543986U discloses a two-section active coke/carbon desulfurization and denitrification integrated tower and a desulfurization and denitrification system, which comprises a tower body filled with active coke/carbon, wherein the tower body sequentially comprises a feeding buffer bin, a first reaction bin, a second reaction bin and a discharging buffer bin from top to bottom, and a material conveying valve is arranged between the first reaction bin and the second reaction bin; the tower body also comprises an original smoke inlet box and a purified smoke exhaust box which are connected to the side wall of the same side of the tower body, and a gas connecting box connected to the side wall of the other side of the tower body; the part of the relative both sides wall on the first reaction storehouse is first ventilative striker plate, the ventilative striker plate of second respectively, the part of the relative both sides wall on the second reaction storehouse is the ventilative striker plate of third, the ventilative striker plate of fourth respectively, first ventilative striker plate, the ventilative striker plate of third are located respectively clean flue gas exhaust box, raw flue gas inlet box, the ventilative striker plate of second and the ventilative striker plate of third all are located in the gas connection box. CN202860399U discloses a high-efficiency active coke desulfurization and denitrification system, which comprises an ammonia adding system, a desulfurization and denitrification system and an active coke regeneration system, wherein the active coke ammonia adding system comprises an ammonia gas storage device, and three paths of ammonia gas outlets are arranged on the ammonia gas storage device; the desulfurization and denitrification system comprises a first ammonia pre-absorption bin; the adsorption tower is connected with the first ammonia pre-absorption bin; the active coke regeneration system comprises a second ammonia pre-absorption bin and a regeneration tower connected with the second ammonia pre-absorption bin, wherein a regeneration preheating zone, a regeneration heating zone and a regeneration cooling zone are arranged in the regeneration tower from top to bottom; the active coke discharged from the lower part of the regeneration tower is conveyed to the first ammonia pre-absorption bin through conveying equipment, and the active coke discharged from the lower part of the adsorption tower is conveyed to the second ammonia pre-absorption bin through conveying equipment.
Therefore, it is necessary to design a flue gas treatment system to reduce the equipment investment and operation cost.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model aims at providing a flue gas processing system based on calcium-based absorbent. The flue gas treatment system can reduce the equipment investment and operation cost, and the absorbent is easy to recycle.
The utility model adopts the following technical scheme to realize the purpose.
The utility model provides a flue gas treatment system based on calcium-based absorbent, which comprises calcium-based absorbent supply equipment, chlorine dioxide supply equipment, pre-dedusting equipment, a moving bed absorption tower and a flue;
the calcium-based absorbent supply equipment comprises a calcium oxide storage tank, a fly ash storage tank, a bentonite storage tank, a process water storage tank, a kneading machine, a granulating machine and a drying machine; the calcium oxide storage tank, the fly ash storage tank, the bentonite storage tank and the process water storage tank are respectively connected with the kneading machine; the kneader is arranged to knead the calcium oxide, the fly ash, the bentonite and the process water into wet materials; the granulator is connected with the kneader and is used for forming the wet materials into granular materials; the dryer is connected with the granulator and is used for drying the granular materials to form the calcium-based absorbent;
the pre-dedusting equipment is arranged to remove dust particles in the original flue gas to form a pre-treated gas; the pre-dedusting equipment is connected with the flue;
the flue is connected with the chlorine dioxide supply equipment; the chlorine dioxide supply equipment supplies a gas-phase oxidant containing chlorine dioxide to the flue, and the pretreated flue gas and the gas-phase oxidant containing chlorine dioxide react in the flue to form oxidized flue gas;
the flue and the dryer are respectively connected with the moving bed absorption tower, and the oxidized flue gas and the calcium-based absorbent react in the moving bed absorption tower to form desulfurized and denitrated flue gas and byproducts.
According to the flue gas treatment system of the present invention, preferably, the chlorine dioxide supply apparatus comprises a gas phase oxidant generator, the gas phase oxidant generator being provided with a raw material inlet and an air inlet; the reactant feedstock from the feedstock inlet generates chlorine dioxide gas in a gas phase oxidant generator, where the chlorine dioxide gas is mixed with dilution air from the air inlet to form a gas phase oxidant containing chlorine dioxide.
According to the flue gas treatment system of the present invention, preferably, the chlorine dioxide supply equipment further comprises a sodium chlorate solution storage, a hydrogen peroxide solution storage and a dilute sulfuric acid storage; the sodium chlorate solution storage device is connected with the raw material inlet and is used for supplying sodium chlorate solution to the gas phase oxidant generator; the hydrogen peroxide solution storage is connected with the raw material inlet and used for supplying hydrogen peroxide solution to the gas-phase oxidant generator; the dilute sulfuric acid reservoir is connected to the feed inlet for supplying dilute sulfuric acid to the vapor phase oxidant generator.
According to the flue gas treatment system of the present invention, preferably, the chlorine dioxide supply apparatus further comprises an air conveyor connected to the air inlet for providing dilution air to the gas phase oxidant generator.
According to the flue gas treatment system of the present invention, preferably, the lower part of the moving bed absorption tower is provided with a flue gas inlet, and the flue gas inlet is connected with the flue; the upper part of the moving bed absorption tower is provided with a flue gas outlet, and the flue gas inlet and the flue gas outlet are arranged at two sides of the moving bed absorption tower; the top of the moving bed absorption tower is provided with a calcium-based absorbent inlet, and the dryer is connected with the calcium-based absorbent inlet.
According to the utility model discloses a flue gas treatment system, preferably, flue gas treatment system still includes the accessory substance storehouse; the byproduct bin is connected with the moving bed absorption tower; the by-product bin is used for storing the by-products generated by the moving bed absorption tower.
According to the utility model discloses a flue gas processing system, preferably, the bottom of moving bed absorption tower looks is provided with the accessory substance export, the accessory substance export with the accessory substance storehouse links to each other.
According to the utility model discloses a flue gas treatment system, preferably, flue gas treatment system still includes the chimney; the chimney is connected with the smoke outlet; the chimney is used for discharging the desulfurization and denitrification flue gas formed by the moving bed absorption tower.
According to the utility model discloses a flue gas treatment system, preferably, flue gas treatment system still includes the draught fan; one end of the induced draft fan is connected with chlorine dioxide supply equipment, and the other end of the induced draft fan is connected with the flue; the gas-phase oxidant containing chlorine dioxide is conveyed to the flue by the induced draft fan.
According to the utility model discloses a flue gas processing system, preferably, dust collecting equipment is electrostatic precipitator in advance, the drying-machine is the guipure formula drying-machine.
The utility model discloses a flue gas processing system based on calcium-based absorbent can reduce equipment investment running cost, and the absorbent is easily recycle.
Drawings
Fig. 1 is a schematic structural diagram of a flue gas treatment system based on a calcium-based absorbent of the present invention.
The reference numerals are explained below:
the method comprises the following steps of 1-moving bed absorption tower, 2-gas phase oxidant generator, 3-kneader, 4-granulator, 5-dryer, 6-sodium chlorate solution storage, 7-hydrogen peroxide solution storage, 8-dilute sulfuric acid storage, 9-pre-dedusting equipment, 10-byproduct bin, 11-chimney, 12-calcium oxide storage tank, 13-fly ash storage tank, 14-bentonite storage tank, 15-induced draft fan, 16-metering pump, 17-air conveyor and 18-process water storage tank.
Detailed Description
The present invention will be further described with reference to the following specific examples, but the scope of the present invention is not limited thereto.
The utility model discloses a flue gas processing system based on calcium-based absorbent includes chlorine dioxide supply apparatus, calcium-based absorbent supply apparatus, dust collecting equipment, removal bed absorption tower, flue in advance. Optionally, an induced draft fan, a chimney, a byproduct bin or a control device can also be included. The utility model discloses a flue gas processing system can reduce equipment investment running cost. As described in detail below.
< calcium-based absorbent feeding apparatus >
In the present invention, the calcium-based absorbent supply apparatus is used for supplying the calcium-based absorbent. The calcium-based absorbent supply equipment comprises a calcium oxide storage tank, a fly ash storage tank, a bentonite storage tank, a process water storage tank, a kneading machine, a granulating machine and a drying machine. The calcium oxide storage tank, the fly ash storage tank, the bentonite storage tank and the process water storage tank are respectively connected with the kneader. The calcium oxide storage tank is connected with the kneader and is used for supplying calcium oxide to the kneader. The fly ash storage tank is connected with the kneader and used for supplying fly ash to the kneader. The bentonite storage tank is connected with the kneader and is used for supplying bentonite to the kneader. The process water storage tank is connected with the kneader and is used for supplying process water to the kneader. The kneader is configured to knead calcium oxide, fly ash, bentonite and process water into a wet material. A granulator is connected to the kneader for forming the wet material into granules. A dryer is connected to the granulator for drying the granulate to form the calcium based absorbent. The granulator can also be connected with the moving bed absorption tower and used for conveying the calcium-based absorbent to the moving bed absorption tower. The dryer is preferably a mesh belt dryer.
< chlorine dioxide supply apparatus >
In the present invention, the chlorine dioxide supply apparatus is used for supplying a gas-phase oxidizing agent containing chlorine dioxide. The chlorine dioxide supply equipment comprises a sodium chlorate solution storage, a hydrogen peroxide solution storage, a dilute sulfuric acid storage, an air conveyor and a gas-phase oxidant generator. A sodium chlorate solution reservoir is connected to the gas phase oxidant generator for providing sodium chlorate thereto. The hydrogen peroxide solution reservoir is connected to the vapor phase oxidizer generator for providing hydrogen peroxide to the vapor phase oxidizer generator. The dilute sulfuric acid reservoir is connected to the vapor phase oxidant generator for providing dilute sulfuric acid to the vapor phase oxidant generator. The vapor phase oxidant generator may be provided with an air inlet. An air conveyor may be connected to the air inlet. The air handler provides dilution air to the gas phase oxidant generator through the air inlet to adjust the concentration of chlorine dioxide in the gas phase oxidant. The gas phase oxidant generator is used for forming the gas phase oxidant containing chlorine dioxide from the sodium chlorate solution, the hydrogen peroxide solution and the dilute sulfuric acid.
The chlorine dioxide supply device of the present invention may further comprise a metering pump. The metering pump has a solution inlet and a solution outlet. The sodium chlorate solution storage, the hydrogen peroxide solution storage and the dilute sulfuric acid storage are respectively connected with the solution inlet of the metering pump. The vapor phase oxidant generator may be provided with a feed inlet. The solution outlet of the metering pump can be connected with the raw material inlet of the gas-phase oxidant generator, and is used for metering the dosage of the sodium chlorate solution, the hydrogen peroxide solution and the dilute sulfuric acid. The specifications of the metering pump are not limited and those known in the art may be employed.
< Equipment for preliminary dust removal >
The utility model discloses in, dust collecting equipment sets up to the dust particle in the former flue gas of desorption and forms the pretreatment gas in advance. The flue is connected with the pre-dust removal equipment. The pre-dedusting equipment can remove most dust particles in the high-temperature flue gas, protect subsequent equipment and reduce the load of the subsequent equipment. The dust removal efficiency can reach more than 90%, preferably more than 95%. The pre-dust removal device is preferably an electrostatic precipitator. According to an embodiment of the utility model, the dust collecting equipment is electrostatic precipitator in advance. The raw flue gas is preferably flue gas from a boiler or a hot blast stove.
< flue >
The utility model discloses in, the flue sets up to make pretreatment gas mix and react with the gaseous phase oxidant that contains chlorine dioxide, forms the oxidation flue gas. The flue is connected with chlorine dioxide supply equipment. The chlorine dioxide supply equipment supplies gas-phase oxidant containing chlorine dioxide to the flue, and the pretreated flue gas and the gas-phase oxidant containing chlorine dioxide react in the flue to form oxidized flue gas. According to some embodiments of the present invention, a chlorine dioxide supply apparatus includes a gas phase oxidant generator; the flue is connected with a gas phase oxidant generator.
The utility model discloses in, the flue can also be connected with the removal bed absorption tower. According to some embodiments of the present invention, the lower part of the moving bed absorption tower is provided with a flue gas inlet; the flue gas inlet is connected with the flue.
< moving bed absorption column >
The utility model discloses in, remove the bed absorption tower and set up to make oxidation flue gas and calcium-based absorbent reverse contact and fully take place the reaction in removing the bed absorption tower, form SOx/NOx control flue gas and accessory substance.
The utility model discloses in, remove the bed absorption tower and can be provided with calcium-based absorbent entry. The calcium-based absorbent inlet may be connected to the dryer. The calcium-based absorbent inlet is preferably arranged at the top of the moving bed absorber. The calcium-based absorbent can pass through the moving bed absorption tower from top to bottom through the calcium-based absorbent inlet.
The utility model discloses in, remove the bed absorption tower and can also be provided with the flue gas entry. The flue gas inlet is connected with the flue. The flue gas inlet is preferably arranged at the lower part of the side wall of the absorption tower of the moving bed. The oxidized flue gas can pass through the moving bed absorption tower from bottom to top through the flue gas inlet. The oxidized flue gas and the calcium-based absorbent react in the moving bed absorption tower to form the desulfurized and denitrated flue gas and byproducts.
The utility model discloses in, remove the bed absorption tower and can also be provided with the accessory substance export. The by-product outlet is preferably arranged at the bottom of the moving bed absorption column. The byproduct outlet may be connected to a byproduct bin.
The utility model discloses in, remove the bed absorption tower and can also be provided with the exhanst gas outlet. The flue gas outlet is preferably arranged at the upper part of the side wall of the absorption tower of the moving bed. The flue gas outlet may be connected to a chimney.
According to a specific embodiment of the present invention, the calcium-based absorbent inlet is disposed at the top of the moving bed absorption tower; the by-product outlet is arranged at the bottom of the moving bed absorption tower; the flue gas inlet is arranged at the lower part of the side wall of the moving bed absorption tower; the flue gas outlet is preferably arranged at the upper part of the side wall of the absorption tower of the moving bed.
< chimney >
The utility model discloses in, the chimney sets up to discharge away the SOx/NOx control flue gas that removes the bed absorption tower and form. The specifications of the chimney are not limited and those known in the art may be employed. The moving bed absorber is preferably provided with a flue gas outlet. The flue gas outlet is preferably arranged on the side wall of the moving bed absorption tower. The chimney can be connected with the flue gas outlet and is used for discharging the desulfurization and denitrification flue gas formed by the moving bed absorption tower.
< by-product storehouse >
The utility model discloses in, the accessory substance storehouse sets up to depositing the accessory substance. The moving bed absorber column may be provided with a by-product outlet. The by-product outlet is preferably arranged at the bottom of the moving bed absorption column. The byproduct bin can be connected with the byproduct outlet and used for storing the byproducts.
< induced draft Fan >
The utility model discloses in, flue gas processing system based on calcium-based absorbent can also include the draught fan. One end of the induced draft fan is connected with the gas phase oxidant generator, and the other end is connected with the flue. The gas-phase oxidant containing chlorine dioxide is conveyed to the flue by the induced draft fan. The induced draft fan can be used for accelerating the conveying speed of the gas-phase oxidant containing chlorine dioxide.
< control apparatus >
The utility model discloses in, flue gas processing system based on calcium-based absorbent can also include controlgear. The control device is preferably a DCS or PLC control device. The DCS or the PLC control equipment is used for acquiring production data and operation parameters in the flue gas treatment process and calculating the emission concentration of the atmospheric pollutants in real time. According to a specific embodiment of the utility model, flue gas processing system based on calcium-based absorbent still includes DCS controlgear. According to another embodiment of the present invention, the calcium-based absorbent based flue gas treatment system further comprises a PLC control device.
The utility model discloses a flue gas processing system based on calcium-based absorbent can reduce equipment investment cost, and the accessory substance can recycle.
Example 1
Fig. 1 is a schematic structural diagram of a flue gas treatment system based on a calcium-based absorbent of the present invention. As shown in fig. 1, the flue gas treatment system based on calcium-based absorbent comprises a calcium-based absorbent supply device, a chlorine dioxide supply device, a moving bed absorption tower 1, a pre-dust removal device 9, a byproduct bin 10, a chimney 11, an induced draft fan 15 and an air conveyor 17.
The calcium-based absorbent supply equipment comprises a calcium oxide storage tank 12, a fly ash storage tank 13, a bentonite storage tank 14, a process water storage tank 18, a kneader 3, a granulator 4 and a dryer 5. The calcium oxide storage tank 12, the fly ash storage tank 13, the bentonite storage tank 14 and the process water storage tank 18 are respectively connected with the kneader 3. The kneader 3 is used for kneading calcium oxide, fly ash and bentonite with process water according to a certain proportion into wet materials. A kneader 3 is connected to the granulator 4 for granulating the wet material. The granulator 4 is connected to a dryer 5 for drying the granulate to form a calcium based absorbent.
The chlorine dioxide supply apparatus includes a sodium chlorate solution reservoir 6, a hydrogen peroxide solution reservoir 7, a dilute sulfuric acid reservoir 8, a gas phase oxidant generator 2, a metering pump 16, and an air conveyor 17. The metering pump 16 has a solution inlet and a solution outlet. The sodium chlorate solution reservoir 6, the hydrogen peroxide solution reservoir 7 and the dilute sulfuric acid reservoir 8 are respectively connected with a solution inlet of a metering pump 16. The vapor phase oxidant generator 2 is provided with a raw material inlet and an air inlet. The solution outlet of the metering pump 16 is connected to the raw material inlet of the gas phase oxidant generator 2, and the metering pump 16 meters the amounts of the sodium chlorate solution, the hydrogen peroxide solution and the dilute sulfuric acid. An air feeder 17 is connected to the air inlet and feeds dilution air to the vapor phase oxidant generator 2. The sodium chlorate solution, the hydrogen peroxide solution and the dilute sulfuric acid form chlorine dioxide gas in the gas-phase oxidant generator 2, the chlorine dioxide gas is mixed with the dilution air, the concentration of the chlorine dioxide is diluted to a safe range, and the gas-phase oxidant containing the chlorine dioxide is formed.
One end of the induced draft fan 15 is connected with the gas phase oxidant generator 2, and the other end is connected with the flue; the gas-phase oxidant containing chlorine dioxide is conveyed to the flue by the induced draft fan 15.
The pre-dust removing device 9 is connected with the flue, removes dust particles in the original flue gas to form pre-treatment gas, and conveys the pre-treatment gas to the flue. The pre-dust removal device 9 is an electrostatic precipitator.
The flue is configured to mix and react the pre-treatment gas with a gas phase oxidant containing chlorine dioxide to form an oxidized flue gas.
The moving bed absorption tower 1 is provided with a calcium-based absorbent inlet, a flue gas outlet and a byproduct outlet. The calcium-based absorbent inlet is disposed at the top of the moving bed absorption tower 1. The calcium-based absorbent inlet is connected to the dryer 5. The calcium-based absorbent passes through the moving bed absorption tower 1 from top to bottom through the calcium-based absorbent inlet. The flue gas inlet is arranged at the lower part of the side wall of the moving bed absorption tower 1, is connected with the flue and conveys the oxidized flue gas to the moving bed absorption tower 1. The oxidized flue gas passes through the moving bed absorption tower 1 from bottom to top through a flue gas inlet, and the flue gas and the calcium-based absorbent in the moving bed absorption tower 1 are in reverse contact and fully react to form the desulfurization and denitrification flue gas and byproducts. The flue gas outlet is arranged at the upper part of the side wall of the moving bed absorption tower 1. The flue gas inlet and the flue gas outlet are arranged at two sides of the moving bed absorption tower 1. The chimney 11 is connected with the flue gas outlet so as to discharge the desulfurization and denitrification flue gas. The by-product outlet is arranged at the bottom of the moving bed absorption tower 1. The by-product bin 11 is connected with the by-product outlet and stores the by-product generated by the moving bed absorption tower 1.
Application example
The flue gas treatment system based on the calcium-based absorbent in example 1 is used for flue gas treatment, the parameters of the calcium-based absorbent are shown in table 1, the formula of the calcium-based absorbent is shown in table 2, the operating parameters of the flue gas treatment system are shown in table 3, and the parameters of the desulfurized and denitrated flue gas treated by the flue gas treatment system are shown in table 4.
TABLE 1 calcium-based absorbent parameters
| Item | Specific surface area (m)2) | Penetration sulfur capacity (mg/g) | Mirabilitum penetration (mg/g) | Compressive strength (N/cm) |
| Number of | 200 | 40 | 15 | 200 |
TABLE 2 calcium-based absorbent formulation
TABLE 3 flue gas treatment System operating parameters
| Parameter(s) | Numerical value | Unit of |
| Inlet smoke volume (Standard condition moisture base) | 166718 | Nm3/h |
| Temperature of inlet smoke | 120 | ℃ |
| Inlet concentration of NO | 180 | mg/Nm3 |
| SO2Inlet concentration | 220 | mg/Nm3 |
| Moisture content of |
10 | vol％ |
| Oxygen content of |
15 | vol％ |
| Dust content of flue gas | 120 | mg/Nm3 |
| ClO2Molar ratio of NO | 1 | |
| Reaction temperature in gas phase oxidant generator | 45 | ℃ |
| Mass fraction of sodium chlorate solution | 30 | ％ |
| Mass fraction of hydrogen peroxide solution | 27.5 | ％ |
| Mass fraction of dilute sulfuric acid | 60 | ％ |
| Molar ratio of sodium chlorate, hydrogen peroxide and sulfuric acid | 1:1:1 | |
| Input amount of dilute sulfuric acid | 0.2 | t/h |
| ClO in gas-phase oxidizing agent containing chlorine dioxide2Volume fraction | 8 | ％ |
| Spraying amount of gas-phase oxidant containing chlorine dioxide | 22.4 | Nm3/h |
| Run time | 4000 | h |
| Amount of calcium-based absorbent | 489 | t/half year |
| Contact time in the column | 15 | s |
TABLE 4 desulfurization and denitration flue gas parameters
| Item | Number of | Unit of |
| Exhaust gas temperature | 65 | ℃ |
| Denitration efficiency | 95 | ％ |
| Efficiency of desulfurization | 95.5 | ％ |
The present invention is not limited to the above embodiments, and any variations, modifications, and substitutions that may occur to those skilled in the art may be made without departing from the spirit of the present invention.
Claims (10)
1. A flue gas treatment system based on a calcium-based absorbent is characterized by comprising calcium-based absorbent supply equipment, chlorine dioxide supply equipment, pre-dedusting equipment, a moving bed absorption tower and a flue;
the calcium-based absorbent supply equipment comprises a calcium oxide storage tank, a fly ash storage tank, a bentonite storage tank, a process water storage tank, a kneading machine, a granulating machine and a drying machine; the calcium oxide storage tank, the fly ash storage tank, the bentonite storage tank and the process water storage tank are respectively connected with the kneading machine; the kneader is arranged to knead the calcium oxide, the fly ash, the bentonite and the process water into wet materials; the granulator is connected with the kneader and is used for forming the wet materials into granular materials; the dryer is connected with the granulator and is used for drying the granular materials to form the calcium-based absorbent;
the pre-dedusting equipment is arranged to remove dust particles in the original flue gas to form a pre-treated gas; the pre-dedusting equipment is connected with the flue;
the flue is connected with the chlorine dioxide supply equipment; the chlorine dioxide supply equipment supplies a gas-phase oxidant containing chlorine dioxide to the flue, and the pretreated flue gas and the gas-phase oxidant containing chlorine dioxide react in the flue to form oxidized flue gas;
the flue and the dryer are respectively connected with the moving bed absorption tower, and the oxidized flue gas and the calcium-based absorbent react in the moving bed absorption tower to form desulfurized and denitrated flue gas and byproducts.
2. The flue gas treatment system of claim 1, wherein the chlorine dioxide supply apparatus comprises a gas phase oxidant generator, the gas phase oxidant generator being provided with a feed inlet and an air inlet; the reactant feedstock from the feedstock inlet generates chlorine dioxide gas in a gas phase oxidant generator, where the chlorine dioxide gas is mixed with dilution air from the air inlet to form a gas phase oxidant containing chlorine dioxide.
3. The flue gas treatment system of claim 2, wherein the chlorine dioxide supply facility further comprises a sodium chlorate solution reservoir, a hydrogen peroxide solution reservoir, and a dilute sulfuric acid reservoir; the sodium chlorate solution storage device is connected with the raw material inlet and is used for supplying sodium chlorate solution to the gas phase oxidant generator; the hydrogen peroxide solution storage is connected with the raw material inlet and used for supplying hydrogen peroxide solution to the gas-phase oxidant generator; the dilute sulfuric acid reservoir is connected to the feed inlet for supplying dilute sulfuric acid to the vapor phase oxidant generator.
4. The flue gas treatment system of claim 3, wherein the chlorine dioxide supply facility further comprises an air conveyor coupled to the air inlet for providing dilution air to the gas phase oxidant generator.
5. The flue gas treatment system according to claim 1, wherein a flue gas inlet is arranged at the lower part of the moving bed absorption tower, and the flue gas inlet is connected with the flue; the upper part of the moving bed absorption tower is provided with a flue gas outlet, and the flue gas inlet and the flue gas outlet are arranged at two sides of the moving bed absorption tower; the top of the moving bed absorption tower is provided with a calcium-based absorbent inlet, and the dryer is connected with the calcium-based absorbent inlet.
6. The flue gas treatment system of claim 1, further comprising a byproduct bin; the byproduct bin is connected with the moving bed absorption tower; the by-product bin is used for storing the by-products generated by the moving bed absorption tower.
7. The flue gas treatment system of claim 6, wherein a byproduct outlet is provided at the bottom of the moving bed absorber phase, and the byproduct outlet is connected to the byproduct silo.
8. The flue gas treatment system of claim 5, further comprising a chimney; the chimney is connected with the smoke outlet; the chimney is used for discharging the desulfurization and denitrification flue gas formed by the moving bed absorption tower.
9. The flue gas treatment system according to any one of claims 1 to 8, further comprising an induced draft fan; one end of the induced draft fan is connected with chlorine dioxide supply equipment, and the other end of the induced draft fan is connected with the flue; the gas-phase oxidant containing chlorine dioxide is conveyed to the flue by the induced draft fan.
10. The flue gas treatment system of claim 9, wherein the pre-dedusting apparatus is an electrostatic precipitator and the dryer is a mesh belt dryer.
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