CN213668653U - Desulfurization and denitrification device containing moving bed desulfurization and denitrification tower - Google Patents
Desulfurization and denitrification device containing moving bed desulfurization and denitrification tower Download PDFInfo
- Publication number
- CN213668653U CN213668653U CN202021990275.1U CN202021990275U CN213668653U CN 213668653 U CN213668653 U CN 213668653U CN 202021990275 U CN202021990275 U CN 202021990275U CN 213668653 U CN213668653 U CN 213668653U
- Authority
- CN
- China
- Prior art keywords
- chlorine dioxide
- storage tank
- flue gas
- inlet
- desulfurization
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a SOx/NOx control device who contains removal bed SOx/NOx control tower. The desulfurization and denitrification device comprises chlorine dioxide preparation equipment, calcium-based absorbent granulation equipment, a pre-deduster, a moving bed desulfurization and denitrification tower and a flue gas pipeline; the chlorine dioxide preparation equipment comprises a sodium chlorate solution storage tank, a hydrogen peroxide solution storage tank, a dilute sulfuric acid storage tank and a chlorine dioxide generator; the calcium-based absorbent granulation equipment comprises a calcium hydroxide powder storage tank, a process water storage tank, a kneading machine, a granulator and a dryer. The utility model discloses a SOx/NOx control device can improve SOx/NOx control efficiency, reduces equipment investment running cost.
Description
Technical Field
The utility model relates to a SOx/NOx control device who contains removal bed SOx/NOx control tower.
Background
With the rapid development of economy, the industrialization and urbanization of China are accelerated, the atmospheric pollution is increasingly serious, and dust, sulfur dioxide, nitrogen oxide, trace heavy metals and the like in pollutants can cause harm to the environment and human health. In order to improve the current situation of air pollution, a desulfurization and denitrification device is often adopted to treat the polluted air.
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. CN205730886U discloses an active carbon/burnt SOx/NOx control integrated device: an air inlet at the lower part of the reaction tower is communicated with an ammonia gas conveying pipeline and a flue gas heat exchanger, and the flue gas heat exchanger is communicated to a coke oven discharge flue; the top of the reaction tower is communicated to a storage bin through a supply pipeline, and activated carbon/activated coke is supplied by the storage bin; an air outlet at the upper part of the reaction tower is communicated to a chimney through a discharge pipeline, and a fan is arranged in the discharge pipeline. CN209438313U discloses an activated carbon adsorption tower for flue gas desulfurization and denitration technology, which comprises a lower section, an upper section and an adsorption tower section which are sequentially connected from bottom to top; the rotating shaft controlled by a motor is matched with the discharge hole to control the discharging speed of the activated carbon, so that the discharging speed of the activated carbon is controllable, the discharging speed of the activated carbon is reasonably adjusted according to the treatment capacity of flue gas, and the utilization rate of the activated carbon is improved; but need set up the distributing device of unloading, the structure is complicated, and the active carbon exists with piling up the form, and the charcoal layer is thicker, and the pressure drop is great.
Therefore, a desulfurization and denitrification device needs to be designed, so that the desulfurization and denitrification efficiency can be improved, and the equipment investment and operation cost can be reduced.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model aims at providing a SOx/NOx control device who contains removal bed SOx/NOx control tower. The desulfurization and denitrification device can improve the desulfurization and denitrification efficiency and reduce the equipment investment and operation cost.
The utility model adopts the following technical scheme to realize the purpose.
The utility model provides a desulfurization and denitrification device with a moving bed desulfurization and denitrification tower, which comprises chlorine dioxide preparation equipment, calcium-based absorbent granulation equipment, a pre-dust remover, the moving bed desulfurization and denitrification tower and a flue gas pipeline;
the chlorine dioxide preparation equipment comprises a sodium chlorate solution storage tank, a hydrogen peroxide solution storage tank, a dilute sulfuric acid storage tank and a chlorine dioxide generator; the sodium chlorate solution storage tank is connected with the chlorine dioxide generator and used for providing the sodium chlorate solution for the chlorine dioxide generator; the hydrogen peroxide solution storage tank is connected with the chlorine dioxide generator and used for providing hydrogen peroxide solution for the chlorine dioxide generator; the dilute sulfuric acid storage tank is connected with the chlorine dioxide generator and is used for providing dilute sulfuric acid for the chlorine dioxide generator; the chlorine dioxide generator is used for enabling the sodium chlorate solution, the hydrogen peroxide solution and the dilute sulfuric acid to form oxidizing gas containing chlorine dioxide;
the calcium-based absorbent granulation equipment comprises a calcium hydroxide powder storage tank, a process water storage tank, a kneading machine, a granulator and a dryer; the calcium hydroxide powder storage tank is connected with the kneading machine and used for supplying calcium hydroxide powder to the kneading machine; the process water storage tank is connected with the kneader and is used for providing process water for the kneader; the kneading machine is arranged to knead the calcium hydroxide powder 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 removing moisture from the granular materials to form granular calcium-based absorbent;
the pre-dust remover is connected with the flue gas pipeline; the pre-dust remover is arranged to remove dust particles in the flue gas to be treated so as to form pre-treatment gas;
the flue gas pipeline is connected with the chlorine dioxide generator; the flue gas pipeline is arranged to mix and react the pretreatment gas and the oxidizing gas containing chlorine dioxide to form oxidized flue gas;
the moving bed desulfurization and denitrification tower is provided with a calcium-based absorbent inlet and a flue gas inlet; the calcium-based absorbent inlet is connected with the dryer, the flue gas inlet is connected with the flue gas pipeline, and the oxidized flue gas and the calcium-based absorbent react in the moving bed desulfurization and denitrification tower to form purified flue gas and desulfurization and denitrification byproducts.
According to the desulfurization and denitrification device of the utility model, preferably, the chlorine dioxide generator is provided with a sodium chlorate solution inlet, a hydrogen peroxide solution inlet and a dilute sulfuric acid inlet;
the sodium chlorate solution storage tank is connected with the sodium chlorate solution inlet; the hydrogen peroxide solution storage tank is connected with the hydrogen peroxide solution inlet; the dilute sulfuric acid storage tank is connected with the dilute sulfuric acid inlet.
According to the utility model discloses a SOx/NOx control device, preferably, SOx/NOx control device still includes air conveyer; the chlorine dioxide generator is provided with an air inlet; the air conveyor is connected with the air inlet; the air conveyer is used for conveying air to the chlorine dioxide generator and adjusting the concentration of the chlorine dioxide in the oxidizing gas.
According to the utility model discloses a SOx/NOx control device, preferably, chlorine dioxide preparation equipment still includes first measuring pump; the sodium chlorate solution storage tank is connected with an inlet of the first metering pump, and an outlet of the first metering pump is connected with an inlet of the sodium chlorate solution.
According to the utility model discloses a SOx/NOx control device, preferably, chlorine dioxide preparation equipment still includes the second measuring pump; the hydrogen peroxide solution storage tank is connected with an inlet of the second metering pump, and an outlet of the second metering pump is connected with the hydrogen peroxide solution inlet.
According to the utility model discloses a SOx/NOx control device, preferably, chlorine dioxide preparation equipment still includes the third metering pump; the dilute sulfuric acid storage tank is connected with an inlet of the third metering pump, and an outlet of the third metering pump is connected with the dilute sulfuric acid inlet.
According to the utility model discloses a SOx/NOx control device, preferably, SOx/NOx control device still includes the draught fan; one end of the induced draft fan is connected with the chlorine dioxide generator, and the other end of the induced draft fan is connected with the flue gas pipeline; and the oxidizing gas containing chlorine dioxide is conveyed to the flue gas pipeline by the induced draft fan.
According to the utility model discloses a SOx/NOx control device, preferably, SOx/NOx control device still includes the accessory substance storehouse; the moving bed desulfurization and denitrification tower is provided with a byproduct outlet; the byproduct storage bin is connected with the byproduct outlet; the byproduct storage bin is used for collecting desulfurization and denitrification byproducts generated by the moving bed desulfurization and denitrification tower.
According to the utility model discloses a SOx/NOx control device, preferably, SOx/NOx control device still includes the chimney; the moving bed desulfurization and denitrification tower is provided with a purified flue gas outlet; the chimney is connected with the purified flue gas outlet.
According to the utility model discloses a SOx/NOx control device, preferably, calcium-based absorbent entry sets up at the top of moving bed SOx/NOx control tower, the by-product export sets up in the bottom of moving bed SOx/NOx control tower, the flue gas entry sets up in the lateral wall lower part of moving bed SOx/NOx control tower, it sets up on the lateral wall upper portion of moving bed SOx/NOx control tower to purify the exhanst gas outlet.
The utility model discloses a SOx/NOx control device who contains removal bed SOx/NOx control tower can improve SOx/NOx control efficiency, reduces equipment investment running cost.
Drawings
Fig. 1 is the utility model discloses a contain SOx/NOx control device's of removal bed SOx/NOx control tower structure schematic diagram.
The reference numerals are explained below:
1-a pre-deduster, 2-a sodium chlorate solution storage tank, 21-a first metering pump, 3-a hydrogen peroxide solution storage tank, 31-a second metering pump, 4-a dilute sulfuric acid storage tank, 41-a third metering pump, 5-a chlorine dioxide generator, 6-a kneader, 7-a granulator, 8-a dryer, 9-a moving bed desulfurization and denitrification tower, 10-a chimney, 11-a byproduct storage bin, 12-an induced draft fan, 13-an air conveyor, 14-a calcium hydroxide powder storage tank and 15-a 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 SOx/NOx control device who contains removal bed SOx/NOx control tower includes calcium-based absorbent granulation equipment, chlorine dioxide preparation equipment, dust remover in advance, removes bed SOx/NOx control tower, flue gas pipeline, chimney and accessory substance storage storehouse. Optionally, an air conveyor, an induced draft fan, or a controller may also be included. The utility model discloses a SOx/NOx control device can improve SOx/NOx control efficiency, reduces equipment investment running cost. As described in detail below.
< calcium-based absorbent granulation apparatus >
The utility model discloses in, calcium-based absorbent granulation equipment is used for the shaping of calcium-based absorbent. The calcium-based absorbent granulation equipment comprises a calcium hydroxide powder storage tank, a process water storage tank, a kneading machine, a granulator and a dryer. The calcium hydroxide powder storage tank is connected with the kneading machine and used for supplying calcium hydroxide powder to the kneading machine. 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 the calcium hydroxide powder with process water into a wet material. A granulator is connected to the kneader for forming the wet material into a granulated material. The dryer is connected with the granulator and is used for removing moisture from the granular materials to form the granular calcium-based absorbent.
< chlorine dioxide production facility >
In the present invention, the chlorine dioxide producing apparatus is used for producing an oxidizing gas containing chlorine dioxide. The chlorine dioxide preparation equipment comprises a sodium chlorate solution storage tank, a hydrogen peroxide solution storage tank, a dilute sulfuric acid storage tank and a chlorine dioxide generator. The sodium chlorate solution storage tank is connected with the chlorine dioxide generator and is used for providing the sodium chlorate solution for the chlorine dioxide generator. The hydrogen peroxide solution storage tank is connected with the chlorine dioxide generator and is used for providing hydrogen peroxide solution for the chlorine dioxide generator. The dilute sulfuric acid storage tank is connected with the chlorine dioxide generator and is used for providing dilute sulfuric acid for the chlorine dioxide generator. The chlorine dioxide generator is used for enabling the sodium chlorate solution, the hydrogen peroxide solution and the dilute sulfuric acid to form oxidizing gas containing chlorine dioxide.
In the utility model, the chlorine dioxide generator can be provided with a sodium chlorate solution inlet, a hydrogen peroxide solution inlet and a dilute sulfuric acid inlet. The sodium chlorate solution storage tank is connected with the sodium chlorate solution inlet. The hydrogen peroxide solution storage tank is connected with the hydrogen peroxide solution inlet. The dilute sulfuric acid storage tank is connected with the dilute sulfuric acid inlet.
In the present invention, preferably, the chlorine dioxide preparing apparatus further comprises a first metering pump. The sodium chlorate solution storage tank is connected with the inlet of the first metering pump. The outlet of the first metering pump is connected with the inlet of the sodium chlorate solution. The specifications of the first metering pump are not limited and those known in the art may be employed.
In the present invention, preferably, the chlorine dioxide producing apparatus further comprises a second metering pump. The hydrogen peroxide solution storage tank is connected with the inlet of the second metering pump. The outlet of the second metering pump is connected to the hydrogen peroxide solution inlet. The specifications of the second metering pump are not limited and those known in the art may be employed.
In the present invention, preferably, the chlorine dioxide producing apparatus further comprises a third metering pump. The dilute sulfuric acid storage tank is connected with the inlet of the third metering pump. The outlet of the third metering pump is connected with the dilute sulphuric acid inlet. The specifications of the third metering pump are not limited and those known in the art may be employed.
According to a specific embodiment of the present invention, the chlorine dioxide preparation apparatus includes a sodium chlorate solution storage tank, a hydrogen peroxide solution storage tank, a dilute sulfuric acid storage tank, a chlorine dioxide generator, a first metering pump, a second metering pump, and a third metering pump. The chlorine dioxide generator is provided with a sodium chlorate solution inlet, a hydrogen peroxide solution inlet and a dilute sulfuric acid inlet. The sodium chlorate solution storage tank is connected with the inlet of the first metering pump. The outlet of the first metering pump is connected with the inlet of the sodium chlorate solution. The hydrogen peroxide solution storage tank is connected with the inlet of the second metering pump. The outlet of the second metering pump is connected to the hydrogen peroxide solution inlet. The dilute sulfuric acid storage tank is connected with the inlet of the third metering pump. The outlet of the third metering pump is connected with the dilute sulphuric acid inlet.
< Pre-dust collector >
The utility model discloses in, the dust particle that the dust catcher is arranged in the desorption pending flue gas in advance and form the preliminary treatment gas. The pre-dust collector is connected with the flue gas pipeline. The pre-dust remover can remove most dust particles in the high-temperature flue gas, protect subsequent equipment and reduce the load of the subsequent equipment at the same time. The pre-precipitator is preferably an electrostatic precipitator. The dust removal efficiency can reach more than 90%, preferably more than 96%. According to an embodiment of the present invention, the pre-dust collector is an electrostatic dust collector. The flue gas to be treated is preferably flue gas from a boiler or a hot blast stove.
< flue gas duct >
The utility model discloses in, flue gas pipeline sets up to make pretreatment gas mix and take place the reaction with the oxidizing gas who contains chlorine dioxide, forms the flue gas after the oxidation. The flue gas pipeline is connected with the chlorine dioxide generator.
< moving bed desulfurization/denitrification column >
The utility model discloses in, remove the bed SOx/NOx control tower and set up to make flue gas and calcium-based absorbent after the oxidation reverse contact and fully take place the reaction in removing the bed SOx/NOx control tower, form and purify flue gas and SOx/NOx control accessory substance.
The utility model discloses in, remove the bed SOx/NOx control tower and be provided with calcium-based absorbent entry and flue gas entry. The calcium-based absorbent inlet is connected with the dryer. The calcium-based absorbent inlet is preferably arranged at the top of the moving bed desulfurization and denitrification tower. The calcium-based absorbent can pass through the moving bed desulfurization and denitrification tower from top to bottom through the calcium-based absorbent inlet. The flue gas inlet is connected with the flue gas pipeline. The flue gas inlet is preferably arranged at the lower part of the side wall of the moving bed desulfurization and denitrification tower. The oxidized flue gas can pass through the moving bed desulfurization and denitrification tower from bottom to top through the flue gas inlet. The oxidized flue gas and the calcium-based absorbent react in the moving bed desulfurization and denitrification tower to form purified flue gas and desulfurization and denitrification byproducts.
The utility model discloses in, remove the bed SOx/NOx control tower and can be provided with the accessory substance export. The byproduct outlet is preferably arranged at the bottom of the moving bed desulfurization and denitrification tower. The moving bed desulfurization and denitrification tower can also be provided with a purified flue gas outlet. The purified flue gas outlet is preferably arranged at the upper part of the side wall of the moving bed desulfurization and denitrification tower. According to a specific embodiment of the utility model, the calcium-based absorbent inlet is arranged at the top of the moving bed desulfurization and denitrification tower; the byproduct outlet is arranged at the bottom of the moving bed desulfurization and denitrification tower; the flue gas inlet is arranged at the lower part of the side wall of the moving bed desulfurization and denitrification tower; the purified flue gas outlet is preferably arranged at the upper part of the side wall of the moving bed desulfurization and denitrification tower.
< chimney >
The utility model discloses in, the chimney sets up to discharge away the purification flue gas that removes bed SOx/NOx control tower formation. The specifications of the chimney are not limited and those known in the art may be employed. The moving bed desulfurization and denitrification tower is preferably provided with a purified flue gas outlet. The purified flue gas outlet is preferably arranged on the side wall of the moving bed desulfurization and denitrification tower. The chimney can be connected with the purified flue gas outlet and is used for discharging the purified flue gas formed by the moving bed desulfurization and denitrification tower.
< storage facility for by-products >
The utility model discloses in, accessory substance storage storehouse sets up to storing SOx/NOx control accessory substance. The moving bed desulfurization and denitrification tower can be provided with a byproduct outlet. The byproduct outlet is preferably arranged at the bottom of the moving bed desulfurization and denitrification tower. The byproduct storage bin can be connected with the byproduct outlet and used for storing desulfurization and denitrification byproducts.
< air conveyor >
The utility model discloses in, the SOx/NOx control device who contains removal bed SOx/NOx control tower can also include air conveyer. The chlorine dioxide generator may be provided with an air inlet. An air conveyor may be connected to the air inlet. The air conveyor conveys air to the chlorine dioxide generator through the air inlet to adjust the concentration of the chlorine dioxide in the oxidizing gas.
< induced draft Fan >
The utility model discloses in, the SOx/NOx control device who contains removal bed SOx/NOx control tower can also include the draught fan. One end of the induced draft fan is connected with the chlorine dioxide generator, and the other end is connected with the flue gas pipeline. The induced draft fan can be used for accelerating the conveying speed of the oxidizing gas containing the chlorine dioxide.
< controller >
The utility model discloses in, the SOx/NOx control device who contains removal bed SOx/NOx control tower can also include the controller. The controller is preferably a DCS or PLC controller. The DCS or the PLC is used for collecting production data and operation parameters of the flue gas desulfurization and denitration integrated process and calculating the emission concentration of the atmospheric pollutants and the desulfurization and denitration efficiency in real time. According to a specific embodiment of the utility model, the SOx/NOx control device who contains removal bed SOx/NOx control tower still includes the DCS controller. According to the utility model discloses a another embodiment, the SOx/NOx control device who contains removal bed SOx/NOx control tower still includes the PLC controller.
The utility model discloses a SOx/NOx control device who contains removal bed SOx/NOx control tower can make flue gas and absorbent contact more abundant, the SO in the flue gas2、NOXThe method has the advantages of simple and efficient removal, no need of subsequent flue gas dust removal step, reduced investment cost, and recyclable by-products, and can be used for producing building material products such as bricks, plates, cementing materials and the like, so as to realize recycling economy by using wastes to prepare wastes.
Example 1
Fig. 1 is the utility model discloses a contain SOx/NOx control device's of removal bed SOx/NOx control tower structure schematic diagram. As shown in fig. 1, the desulfurization and denitrification apparatus including the moving bed desulfurization and denitrification tower includes a calcium-based absorbent granulation device, a chlorine dioxide preparation device, a pre-dust collector 1, a flue gas duct, a moving bed desulfurization and denitrification tower 9, a chimney 10, a byproduct storage bin 11, an induced draft fan 12, and an air conveyor 13.
The calcium-based absorbent granulation equipment comprises a calcium hydroxide powder storage tank 14, a process water storage tank 15, a kneader 6, a granulator 7 and a dryer 8. The calcium hydroxide powder tank 14 is connected to the kneader 6, and supplies calcium hydroxide powder to the kneader 6. The process water tank 15 is connected to the kneader 6 and supplies process water to the kneader 6. The kneader 6 kneads the calcium hydroxide powder and the process water into wet material. A granulator 7 is connected to the kneader 6 and forms the wet material into a granulated material. A dryer 8 is connected to the granulator 7 to dehydrate the granulated material to form a granulated calcium-based absorbent.
The chlorine dioxide preparation equipment comprises a sodium chlorate solution storage tank 2, a hydrogen peroxide solution storage tank 3, a dilute sulfuric acid storage tank 4, a chlorine dioxide generator 5, a first metering pump 21, a second metering pump 31 and a third metering pump 41. The chlorine dioxide generator 5 is provided with a sodium chlorate solution inlet, a hydrogen peroxide solution inlet, a dilute sulfuric acid inlet and an air inlet. The sodium chlorate solution storage tank 2 is connected with an inlet of the first metering pump 21, an outlet of the first metering pump 21 is connected with an inlet of the sodium chlorate solution, and the sodium chlorate solution storage tank 2 provides the sodium chlorate solution for the chlorine dioxide generator 5. The hydrogen peroxide solution tank 3 is connected to an inlet of the second metering pump 31, an outlet of the second metering pump 31 is connected to an inlet of the hydrogen peroxide solution, and the hydrogen peroxide solution tank 3 supplies the hydrogen peroxide solution to the chlorine dioxide generator 5. The dilute sulfuric acid storage tank 4 is connected with the inlet of the third metering pump 41, the outlet of the third metering pump 41 is connected with the dilute sulfuric acid inlet, and the dilute sulfuric acid storage tank 4 provides dilute sulfuric acid for the chlorine dioxide generator 5. An air delivery device 13 is connected to the air inlet and delivers air to the chlorine dioxide generator 5. The sodium chlorate solution, the hydrogen peroxide solution and the dilute sulfuric acid form chlorine dioxide gas in the chlorine dioxide generator 5, and the chlorine dioxide gas is mixed with air to dilute the concentration of the chlorine dioxide to a safe range to form the oxidizing gas containing the chlorine dioxide.
The pre-dust remover 1 is connected with the flue gas pipeline, removes dust particles in the flue gas to be treated to form pre-treatment gas, and conveys the pre-treatment gas to the flue gas pipeline.
One end of the induced draft fan 12 is connected with the chlorine dioxide generator 5, and the other end is connected with the flue gas pipeline, and the oxidizing gas containing chlorine dioxide is conveyed to the flue gas pipeline.
The flue gas duct is configured to mix and react the pre-treatment gas with the oxidizing gas containing chlorine dioxide to form oxidized flue gas.
The moving bed desulfurization and denitrification tower 9 is provided with a calcium-based absorbent inlet, a flue gas inlet, a purified flue gas outlet and a byproduct outlet. The calcium-based absorbent inlet is arranged at the top of the moving bed desulfurization and denitrification tower 9. The calcium-based absorbent inlet is connected to the dryer 8. The flue gas inlet is arranged at the lower part of the side wall of the moving bed desulfurization and denitrification tower 9, is connected with a flue gas pipeline, and conveys the oxidized flue gas to the moving bed desulfurization and denitrification tower 9. The oxidized flue gas passes through the moving bed desulfurization and denitrification tower 9 from bottom to top through a flue gas inlet, and the flue gas is in reverse contact with the calcium-based absorbent in the moving bed desulfurization and denitrification tower 9 and fully reacts to form purified flue gas and desulfurization and denitrification byproducts. The purified flue gas outlet is arranged on the upper part of the side wall of the moving bed desulfurization and denitrification tower 9. The chimney 10 is connected to the purified flue gas outlet for discharging the purified flue gas. The byproduct outlet is arranged at the bottom of the moving bed desulfurization and denitrification tower 9. The byproduct storage bin 11 is connected with a byproduct outlet and used for collecting desulfurization and denitrification byproducts generated by the moving bed desulfurization and denitrification tower.
Example 2
The same as in example 1 except for the following settings: the pre-precipitator 1 is an electrostatic precipitator.
Application example
The desulfurization and denitrification device containing the moving bed desulfurization and denitrification tower in example 1 was subjected to flue gas desulfurization and denitrification treatment, wherein the parameters of the calcium-based absorbent are shown in table 1, the operating parameters of the desulfurization and denitrification device are shown in table 2, and the parameters of the purified flue gas after treatment by the desulfurization and denitrification device are shown in table 3.
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) |
| Numerical value | 200 | 40 | 15 | 200 |
TABLE 2 desulfurization and denitrification facility operating parameters
| Parameter(s) | Numerical value | Unit of |
| Inlet smoke volume (Standard condition moisture base) | 152824 | Nm3/h |
| Temperature of inlet smoke | 120 | ℃ |
| Inlet concentration of NO | 200 | mg/Nm3 |
| SO2Inlet concentration | 250 | 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 | -- |
| Chlorine dioxide generator reaction temperature | 45 | ℃ |
| Mass fraction of sodium chlorate solution | 30 | ％ |
| Mass fraction of hydrogen peroxide solution | 27.5 | ％ |
| Mass fraction of dilute sulfuric acid | 60 | ％ |
| Sodium chlorate: hydrogen peroxide: molar ratio of sulfuric acid | 1：1：1 | -- |
| Input amount of dilute sulfuric acid | 0.2 | t/h |
| ClO in oxidizing gases2Volume fraction | 8 | ％ |
| Oxidizing agent (ClO)2) Amount of spray | 16 | Nm3/h |
| Run time | 4000 | h |
| Amount of absorbent | 509.4 | t/half year |
| Contact time in the column | 15 | s |
TABLE 3 purified flue gas parameters
| Item | Number of | Unit of |
| Exhaust gas temperature | 65 | ℃ |
| Denitration efficiency | 95 | ％ |
| Efficiency of desulfurization | 96.8 | ％ |
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 desulfurization and denitrification device containing a moving bed desulfurization and denitrification tower is characterized by comprising chlorine dioxide preparation equipment, calcium-based absorbent granulation equipment, a pre-dust remover, the moving bed desulfurization and denitrification tower and a flue gas pipeline;
the chlorine dioxide preparation equipment comprises a sodium chlorate solution storage tank, a hydrogen peroxide solution storage tank, a dilute sulfuric acid storage tank and a chlorine dioxide generator; the sodium chlorate solution storage tank is connected with the chlorine dioxide generator and used for providing the sodium chlorate solution for the chlorine dioxide generator; the hydrogen peroxide solution storage tank is connected with the chlorine dioxide generator and used for providing hydrogen peroxide solution for the chlorine dioxide generator; the dilute sulfuric acid storage tank is connected with the chlorine dioxide generator and is used for providing dilute sulfuric acid for the chlorine dioxide generator; the chlorine dioxide generator is used for enabling the sodium chlorate solution, the hydrogen peroxide solution and the dilute sulfuric acid to form oxidizing gas containing chlorine dioxide;
the calcium-based absorbent granulation equipment comprises a calcium hydroxide powder storage tank, a process water storage tank, a kneading machine, a granulator and a dryer; the calcium hydroxide powder storage tank is connected with the kneading machine and used for supplying calcium hydroxide powder to the kneading machine; the process water storage tank is connected with the kneader and is used for providing process water for the kneader; the kneading machine is arranged to knead the calcium hydroxide powder 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 removing moisture from the granular materials to form granular calcium-based absorbent;
the pre-dust remover is connected with the flue gas pipeline; the pre-dust remover is arranged to remove dust particles in the flue gas to be treated so as to form pre-treatment gas;
the flue gas pipeline is connected with the chlorine dioxide generator; the flue gas pipeline is arranged to mix and react the pretreatment gas and the oxidizing gas containing chlorine dioxide to form oxidized flue gas;
the moving bed desulfurization and denitrification tower is provided with a calcium-based absorbent inlet and a flue gas inlet; the calcium-based absorbent inlet is connected with the dryer, the flue gas inlet is connected with the flue gas pipeline, and the oxidized flue gas and the calcium-based absorbent react in the moving bed desulfurization and denitrification tower to form purified flue gas and desulfurization and denitrification byproducts.
2. The desulfurization and denitrification apparatus according to claim 1, wherein the chlorine dioxide generator is provided with a sodium chlorate solution inlet, a hydrogen peroxide solution inlet and a dilute sulfuric acid inlet;
the sodium chlorate solution storage tank is connected with the sodium chlorate solution inlet; the hydrogen peroxide solution storage tank is connected with the hydrogen peroxide solution inlet; the dilute sulfuric acid storage tank is connected with the dilute sulfuric acid inlet.
3. The desulfurization and denitrification apparatus according to claim 2, further comprising an air conveyor; the chlorine dioxide generator is provided with an air inlet; the air conveyor is connected with the air inlet; the air conveyer is used for conveying air to the chlorine dioxide generator and adjusting the concentration of the chlorine dioxide in the oxidizing gas.
4. The SOx/NOx control device of claim 2, wherein the chlorine dioxide production facility further comprises a first metering pump; the sodium chlorate solution storage tank is connected with an inlet of the first metering pump, and an outlet of the first metering pump is connected with an inlet of the sodium chlorate solution.
5. The SOx/NOx control device of claim 4, wherein the chlorine dioxide production facility further comprises a second metering pump; the hydrogen peroxide solution storage tank is connected with an inlet of the second metering pump, and an outlet of the second metering pump is connected with the hydrogen peroxide solution inlet.
6. The SOx/NOx control device of claim 5, wherein the chlorine dioxide production facility further comprises a third metering pump; the dilute sulfuric acid storage tank is connected with an inlet of the third metering pump, and an outlet of the third metering pump is connected with the dilute sulfuric acid inlet.
7. The desulfurization and denitrification apparatus according to claim 1, further comprising an induced draft fan; one end of the induced draft fan is connected with the chlorine dioxide generator, and the other end of the induced draft fan is connected with the flue gas pipeline; and the oxidizing gas containing chlorine dioxide is conveyed to the flue gas pipeline by the induced draft fan.
8. The desulfurization and denitrification apparatus according to claim 1, further comprising a byproduct storage bin; the moving bed desulfurization and denitrification tower is provided with a byproduct outlet; the byproduct storage bin is connected with the byproduct outlet; the byproduct storage bin is used for collecting desulfurization and denitrification byproducts generated by the moving bed desulfurization and denitrification tower.
9. The desulfurization and denitrification apparatus according to claim 8, further comprising a chimney; the moving bed desulfurization and denitrification tower is provided with a purified flue gas outlet; the chimney is connected with the purified flue gas outlet.
10. The desulfurization and denitrification apparatus according to claim 9, wherein the calcium-based absorbent inlet is disposed at the top of the moving bed desulfurization and denitrification tower, the byproduct outlet is disposed at the bottom of the moving bed desulfurization and denitrification tower, the flue gas inlet is disposed at the lower portion of the sidewall of the moving bed desulfurization and denitrification tower, and the purified flue gas outlet is disposed at the upper portion of the sidewall of the moving bed desulfurization and denitrification tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021990275.1U CN213668653U (en) | 2020-09-11 | 2020-09-11 | Desulfurization and denitrification device containing moving bed desulfurization and denitrification tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021990275.1U CN213668653U (en) | 2020-09-11 | 2020-09-11 | Desulfurization and denitrification device containing moving bed desulfurization and denitrification tower |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN213668653U true CN213668653U (en) | 2021-07-13 |
Family
ID=76748591
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202021990275.1U Active CN213668653U (en) | 2020-09-11 | 2020-09-11 | Desulfurization and denitrification device containing moving bed desulfurization and denitrification tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN213668653U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115228261A (en) * | 2022-08-04 | 2022-10-25 | 中国石油化工股份有限公司 | Moving bed process method and device for direct dechlorination and dust removal of high-temperature flue gas |
-
2020
- 2020-09-11 CN CN202021990275.1U patent/CN213668653U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115228261A (en) * | 2022-08-04 | 2022-10-25 | 中国石油化工股份有限公司 | Moving bed process method and device for direct dechlorination and dust removal of high-temperature flue gas |
| CN115228261B (en) * | 2022-08-04 | 2023-10-17 | 中国石油化工股份有限公司 | Moving bed process method and device for directly dechlorinating and dedusting high-temperature flue gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP3272414B1 (en) | Method for removing nitrogen oxides from a gas stream | |
| CN107983119A (en) | The dry desulfurization method of denitration of oxidation is forced based on ozone | |
| CN104324575B (en) | A kind of system of spray absorber formula sintering flue gas and desulfurizing and denitrifying | |
| CN105080332A (en) | Resource utilization system for pellet sintering waste gas and method | |
| CN102233230A (en) | Waste burning smoke purification process and purification system | |
| CN106955571A (en) | A kind of industrial smoke ozone step-by-step oxidation absorbs the device and method of simultaneous SO_2 and NO removal | |
| CN105126567A (en) | Method and device for removing nitric oxide and sulfur oxide from gas flow | |
| CN213668653U (en) | Desulfurization and denitrification device containing moving bed desulfurization and denitrification tower | |
| CN107812441A (en) | Flue gas dry desulfurizing method of denitration based on red mud | |
| CN214210020U (en) | Ceramic flue gas treatment system | |
| CN211837168U (en) | Active material generating device containing plasma generating equipment and flue gas denitration device | |
| WO2021134927A1 (en) | Dry process of integrated flue gas desulfurization and denitration | |
| CN211913303U (en) | Oxidizing gas generation device and flue gas denitration device | |
| CN107583457A (en) | Smoke denitrifier and its production method and application | |
| CN113634100A (en) | Method for carrying out oxidation denitration on sintering flue gas by using chlorine dioxide | |
| CN113117479A (en) | Semi-dry flue gas desulfurization and denitrification method | |
| CN113117478A (en) | Flue gas desulfurization and denitrification method based on fly ash | |
| CN111167278B (en) | Flue gas denitration device and method containing plasma generating equipment | |
| CN212999279U (en) | Flue gas treatment system for efficiently utilizing carbon monoxide | |
| CN110787617B (en) | Sintering flue gas semi-dry desulfurization and denitrification integrated device and method | |
| CN213408210U (en) | Flue gas treatment system based on calcium-based absorbent | |
| CN213408209U (en) | Flue gas desulfurization and denitrification system containing fixed bed absorption tower | |
| CN113019092A (en) | Flue gas desulfurization and denitrification method and system based on dense-phase semi-dry method | |
| CN113117493A (en) | Method for flue gas desulfurization and denitration by using mixed reducing agent | |
| CN213348384U (en) | Absorbent production equipment, moving bed absorption tower and flue gas treatment device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |