CN219580220U - SDS desulfurization system suitable for low temperature flue gas - Google Patents
SDS desulfurization system suitable for low temperature flue gas Download PDFInfo
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- CN219580220U CN219580220U CN202320263897.1U CN202320263897U CN219580220U CN 219580220 U CN219580220 U CN 219580220U CN 202320263897 U CN202320263897 U CN 202320263897U CN 219580220 U CN219580220 U CN 219580220U
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- flue gas
- desulfurization
- temperature flue
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- desulfurization reactor
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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Abstract
The utility model discloses an SDS desulfurization system suitable for low-temperature flue gas, which comprises a baking soda hopper, a superfine pulverizer, a baking soda agent conveying fan, a baking soda agent conveying pipeline and a surface heat exchanger which are sequentially connected, wherein one side end of the surface heat exchanger is connected with a high-temperature flue gas inlet pipeline of the surface heat exchanger, the other side of the surface heat exchanger is connected with a high-temperature flue gas outlet pipeline of a desulfurization reactor, the inlet pipeline of the desulfurization reactor is connected with a desulfurization reactor tower body, and the lower end of the surface heat exchanger is connected with a baking soda agent spray gun positioned in the inlet pipeline of the desulfurization reactor; the outlet pipeline of the desulfurization reactor tower body is connected with the inlet of the bag-type dust remover, and the outlet of the bag-type dust remover is connected with a chimney through a suction fan. The utility model aims to provide an SDS desulfurization system suitable for low-temperature flue gas, which solves the problem of energy loss caused by low temperature of the flue gas at the inlet of the existing SDS reactor.
Description
Technical Field
The utility model relates to an SDS desulfurization system suitable for low-temperature flue gas.
Background
Sodium-based dry SDS desulfurization injection technology was developed in the eighties of the twentieth century. The technology is mainly an HCl removal dry system developed for the waste incineration industry, and the byproduct component produced by the HCl removal dry system is sodium chloride and is used for recycling, and sodium carbonate is recycled as a raw material to reproduce. Then sodium-based dry SDS desulfurization technology is rapidly developed in Europe, and jet systems, grinding systems, special products, optimization of basic system design and the like are developed. The European market is mainly used for desulfurizing tail gas of a garbage incinerator, and has good purifying effect in other industries including coking, glass manufacturing, coal-fired power plants, hazardous waste incinerators, diesel power generation, biomass power generation, cement and the like. The sodium-based dry SDS desulfurization process desulfurizing agent is activated by the heat of the flue gas in the flue by the high-efficiency spraying and uniformly distributing device, the specific surface area of the superfine sodium bicarbonate powder is rapidly increased, the superfine sodium bicarbonate powder is fully contacted with the flue gas, physical and chemical reactions occur, and acidic substances such as SO2 in the flue gas are absorbed and purified. Sodium bicarbonate (baking soda, naHCO 3) is used as an adsorbent for flue gas desulfurization, acidic pollutants in flue gas are removed through chemical adsorption, and simultaneously, some organic and inorganic trace substances can be removed through physical adsorption.
The NaHCO3 fine powder is directly sprayed into the flue gas with the temperature higher than 150 ℃, activated under the action of high-temperature flue gas, and a micropore structure is formed on the surface, SO that the flue gas in the flue fully contacts with the activated desulfurizing agent to generate chemical reaction, SO2 and other acidic media in the flue gas are absorbed and purified, and the desulfurized and dried Na2SO4 byproducts enter a bag-type dust collector along with the air flow to be trapped.
The optimal reaction temperature of SDS desulfurization is about 180 ℃, when the flue gas temperature is lower than 150 ℃, the activity of baking soda is greatly reduced, and in order to ensure the desulfurization effect, the flue gas temperature at the inlet of a desulfurization system is required to be higher than 150 ℃. Many thermodynamic devices are not transformed, the temperature of flue gas at the inlet of a desulfurization system cannot be guaranteed to be higher than 150 ℃, a common solution is to add a set of heating furnace system, the temperature of the flue gas is increased to be higher than 150 ℃, huge energy loss is caused, and the economical efficiency of the thermodynamic device is greatly influenced. Therefore, developing an SDS desulfurization method and system suitable for low-temperature flue gas is significant.
Disclosure of Invention
The utility model aims to provide an SDS desulfurization system suitable for low-temperature flue gas, which solves the problem of energy loss caused by low temperature of the flue gas at the inlet of the existing SDS reactor.
In order to solve the technical problems, the utility model adopts the following technical scheme:
the utility model discloses an SDS desulfurization system suitable for low-temperature flue gas, which comprises a baking soda hopper, an ultrafine powder mill, a baking soda agent conveying fan, a baking soda agent conveying pipeline and a surface heat exchanger which are sequentially connected, wherein one side end of the surface heat exchanger is connected with a high-temperature flue gas inlet pipeline of the surface heat exchanger, the other side of the surface heat exchanger is connected with a high-temperature flue gas outlet pipeline of a desulfurization reactor, the inlet pipeline of the desulfurization reactor is connected with a desulfurization reactor tower body, and the lower end of the surface heat exchanger is connected with a baking soda agent spray gun positioned in the inlet pipeline of the desulfurization reactor; the outlet pipeline of the desulfurization reactor tower body is connected with the inlet of the bag-type dust remover, and the outlet of the bag-type dust remover is connected with a chimney through a suction fan.
Further, a gate valve, a discharge valve, a recycling material agent bin pump and a recycling material agent conveying pipeline are sequentially arranged at the lower end of an ash bucket of the desulfurization reactor tower body.
Further, the recycled material agent conveying pipeline is connected with a recycled material agent spray gun positioned in the ash bucket.
Further, the lower end of the bag-type dust collector is connected with an ash warehouse through a pneumatic ash conveying system.
Further, a radar level gauge is arranged at the upper end of the desulfurization reactor tower body.
Further, a desulfurization reactor baffle plate is arranged in the desulfurization reactor tower body.
Further, fins are arranged in the surface type heat exchanger.
Compared with the prior art, the utility model has the beneficial technical effects that:
the baking soda agent is activated in advance before entering the desulfurization reactor, and a popcorn effect occurs, so that the specific surface area of the baking soda agent is increased, sulfur dioxide in the flue gas is trapped, and the desulfurization efficiency of the baking soda agent in low-temperature flue gas is improved;
the raw flue gas forms 2 flue gas vortexes in the desulfurization reactor, so that the residence time of the raw flue gas in the desulfurization reaction tower is increased, and the desulfurization efficiency of the desulfurization reactor is increased;
the material agent recycling system sends the incompletely reacted material agent which is deposited in the ash bucket of the desulfurizing tower into the desulfurizing reactor again to react with sulfur dioxide in the flue gas again, thereby increasing the utilization rate of the baking soda material agent and reducing the material agent cost;
the energy loss caused by the fact that the temperature of the flue gas needs to be increased in the traditional SDS desulfurization is solved, a flue gas heating system is not required to be arranged in the system, investment of newly-built environment-friendly facilities is reduced, and operation cost is reduced;
drawings
The utility model is further described with reference to the following description of the drawings.
FIG. 1 is a system flow diagram of an SDS desulfurization system for low temperature flue gas according to the present utility model;
reference numerals illustrate: 1. baking soda agent spray gun; 2. a recycling agent spray gun; 3. an ash bucket; 4. a gate valve; 5. a discharge valve; 6. a recycling agent bin pump; 7. a recycling agent conveying pipeline; 8. an inlet pipe of the desulfurization reactor; 9. a radar level gauge; 10. an outlet pipe of the desulfurization reactor; 11. a desulfurizing reactor tower body; 12. a desulfurization reactor separator; 13. a fin; 14. a surface heat exchanger; 15. a high-temperature flue gas inlet pipeline of the surface heat exchanger; 16. a high-temperature flue gas outlet pipeline of the surface heat exchanger; 17. a baking soda hopper; 18. a superfine pulverizer; 19. a baking soda agent conveying pipeline; 20. a baking soda agent conveying fan; 21. a suction fan; 22. a chimney; 23. a bag-type dust collector; 24. a pneumatic ash conveying system; 25. and (5) ash warehouse.
Detailed Description
The SDS desulfurization system suitable for low-temperature flue gas comprises a baking soda hopper 17, an ultrafine powder mill 18, a baking soda agent conveying fan 20, a baking soda agent conveying pipeline 19 and a surface heat exchanger 14 which are sequentially connected, wherein one side end of the surface heat exchanger 14 is connected with a surface heat exchanger high-temperature flue gas inlet pipeline 15, the other side of the surface heat exchanger high-temperature flue gas outlet pipeline 16 is connected to a desulfurization reactor inlet pipeline 8, the desulfurization reactor inlet pipeline 8 is connected with a desulfurization reactor tower body 11, and the lower end of the surface heat exchanger 14 is connected with a baking soda agent spray gun 1 positioned in the desulfurization reactor inlet pipeline 8; the outlet pipeline 10 of the desulfurization reactor tower body 11 is connected with the inlet of a bag-type dust remover 23, and the outlet of the bag-type dust remover 23 is connected with a chimney 22 through a suction fan 21.
The lower end of the ash bucket 3 is provided with a gate valve 4, a discharge valve 5, a recycling material agent bin pump 6 and a recycling material agent conveying pipeline 7 in sequence. The recycling agent conveying pipeline 7 is connected with the recycling agent spray gun 2 positioned in the ash bucket.
The lower end of the bag-type dust collector 23 is connected with an ash warehouse 25 through a pneumatic ash conveying system 24. The upper end of the desulfurization reactor tower body 11 is provided with a radar level gauge 9. A desulfurization reactor baffle plate 12 is arranged in the desulfurization reactor tower body 11. Fins 13 are arranged in the surface heat exchanger 14
The baking soda hopper, the superfine pulverizer, the baking soda agent conveying fan and the baking soda agent conveying pipeline form a material agent preparation system, and the baking soda agent preparation system is mainly used for grinding baking soda raw materials into material agents with the particle size of 20-25 mu m and conveying the material agents to the surface heater. The heat source of the surface heat exchanger adopts high-temperature flue gas at the front end of thermodynamic equipment (for example, a boiler SDS reactor is generally arranged at the outlet of a low-temperature preheater, a flue gas bypass is arranged in the inlet direction of a low-temperature economizer, the high-temperature flue gas at the inlet of the low-temperature economizer is conveyed to the high-temperature flue gas inlet pipeline of the surface heat exchanger by a bypass pipeline), the temperature of the high-temperature flue gas is about 220 ℃, and the input quantity of the high-temperature flue gas is determined after the heat exchange quantity is calculated according to the material agent sprayed into the SDS reactor; the baking soda agent conveying pipeline arranged in the surface heat exchanger is required to be additionally provided with fins to increase the heat exchange area, and the area of the fins is required to be determined according to the temperature of high-temperature flue gas and the heat exchange quantity; the high-temperature flue gas in the surface heat exchanger is sent to an inlet pipeline of the SDS reactor through a high-temperature flue gas outlet pipeline of the surface heat exchanger after heat exchange; the surface heat exchanger shell reduces the flow rate of the high-temperature flue gas, increases the contact time of the high-temperature flue gas and a baking soda agent conveying pipeline with fins, and increases the heat exchange quantity of the high-temperature flue gas and the agent; the surface heat exchanger raises the baking soda agent temperature to above 150 ℃. The baking soda agent is activated in advance under the action of high temperature, a micropore structure is formed on the surface, the baking soda agent is just like popcorn is exploded, and finally, the baking soda agent is uniformly sprayed into an SDS reactor by a baking soda agent spray gun; the baking soda agent spray gun uniformly sprays the baking soda agent into the SDS reactor, and sulfur dioxide in the raw flue gas is absorbed by the baking soda agent; the inlet pipeline of the desulfurization reactor upwards enters the desulfurization reactor, and a smoke vortex is formed at the upper part of the desulfurization reactor, so that the residence time of raw smoke in the SDS reactor is prolonged; the inlet pipeline of the desulfurization reactor enters the desulfurization reactor upwards as shown in fig. 1, and a smoke vortex is formed at the upper part of the desulfurization reactor, so that the residence time of raw smoke in the SDS reactor is prolonged; the separation plate of the desulfurization reactor is arranged in the middle of the desulfurization reactor, raw flue gas firstly enters the left space of the desulfurization reactor as shown in figure 1 and then enters the right space of the desulfurization reactor, and a flue gas vortex is formed at the ash bucket of the desulfurization reactor, so that the residence time of the raw flue gas in the SDS reactor is prolonged; the stay time of the raw flue gas in the desulfurization reactor body is more than 2-3 seconds; the ash bucket, the gate valve, the discharge valve, the recycling agent bin pump, the recycling agent conveying pipeline and the recycling agent spray gun form a recycling system of the recycling agent, and the incompletely reacted recycling agent which is precipitated in the ash bucket of the desulfurizing tower is fed into the desulfurizing reactor again to react with sulfur dioxide in the flue gas again, so that the utilization rate of the baking soda agent is increased; the recycled material agent spray gun is sprayed upwards into the desulfurization reactor as shown in fig. 1, and the flow direction of the flue gas is opposite to that of the flue gas, so that the time for the recycled material agent to contact the raw flue gas is increased; the radar level gauge is arranged at the top of the desulfurization reactor and is used for measuring the level of an ash bucket of the desulfurization reactor; the desulfurization reactor is used for processing the raw flue gas into qualified clean flue gas, the clean flue gas is sent to a bag-type dust remover for dust removal through an outlet pipeline of the desulfurization reactor, and finally sent to a chimney for emission through a suction fan; the pneumatic ash conveying system adopts a gas source which can be nitrogen or compressed air, and the pneumatic ash conveying system conveys the desulfurized ash and other particulate matters to an ash warehouse for outward transportation treatment.
The action process of the utility model is as follows:
the heat source of the surface heat exchanger adopts high-temperature flue gas at the front end of thermodynamic equipment (for example, a boiler SDS reactor is generally arranged at the outlet of a low-temperature preheater, a flue gas bypass is arranged in the inlet direction of a low-temperature economizer, the high-temperature flue gas at the inlet of the low-temperature economizer is conveyed to the high-temperature flue gas inlet pipeline of the surface heat exchanger by a bypass pipeline), the temperature of the high-temperature flue gas is about 220 ℃, and the input quantity of the high-temperature flue gas is determined after the heat exchange quantity is calculated according to the material agent sprayed into the SDS reactor;
preferably, fins are added to the baking soda agent conveying pipeline arranged in the surface heat exchanger to increase the heat exchange area, and the area of the fins is determined according to the temperature of high-temperature flue gas and the heat exchange amount;
preferably, the high-temperature flue gas in the surface heat exchanger is sent to an inlet pipeline of the SDS reactor through a high-temperature flue gas outlet pipeline of the surface heat exchanger after heat exchange;
preferably, the surface heat exchanger shell reduces the flow rate of the high-temperature flue gas, increases the contact time of the high-temperature flue gas and a baking soda agent conveying pipeline with fins, and increases the heat exchange quantity of the high-temperature flue gas and the agent;
preferably, the surface heat exchanger elevates the baking soda agent temperature above 150 ℃. The baking soda agent is activated in advance under the action of high temperature, a micropore structure is formed on the surface, the baking soda agent is just like popcorn is exploded, and finally, the baking soda agent is uniformly sprayed into an SDS reactor by a baking soda agent spray gun;
preferably, the baking soda agent spray gun uniformly sprays the baking soda agent into the SDS reactor, and sulfur dioxide in raw flue gas is absorbed by the baking soda agent;
preferably, the inlet pipeline of the desulfurization reactor enters the desulfurization reactor upwards, and a smoke vortex is formed at the upper part of the desulfurization reactor, so that the residence time of raw smoke in the SDS reactor is increased;
preferably, the inlet pipeline of the desulfurization reactor is upwards introduced into the desulfurization reactor as shown in fig. 1, and a smoke vortex is formed at the upper part of the desulfurization reactor, so that the residence time of raw smoke in the SDS reactor is increased;
preferably, the baffle plate of the desulfurization reactor is arranged in the middle of the desulfurization reactor, and raw flue gas firstly enters the left space of the desulfurization reactor as shown in fig. 1 and then enters the right space of the desulfurization reactor, and flue gas vortex is formed at the ash bucket of the desulfurization reactor, so that the residence time of the raw flue gas in the SDS reactor is prolonged;
preferably, the residence time of the raw flue gas in the desulfurization reactor body should be greater than 2-3 seconds;
preferably, the ash bucket, the gate valve, the discharge valve, the recycling agent bin pump, the recycling agent conveying pipeline and the recycling agent spray gun form an agent recycling system together, and the incompletely reacted agent which is deposited in the ash bucket of the desulfurizing tower is fed into the desulfurizing reactor again to react with sulfur dioxide in the flue gas again, so that the utilization rate of the baking soda agent is increased;
preferably, the regrind spray gun sprays upwards into the desulfurization reactor as shown in fig. 1, opposite to the flow direction of the flue gas, increasing the time for the regrind to contact the raw flue gas;
preferably, the radar level gauge is arranged at the top of the desulfurization reactor and is used for measuring the level of an ash bucket of the desulfurization reactor;
preferably, the desulfurization reactor treats raw flue gas into qualified clean flue gas, the clean flue gas is sent to a bag-type dust remover for dust removal through an outlet pipeline of the desulfurization reactor, and finally is sent to a chimney for emission through a suction fan;
preferably, the air source adopted by the pneumatic ash conveying system and the bin pump can be nitrogen or compressed air, and the pneumatic ash conveying system conveys the desulfurized ash and other particulate matters to an ash warehouse for outward transportation treatment.
The working principle and the using flow of the utility model are as follows:
the stachys pubescens is sent to an ultrafine mill 18 through a baking soda hopper 17 to grind the materials into the materials with the particle size of 20-25 mu m, and the materials are sent to a surface heat exchanger 14 through a baking soda material conveying fan 20 and a baking soda material conveying pipeline (19);
the high-temperature flue gas with the temperature of about 220 ℃ is sent to a surface heat exchanger 14, the baking soda agent is heated to about 150 ℃ and activated in advance, a micropore structure is formed on the surface, and the baking soda agent is uniformly sprayed into an SDS reactor by a baking soda agent spray gun 1;
the baking soda agent captures sulfur dioxide in the raw flue gas in the desulfurization reactor body 11, and a desulfurization reactor partition plate 12 arranged in the desulfurization reactor increases the residence time of the raw flue gas in the desulfurization reactor and increases the desulfurization efficiency of the desulfurization reactor;
the recycling system is composed of the ash bucket 3 of the desulfurization reactor, the gate valve 4, the discharge valve 5, the recycling agent bin pump 6, the recycling agent conveying pipeline 7 and the recycling agent spray gun 2, and the recycling agent which is precipitated at the bottom of the ash bucket 3 of the desulfurization tower and is not completely reacted is fed into the desulfurization reactor again to react with sulfur dioxide in the flue gas again, so that the utilization rate of the baking soda agent is increased; the clean flue gas treated by the desulfurization reactor is sent to a bag-type dust remover for dust removal through an outlet pipeline of the desulfurization reactor, and finally sent to a chimney for emission through a suction fan.
The above embodiments are only illustrative of the preferred embodiments of the present utility model and are not intended to limit the scope of the present utility model, and various modifications and improvements made by those skilled in the art to the technical solutions of the present utility model should fall within the protection scope defined by the claims of the present utility model without departing from the design spirit of the present utility model.
Claims (7)
1. The SDS desulfurization system suitable for the low-temperature flue gas is characterized by comprising a baking soda hopper (17), an ultrafine powder mill (18), a baking soda agent conveying fan (20), a baking soda agent conveying pipeline (19) and a surface heat exchanger (14) which are sequentially connected, wherein one side end of the surface heat exchanger (14) is connected with a high-temperature flue gas inlet pipeline (15) of the surface heat exchanger, the high-temperature flue gas outlet pipeline (16) of the surface heat exchanger on the other side is connected with an inlet pipeline (8) of a desulfurization reactor, the inlet pipeline (8) of the desulfurization reactor is connected with a tower body (11) of the desulfurization reactor, and the lower end of the surface heat exchanger (14) is connected with a baking soda agent spray gun (1) positioned in the inlet pipeline (8) of the desulfurization reactor; the outlet pipeline (10) of the desulfurization reactor tower body (11) is connected with the inlet of the bag-type dust remover (23), and the outlet of the bag-type dust remover (23) is connected with a chimney (22) through a suction fan (21).
2. The SDS desulfurization system for low-temperature flue gas according to claim 1, wherein a gate valve (4), a discharge valve (5), a regrind agent bin pump (6) and a regrind agent conveying pipeline (7) are sequentially arranged at the lower end of an ash bucket (3) of the desulfurization reactor tower body (11).
3. SDS desulfurization system for low temperature flue gas according to claim 2, characterized in that the regrind agent delivery conduit (7) is connected to a regrind agent lance (2) located in the hopper.
4. SDS desulfurization system suitable for low-temperature flue gas according to claim 1, characterized in that the lower end of the bag-type dust collector (23) is connected to an ash silo (25) via a pneumatic ash conveying system (24).
5. The SDS desulfurization system for low-temperature flue gas according to claim 1, wherein a radar level gauge (9) is provided at the upper end of the desulfurization reactor tower body (11).
6. SDS desulfurization system suitable for low temperature flue gas according to claim 1, characterized in that a desulfurization reactor partition (12) is arranged in the desulfurization reactor tower (11).
7. SDS desulfurization system suitable for low temperature flue gas according to claim 1, characterized in that fins (13) are provided in the surface heat exchanger (14).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202320263897.1U CN219580220U (en) | 2023-02-17 | 2023-02-17 | SDS desulfurization system suitable for low temperature flue gas |
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| CN202320263897.1U CN219580220U (en) | 2023-02-17 | 2023-02-17 | SDS desulfurization system suitable for low temperature flue gas |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116020251A (en) * | 2023-02-17 | 2023-04-28 | 包头钢铁（集团）有限责任公司 | A SDS desulfurization system suitable for low temperature flue gas |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116020251A (en) * | 2023-02-17 | 2023-04-28 | 包头钢铁（集团）有限责任公司 | A SDS desulfurization system suitable for low temperature flue gas |
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