CN212395927U - Near zero emission type flue gas multi-pollutant integrated removing system - Google Patents
Near zero emission type flue gas multi-pollutant integrated removing system Download PDFInfo
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- CN212395927U CN212395927U CN202021703565.3U CN202021703565U CN212395927U CN 212395927 U CN212395927 U CN 212395927U CN 202021703565 U CN202021703565 U CN 202021703565U CN 212395927 U CN212395927 U CN 212395927U
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Abstract
The utility model discloses a nearly zero release type flue gas multi-pollutant integration desorption system, packageThe device comprises an economizer, an air preheater, an electrostatic dust collector, a flue gas cooler and a low-temperature adsorption tower; the shell pass inlet of economizer connects the boiler flue gas, and the tube pass inlet connects the boiler and gives water, and the shell pass outlet of economizer connects to air heater's tube pass inlet, and air heater's shell pass inlet connects to the boiler air inlet, and air heater's tube pass outlet connects to electrostatic precipitator, and the electrostatic precipitator bottom is provided with the ash discharge mouth, and electrostatic precipitator's exhanst gas outlet is connected to the gas cooler, and the gas cooler bottom is provided with the comdenstion water export, and the cold exhanst gas outlet at top is connected to the low temperature adsorption tower, and the low temperature adsorption tower afterbody sets up clean flue gas export. The utility model discloses utilize the dissolution characteristic and the adsorption characteristic of pollutant component at low temperature in the flue gas to carry out the desorption of pollutant, SO in the desorption flue gas simultaneously2、SO3、NO、NO2HCl, HF, Hg and VOCs, and achieves near zero emission.
Description
Technical Field
The utility model belongs to the technical field of the purification is administered to the flue gas pollutant, concretely relates to nearly zero release type flue gas multi-pollutant integration desorption system.
Background
The generation of a large amount of pollutants from coal-fired flue gas is one of the important factors harming the atmospheric environment and human health. Coal-fired flue gas pollutants can be divided into two main pollutants and other pollutants according to the emission amount and the harm degree of the pollutants.
The main pollutants comprise dust and SO2And NOx, the pollutants have mature control technologies, the technologies widely adopted on the large coal-fired boiler at present comprise cloth bag dust removal, electrostatic dust removal, limestone-gypsum wet desulphurization, Selective Catalytic Reduction (SCR) denitration and the like, and calcium spraying desulphurization and non-selective catalytic reduction are carried out in the upper furnace of a small and medium fluidized bed boiler(SNCR) denitration techniques are also widely used.
Other contaminants include SO3HCl, HF, Hg, VOCs, and the like. Of these, HCl and HF generally follow SO in wet desulfurization2And removing the components together. But SO3The pollutants of Hg and VOCs can not be effectively removed in the current flue gas treatment system. However, with the increasing environmental requirements, the control of these harmful substances is also imperative.
The current pollutant removal technology adopts a process route of removing pollutants one by one and connecting the pollutants in series. The process flow is complicated and the operation cost is high. Therefore, the development of the integrated removal technology of multiple pollutants in flue gas has been devoted to domestic and overseas for many years, such as an ozone oxidation method, a hydrogen peroxide oxidation method, an electron beam ammonia method, an electrocatalytic oxidation method, a liquid phase catalytic oxidation method, an active coke method and the like. Most of the technologies are to oxidize NO which is difficult to be removed by wet absorption and oxidation to NO2Then with SO2The removal is carried out together with the wet method, SO that the method is only limited to integrated desulfurization and denitrification and the simultaneous removal of HCl and HF and SO3And pollutants such as Hg and VOCs cannot be effectively treated. The active coke method can simultaneously remove SO by an adsorption mode3、SO3、NO2And pollutants such as HCl, HF, Hg and VOCs, but NO cannot be removed by adsorption, and the NO is the most main component of NOx and accounts for more than 95%. By spraying ammonia gas into the active coke bed layer, the denitration rate of 70-80% can be realized in a catalytic reduction mode, but the requirement of near zero emission is difficult to meet.
Besides the integrated removal of multiple pollutants in flue gas, the development of near-zero emission technology also becomes a hot spot in current flue gas treatment. At present, most of large units in China complete ultra-low emission reconstruction, namely, the emission standard is realized: SO (SO)2≦35mg/Nm3，NOx≦50mg/Nm3Dust ≦ 5mg/Nm3. Although the emission concentration has been controlled to be rather low, the absolute value of the pollutant emissions is still not negligible due to the large total amount of flue gas emissions. Near zero emission of flue gas pollutants is still one of the ultimate targets of cleaning coal and electricity.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a nearly zero release type flue gas multi-pollutant integration desorption system to overcome prior art's defect, the utility model discloses utilize in the flue gas pollutant component to carry out the desorption of pollutant with the adsorption characteristic at low temperature, SO in the flue gas can be desorption simultaneously2、SO3、NO、NO2HCl, HF, Hg and VOCs, and achieves near zero emission.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
the near zero emission type integrated removal system for multiple pollutants in flue gas comprises an economizer, an air preheater, an electrostatic precipitator, a flue gas cooler and a low-temperature adsorption tower;
the shell pass inlet of economizer connects the boiler flue gas, and the tube pass inlet connects the boiler and gives water, and the shell pass outlet of economizer connects to air heater's tube pass inlet, and air heater's shell pass inlet connects to the boiler air inlet, and air heater's tube pass outlet connects to electrostatic precipitator, and the electrostatic precipitator bottom is provided with the ash discharge mouth, and electrostatic precipitator's exhanst gas outlet is connected to the gas cooler, and the gas cooler bottom is provided with the comdenstion water export, and the cold exhanst gas outlet at top is connected to the low temperature adsorption tower, and the low temperature adsorption tower afterbody sets up clean flue gas export.
Further, a direct spray cooling device or an indirect heat exchange cooling device is connected to the flue gas cooler.
Further, the low-temperature adsorption tower adopts a fixed bed adsorption tower or a moving bed adsorption tower.
Further, the cryogenic adsorption tower is provided with two.
Compared with the prior art, the utility model discloses following profitable technological effect has:
the utility model is suitable for a coal-fired flue gas such as flue gas of power plant, steel mill sintering flue gas, coke oven flue gas, in the flue gas cooler, flue gas temperature falls to room temperature and following temperature, HCl HF and part SO in the flue gas3、NO2And dissolving Hg in the condensed water of the flue gas to remove the residual SO2NOx, Hg and VOCThe pollutants such as s and the like are absorbed and removed integrally through a low-temperature absorption tower, and NO components which are difficult to absorb are oxidized into NO through a low-temperature oxidation absorption mechanism2The adsorption removal and the pollutant removal link are physical methods (dissolution or adsorption), and NH is not consumed3And limestone, the operation cost is mainly the energy consumption cost of flue gas cooling, and in addition, the low-temperature adsorbent adopted by the utility model is regenerated in a heating or vacuum suction mode and can be recycled; h in flue gas2O、SO2And NOx can be recycled.
Furthermore, the flue gas cooler adopts a direct spray cooling mode or an indirect heat exchange cooling mode, and when the spray cooling mode is adopted, a small amount of dust which is not removed by the electrostatic dust collector is also washed and discharged along with condensed water.
Further, two low-temperature adsorption towers are arranged, and when the first low-temperature adsorption tower is saturated in adsorption, SO is adsorbed2Or after NO starts to penetrate through, the low-temperature flue gas is switched to a second low-temperature adsorption tower for adsorption and removal, and the first low-temperature adsorption tower is regenerated in a heating or vacuum suction mode.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without undue limitation.
FIG. 1 is a schematic view of the near zero emission type integrated removal method for multiple pollutants in flue gas of the present invention;
figure 2 is the removal efficiency of flue gas contaminants by dissolution of condensed water at different condensation temperatures.
Wherein, 1, a coal economizer; 2. an air preheater; 3. an electrostatic precipitator; 4. a flue gas cooler; 5. a low temperature adsorption tower.
Detailed Description
The present invention is described in further detail below:
as shown in fig. 1, the near-zero emission type flue gas multi-pollutant integrated removal system comprises an economizer 1, an air preheater 2, an electrostatic dust collector 3, a flue gas cooler 4 and a low-temperature adsorption tower 5;
the shell pass inlet of the economizer 1 is connected with boiler flue gas, the tube pass inlet is connected with boiler water supply, the shell pass outlet of the economizer 1 is connected with the tube pass inlet of the air preheater 2, the shell pass inlet of the air preheater 2 is connected with boiler air inlet, the tube pass outlet of the air preheater 2 is connected with the electrostatic dust collector 3, the bottom of the electrostatic dust collector 3 is provided with an ash discharge port, the flue gas outlet of the electrostatic dust collector 3 is connected with the flue gas cooler 4, the flue gas cooler 4 is connected with a direct spray cooling device or an indirect heat exchange cooling device, the bottom of the flue gas cooler 4 is provided with a condensate water outlet, the cold flue gas outlet at the top is connected with the low-temperature adsorption tower 5, the tail of the low-temperature adsorption tower 5 is provided with a clean flue gas outlet, the low-temperature adsorption tower 5 adopts a fixed bed adsorption tower.
The boiler flue gas passes through the economizer 1 to heat boiler feed water; then, the air enters the boiler through an air preheater 2 by heating; the flue gas after heat recovery by the economizer 1 and the air preheater 2 enters an electrostatic dust collector 3 to remove dust in the flue gas; the flue gas after dust removal enters the flue gas cooler 4, and is cooled to room temperature or lower temperature, and the flue gas cooler 4 adopts a direct spraying cooling mode or an indirect heat exchange cooling mode. And moisture in the flue gas is condensed and then discharged out of the flue gas system.
In the flue gas cooler 4, the pollutant components in the flue gas are totally or partially dissolved in the condensed water and discharged together. As shown in figure 2, HCl and HF have strong solubility and almost completely dissolve in condensed water of flue gas, NO2And SO3Partially dissolved in condensed water, SO2A small amount of mercury (Hg) dissolved in the condensed water0) Insoluble in water, bivalent mercury (Hg)2+) Part of the dust is dissolved in the condensed water, and if a spraying cooling mode is adopted, most of the small amount of dust which is not removed by the dust remover is also washed and discharged along with the condensed water.
The cooled cold flue gas enters a low-temperature adsorption tower 5, and SO is generated2NO, elemental mercury (Hg)0) And residual NO2、SO3Bivalent mercury (Hg)2+) Is absorbed with pollutants such as VOCsAnd (4) removing. Wherein, SO2、NO2、SO3Hg, VOCs and other pollutants are directly adsorbed and removed, NO cannot be directly adsorbed and removed, but NO can be directly adsorbed and removed with O in smoke2Is removed by an oxidation adsorption mechanism under the action of low temperature and an adsorbent, namely NO and O in the smoke2Is rapidly oxidized to NO by surface enrichment of the adsorbent at low temperatures to form locally high concentrations2And further adsorbed on the surface of the adsorbent. The oxidation adsorption mechanism is the key to realize low-temperature adsorption denitration.
SO in the flue gas passes through a flue gas cooler 4 and a low-temperature adsorption tower 52、SO3、NO、NO2、HCl、HF、Hg0、Hg2+Almost all pollutants such as VOCs, dust and the like are removed, and near zero emission is realized.
The adsorbent in the low-temperature adsorption tower 5 is regenerated in a heating or vacuum suction mode and is repeatedly used. The low-temperature adsorption tower 5 can adopt a fixed bed adsorption tower or a moving bed adsorption tower. Desorbed SO-rich gas2The gas of NOx is recycled by producing sulfuric acid, sulfur, nitric acid, sulfate or nitrate and the like.
For the sake of clarity, the present invention will be further described in detail with reference to the following embodiments and accompanying drawings. It is understood by those skilled in the art that the following descriptions are not intended to limit the scope of the present invention, and any modifications and variations based on the present invention are within the scope of the present invention.
Example (b): as shown in figure 1, after heat recovery is carried out on boiler flue gas by an economizer 1, the temperature is reduced to 400 ℃, then the temperature is further reduced to 120 ℃ by an air preheater 2, and dust in the flue gas is reduced to 20mg/Nm by an electrostatic dust collector 33The flue gas enters a flue gas cooler 4 to indirectly exchange heat with low-temperature refrigerating fluid, SO that the flue gas is cooled to 5 ℃, and HCl, HF and part of SO in the flue gas2、SO3、NO2And divalent mercury Hg2+The dissolved flue gas condensate is discharged from the flue gas cooler 4. The low-temperature flue gas enters a fixed bed adsorption tower 5, SO2、NO、NO2、SO3Pollution of Hg and VOCThe substances are absorbed and removed by the filled active carbon, and near zero emission is achieved.
The low-temperature adsorption tower 5 is provided with an A/B tower for carrying out adsorption-regeneration alternate operation. When the adsorption of the tower A is saturated, SO2Or after NO starts to penetrate through, the low-temperature flue gas is switched to the tower B to be adsorbed and removed, and the tower A is regenerated in a heating mode.
Claims (4)
1. The near-zero emission type integrated removal system for multiple pollutants in flue gas is characterized by comprising an economizer (1), an air preheater (2), an electrostatic dust collector (3), a flue gas cooler (4) and a low-temperature adsorption tower (5);
the shell side entry linkage boiler flue gas of economizer (1), tube side entry linkage boiler feedwater, the shell side exit linkage of economizer (1) is to the tube side entry of air heater (2), the shell side entry linkage of air heater (2) is to the boiler air inlet, the tube side exit linkage of air heater (2) is to electrostatic precipitator (3), electrostatic precipitator (3) bottom is provided with the ash discharge mouth, the exhanst gas outlet of electrostatic precipitator (3) is connected to gas cooler (4), gas cooler (4) bottom is provided with the comdenstion water export, the cold exhanst gas outlet at top is connected to cryosorption tower (5), cryosorption tower (5) afterbody sets up net exhanst gas outlet.
2. The integrated near-zero emission flue gas multi-pollutant removal system according to claim 1, wherein the flue gas cooler (4) is connected with a direct spray cooling device or an indirect heat exchange cooling device.
3. The integrated removal system for multiple pollutants in flue gas with near zero emission according to claim 1, wherein the low-temperature adsorption tower (5) adopts a fixed bed adsorption tower or a moving bed adsorption tower.
4. The integrated removal system for multiple pollutants in flue gas with near zero emission according to claim 1, wherein two low-temperature adsorption towers (5) are provided.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111841065A (en) * | 2020-08-14 | 2020-10-30 | 中国华能集团清洁能源技术研究院有限公司 | Near-zero emission type integrated removal system and method for multiple pollutants in flue gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111841065A (en) * | 2020-08-14 | 2020-10-30 | 中国华能集团清洁能源技术研究院有限公司 | Near-zero emission type integrated removal system and method for multiple pollutants in flue gas |
| WO2022032860A1 (en) * | 2020-08-14 | 2022-02-17 | 中国华能集团清洁能源技术研究院有限公司 | Near-zero emission-type flue gas multi-pollutant integrated removal system and method |
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