CN214287485U - Calcium-carbon method flue gas desulfurization and denitrification device - Google Patents

Calcium-carbon method flue gas desulfurization and denitrification device Download PDF

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CN214287485U
CN214287485U CN202021663058.1U CN202021663058U CN214287485U CN 214287485 U CN214287485 U CN 214287485U CN 202021663058 U CN202021663058 U CN 202021663058U CN 214287485 U CN214287485 U CN 214287485U
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flue gas
heat exchange
calcium
outlet
exchange channel
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徐克�
李诗京
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China Metallurgical Engineering Co ltd
Sinosteel Equipment and Engineering Co Ltd
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China Metallurgical Engineering Co ltd
Sinosteel Equipment and Engineering Co Ltd
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Abstract

The utility model discloses a calcium charcoal method flue gas desulfurization denitrification facility, calcium charcoal method flue gas desulfurization denitrification facility includes: the wet calcium desulphurization device is used for desulphurization of the flue gas and is provided with a first flue gas inlet and a first flue gas outlet which are communicated with each other; the carbon-based catalyst denitration device is used for denitration of flue gas and is provided with a second flue gas inlet and a second flue gas outlet which are communicated with each other; the heat exchange device is provided with a first heat exchange channel and a second heat exchange channel and is arranged to transfer the heat of the flue gas in the first heat exchange channel to the flue gas in the second heat exchange channel. According to the utility model discloses calcium charcoal method flue gas desulfurization denitrification facility has solved the solid waste that the denitration produced and the high problem of SOx/NOx control running cost.

Description

Calcium-carbon method flue gas desulfurization and denitrification device
Technical Field
The utility model relates to a technical field is administered to the flue gas, more specifically relates to a calcium charcoal method flue gas desulfurization denitrification facility.
Background
The energy consumption structure of China is mainly coal, along with the development of national economy of China, a large amount of sulfur oxides and nitrogen oxides are generated in the consumption and use processes of coal, and meanwhile, the emission of industrial gas is accompanied with the emission of a large amount of dust, so that serious pollution is caused to air.
With the gradual enhancement of environmental awareness, the requirements of China on the desulfurization and denitrification of industrial gases are gradually improved. The desulfurization and denitrification methods are various, and the main technology at present is semi-dry desulfurization and Selective Catalytic Reduction (SCR) denitrification, or desulfurization and denitrification simultaneously by adopting a desulfurization and denitrification device. Wherein, Selective Catalytic Reduction (SCR) denitration has high heat supplementing cost, and the catalyst becomes dangerous waste after being used for 3 years and cannot be treated. Semi-dry desulfurization generates a large amount of desulfurization ash with complex components, cannot be treated, and is equivalent to transferring atmospheric pollution to solid waste. The active carbon desulfurization and denitrification device has high operation cost and high manufacturing cost, and the problem of byproduct treatment is difficult to solve. Simultaneously, in the SOx/NOx control process, because SOx/NOx control's best processing temperature is different, an active carbon SOx/NOx control device need carry out SOx/NOx control and denitration simultaneously, and mutual interference's the condition can take place for these two processes to influence SOx/NOx control's treatment effect, there is the hot problem.
SUMMERY OF THE UTILITY MODEL
The utility model discloses aim at solving one of the technical problem that exists among the prior art at least. Therefore, an object of the utility model is to provide a calcium charcoal method flue gas desulfurization denitrification facility, calcium charcoal method flue gas desulfurization denitrification facility has solved the solid waste that the denitration produced and the high problem of SOx/NOx control running cost.
According to the utility model discloses calcium charcoal method flue gas desulfurization denitrification facility, include: the wet calcium desulphurization device is used for desulphurization of the flue gas and is provided with a first flue gas inlet and a first flue gas outlet which are communicated with each other; the carbon-based catalyst denitration device is used for denitration of flue gas and is provided with a second flue gas inlet and a second flue gas outlet which are communicated with each other; the heat exchange device is provided with a first heat exchange channel and a second heat exchange channel, wherein raw flue gas enters the first heat exchange channel through an inlet of the first heat exchange channel, an outlet of the first heat exchange channel is communicated with the first flue gas inlet, an inlet of the second heat exchange channel is communicated with the first flue gas outlet, an outlet of the second heat exchange channel is communicated with the second flue gas inlet, the second flue gas outlet is communicated with the outside so as to discharge treated flue gas, and the heat exchange device is arranged to transmit heat of the flue gas in the first heat exchange channel to the flue gas in the second heat exchange channel.
According to the utility model discloses calcium charcoal method flue gas desulfurization and denitration device carries out the SOx/NOx control to the flue gas through wet calcium method desulphurization unit and charcoal base catalyst denitration device, and the desulfurizer obtains easily, reduces the running cost, and the denitration discarded object is powdered carbon, can regard as the fuel to use, has solved solid waste's problem. Through heat transfer device, utilize the temperature of former flue gas, realized zero heat supply or few heat supply, reduce the loss of energy by a wide margin, reduce the concurrent heating cost.
In addition, according to the utility model discloses the calcium charcoal method flue gas desulfurization denitrification facility of above-mentioned embodiment can also have following additional technical characterstic:
according to the utility model discloses calcium charcoal method flue gas desulfurization denitrification facility of some embodiments, the export exhaust gas temperature of first heat transfer passageway is T1, T1 satisfies: t1 is more than or equal to 80 ℃ and less than or equal to 120 ℃.
According to some embodiments of the present invention, the temperature of the flue gas discharged from the first flue gas outlet is T2, T2 satisfies: t1 is more than or equal to 50 ℃ and less than or equal to 55 ℃.
According to some embodiments of the utility model, calcium charcoal method flue gas desulfurization denitrification facility still includes: the cooling device is arranged between the first smoke outlet and the inlet of the first heat exchange channel, and is used for reducing the temperature of the smoke exhausted from the first smoke outlet.
According to some embodiments of the utility model, the flue gas temperature after the heat sink cooling is T3, T3 satisfies: t3 is more than or equal to 40 ℃ and less than or equal to 60 ℃.
According to some embodiments of the present invention, the temperature of the flue gas discharged from the outlet of the second heat exchange channel is T4, T4 satisfies: t4 is more than or equal to 70 ℃ and less than or equal to 120 ℃.
According to some embodiments of the utility model, calcium charcoal method flue gas desulfurization denitrification facility still includes: and the temperature rising device is arranged between the outlet of the second heat exchange channel and the second flue gas inlet and is used for rising the temperature of the flue gas discharged from the outlet of the second heat exchange channel.
According to the utility model discloses a some embodiments, the flue gas temperature after the rising temperature device heaies up is T5, T5 satisfies: t5 is more than or equal to 80 ℃ and less than or equal to 120 ℃.
According to some embodiments of the utility model, calcium charcoal method flue gas desulfurization denitrification facility still includes: and the ammonia spraying device is arranged between the temperature rising device and the second flue gas inlet and is used for spraying ammonia to the flue gas.
According to some embodiments of the utility model, charcoal base catalyst denitrification facility still has analytic export, wet calcium method desulphurization unit still have with the analytic gaseous import of first exhanst gas outlet intercommunication, calcium-carbon method flue gas desulfurization denitrification facility still includes: and the analysis device is arranged between the analysis outlet and the analysis gas inlet and is used for analyzing the carbon base discharged from the analysis outlet and discharging the gas generated by analysis into the wet calcium desulphurization device through the analysis gas inlet to carry out calcium desulphurization.
Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
The above and/or additional aspects and advantages of the present invention will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings of which:
fig. 1 is a schematic diagram of a flue gas desulfurization and denitrification device by a calcium-carbon method according to an embodiment of the present invention.
Reference numerals:
a flue gas desulfurization and denitrification device 100 by a calcium-carbon method,
a wet calcium desulphurization device 10, a first flue gas inlet 101, a first flue gas outlet 102, a desorption gas inlet 103,
a carbon-based catalyst denitration device 20, a second flue gas inlet 201, a second flue gas outlet 202, a desorption outlet 203,
heat exchange means 30, an inlet 301 of the first heat exchange channel, an outlet 302 of the first heat exchange channel, an inlet 303 of the second heat exchange channel, an outlet 304 of the second heat exchange channel,
a temperature reducing device 50, a temperature increasing device 51, an ammonia spraying device 52,
and an analysis device 60.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are exemplary only for the purpose of explaining the present invention, and should not be construed as limiting the present invention.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", and the like, indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention.
In the description of the present invention, "a first feature" or "a second feature" may include one or more of the features, and "a plurality" means two or more, and the first feature may be "on" or "under" the second feature, and may include the first and second features being in direct contact, or may include the first and second features being in contact not directly but through another feature therebetween, and the first feature being "on", "above" and "above" the second feature may include the first feature being directly above and obliquely above the second feature, or merely indicating that the first feature is higher in level than the second feature.
The following describes a flue gas desulfurization and denitration apparatus 100 by a calcium-carbon method according to an embodiment of the present invention with reference to the drawings.
Referring to fig. 1, a flue gas desulfurization and denitration device 100 by calcium-carbon method according to an embodiment of the present invention may include: a wet calcium desulphurization device 10, a carbon-based catalyst denitration device 20 and a heat exchange device 30.
Specifically, the wet calcium desulfurization device 10 desulfates the flue gas by the wet calcium method, and the wet calcium desulfurization device 10 has a first flue gas inlet 101 and a first flue gas outlet 102 that communicate with each other. The carbon-based catalyst denitration device 20 catalytically denitrates the flue gas by using a carbon-based catalyst (for example, activated carbon or activated coke), and the carbon-based catalyst denitration device 20 has a second flue gas inlet 201 and a second flue gas outlet 202 which are communicated with each other.
In the related technology, SCR denitration is adopted, the heat supplementing cost is high, and the catalyst becomes dangerous waste after being used for 3 years and cannot be treated. By adopting the semi-dry method for desulfurization, a large amount of desulfurized ash with complex components can be generated and cannot be treated, which is equivalent to transferring the pollution of the atmosphere to solid waste. The adoption of the activated carbon desulfurization and denitrification device has high operation cost and high manufacturing cost, and the problem of byproduct treatment is difficult to solve. Simultaneously, in the SOx/NOx control process, because SOx/NOx control's best processing temperature is different, a charcoal base SOx/NOx control device need carry out SOx/NOx control and denitration simultaneously, and the condition of mutual interference can take place for these two processes to influence SOx/NOx control's treatment effect, there is the hot problem.
And the utility model discloses a calcium charcoal method flue gas desulfurization and denitration device 100 adopts wet calcium method desulfurization and the method of carbon-based catalyst catalysis denitration to carry out desulfurization and denitration treatment to the flue gas. And compared with the semi-dry calcium desulphurization, the wet calcium desulphurization has a higher desulphurization rate than the semi-dry calcium desulphurization, and the desulphurization rate can reach more than 95%. The semi-dry calcium method is mainly suitable for treating flue gas of medium and small boilers, and the wet calcium method is mature in desulfurization process, stable in operation and suitable for desulfurization of large and medium enterprises.
In addition, flue gas desulfurization has been widely used in China, and flue gas denitration has been paid attention gradually with the enhancement of environmental awareness in recent years. The utility model discloses a calcium charcoal method flue gas desulfurization denitrification facility 100 can build denitrification facility on former desulphurization unit's basis, utilizes original desulphurization unit or only needs to do simple improvement, greatly reduced engineering cost to former desulphurization unit. In the currently widely used desulfurization devices, the wet calcium desulfurization device accounts for over 90 percent and is in the mainstream position. The utility model discloses a wet calcium method desulphurization unit 10 that calcium charcoal method flue gas desulfurization denitrification facility 100 adopted can not only bring a series of beneficial effects such as no solid waste, but also can further reduce engineering cost by a wide margin.
Referring to fig. 1, wet calcium desulfurization adopts limestone or lime as a desulfurization absorbent, and the limestone is crushed and ground into powder and mixed with water to form absorption slurry. For example, when lime is used as the absorbent, lime powder is digested and then added with water to make an absorbent slurry. The flue gas enters the wet calcium desulphurization device 10 from the first flue gas inlet 101 of the wet calcium desulphurization device 10, the absorbent slurry is contacted and mixed with the flue gas in the wet calcium desulphurization device 10, and sulfur dioxide in the flue gas, calcium carbonate in the slurry and blown oxidizing air perform chemical reaction, so that the desulphurization of the flue gas is realized. The flue gas is discharged from the first flue gas outlet 102 after being desulfurized, and the final reaction product is gypsum. The wet calcium method desulfurization device 10 has high desulfurization efficiency, and the limestone or lime is used as a desulfurization absorbent, so that a desulfurizing agent is easily obtained, the desulfurization cost is low, and the operation cost and the manufacturing cost are reduced. Meanwhile, the generated reaction product is gypsum which can be used as a raw material of cement or a building material, so that pollution is not transferred to solid waste, and the waste is recycled.
As shown in fig. 1, the denitration is catalyzed by a carbon-based catalyst, and the process of catalyzing denitration by the carbon-based catalyst is to oxidize sulfur dioxide in flue gas into sulfur trioxide and dissolve the sulfur trioxide into water to generate dilute sulfuric acid aerosol, and the dilute sulfuric acid aerosol is adsorbed by the carbon-based catalyst. And then ammonia gas is sprayed, and the ammonia gas and the nitrogen oxide generate nitrogen under the catalytic reduction action of the carbon-based catalyst, so that the aim of desulfurization is fulfilled. For example, the ammonia injection gas may be used to treat the flue gas via the ammonia injection device 52. The carbon base has the structure of irregularly arranged microcrystalline carbon, so small gaps are formed in a fixed place, and the mutual combination of the small gaps generates a large number of micropores and a large internal specific surface area, so that the carbon-based catalyst has a good adsorption function. Meanwhile, the larger specific surface and the more pore structures of the carbon-based catalyst enable molecules to be more easily diffused. Therefore, the carbon-based catalyst has high-efficiency dioxin removal capability due to the self adsorption property and the catalytic property, and has a good purification effect on flue gas.
The flue gas can enter from the second flue gas inlet 201, and in the carbon-based catalyst denitration device 20, the flue gas is subjected to denitration treatment, and then is discharged from the second flue gas outlet 202. The waste generated by denitration is carbon powder which can be used as fuel. Different from SCR denitration in the related technology, the carbon-based catalyst catalytic denitration can avoid a large amount of analysis amount and catalyst loss amount generated in the adsorption process, and can recover the activity of the carbon-based catalyst through a regeneration reaction, so that the problem of an adsorbed waste gas treatment channel is solved, and the problem that the catalyst becomes dangerous waste and cannot be treated after being used for several years can not occur.
The utility model discloses the wet calcium method desulfurization that calcium charcoal method flue gas desulfurization denitrification facility 100 adopted and the matching nature of charcoal base catalyst catalysis denitration technology are splendid, have solved the short slab of self independent unit part each other. After reasonable combination, the method has the advantages of wide application range, no three wastes, low operation cost, moderate investment and cost, simple operation, stable operation, realization of ultralow emission and the like, and byproducts are raw materials of cement or building materials.
Further, the heat exchange means 30 has a first heat exchange passage and a second heat exchange passage. As shown in fig. 1, the raw flue gas enters the first heat exchange channel through the inlet 301 of the first heat exchange channel to exchange heat with the raw flue gas. For example, the raw flue gas may be flue gas generated by coal firing, directly exhausted from a boiler. The outlet 302 of the first heat exchange channel is communicated with the first flue gas inlet 101, and flue gas is discharged from the outlet 302 of the first heat exchange channel and enters the wet calcium desulphurization device 10 through the first flue gas inlet 101 for desulphurization. The inlet 303 of the second heat exchange channel is communicated with the first flue gas outlet 102, the outlet 304 of the second heat exchange channel is communicated with the second flue gas inlet 201, flue gas is discharged from the first flue gas outlet 102 after being desulfurized, enters the second heat exchange channel through the inlet 303 of the second heat exchange channel, is subjected to heat exchange, then enters the carbon-based catalyst denitration device 20 for denitration, and the second flue gas outlet 202 is communicated with the outside, so that the treated flue gas can be discharged to the outside. The utility model discloses a calcium charcoal method flue gas desulfurization and denitration device 100 establishes ties wet calcium method desulphurization unit 10, carbon-based catalyst denitrification facility 20 and heat transfer device 30 together, forms a complete flue gas desulfurization and denitration's route, can accept the concentration requirement of extensive former flue gas to can obtain higher SOx/NOx control's efficiency, reach the emission requirement of flue gas. For example, a flue connection may be used to connect the various components.
The heat exchange device 30 is arranged to transfer the heat of the flue gas in the first heat exchange channel to the flue gas in the second heat exchange channel, namely, the heat of the original flue gas entering the first heat exchange channel is transferred to the flue gas entering the second heat exchange channel, so that the low-temperature latent heat of the flue gas is utilized, and the heat supplementing cost is remarkably reduced. The temperature of the original flue gas is utilized to heat the flue gas in the second heat exchange channel, the arrangement fully utilizes the temperature of the original flue gas, zero heat compensation heating or less heat compensation heating is realized, the energy loss is greatly reduced, the energy is effectively saved, and the operation cost is reduced.
In some embodiments, the heat exchange device 30 may be a heat exchanger. A first heat exchange channel and a second heat exchange channel are arranged in one heat exchanger, and the heat exchanger can directly transfer the heat of the flue gas in the first heat exchange channel to the flue gas in the second heat exchange channel. In other embodiments, the heat exchange device 30 may be two heat exchangers. One heat exchanger is provided with a first heat exchange channel, the other heat exchanger is provided with a second heat exchange channel, smoke in the first heat exchange channel of the one heat exchanger can transfer heat to the second heat exchange channel of the other heat exchanger through a medium, and heat exchange is carried out on the smoke in the second heat exchange channel. For example, the medium may be water or air, etc. The arrangement of the two heat exchangers can enlarge the layout range of the wet calcium desulphurization device 10 and the carbon-based catalyst denitration device 20, and reduce the limitation of the layout.
According to the utility model discloses calcium charcoal method flue gas desulfurization and denitration device 100 carries out SOx/NOx control to the flue gas through wet calcium method desulphurization unit 10 and charcoal base catalyst denitrification facility 20, and the desulfurizer obtains easily, reduces the running cost, and the denitration discarded object is powdered carbon, can regard as the fuel to use, has solved solid waste's problem. Through heat transfer device 30, utilize the temperature of former flue gas, realized zero heat supply or few heat supply, reduce the loss of energy by a wide margin, reduce the concurrent heating cost.
According to some embodiments of the utility model, the flue gas temperature of the export 302 exhaust of first heat transfer passageway is T1, and T1 satisfies: t1 is more than or equal to 80 ℃ and less than or equal to 120 ℃. For example, in some embodiments, T1 can be 85 ℃, 90 ℃, 95 ℃, 100 ℃, 105 ℃, 110 ℃, 115 ℃, and the like. The heat of the original flue gas is effectively recovered by the heat exchange device 30, the temperature of the original flue gas is reduced, the temperature of the original flue gas entering the wet calcium desulphurization device 10 is ensured, and the desulphurization efficiency is improved. Simultaneously, the temperature that makes the flue gas accords with the utility model discloses the temperature resistant requirement of equipment, pipeline and material in the calcium charcoal method flue gas desulfurization denitrification facility 100 of embodiment improves clean system's security. The temperature of high temperature flue gas is reduced, the flue gas volume can be obviously reduced, the wet calcium method desulfurization efficiency and desulfurization rate of flue gas after the flue gas is carried out are improved, the specification requirements on equipment and fans in the calcium-carbon method flue gas desulfurization and denitrification device 100 can be reduced, and the equipment investment is reduced.
Further, in some embodiments, the temperature T1 of the flue gas discharged from the outlet 302 of the first heat exchange channel may satisfy: t1 is more than or equal to 90 ℃ and less than or equal to 110 ℃. Within the temperature range, the desulfurization efficiency of the flue gas in the wet calcium desulfurization device 10 is higher, and the desulfurization is more efficient.
In some embodiments of the present invention, the temperature of the flue gas discharged from the first flue gas outlet 102 is T2, and T2 satisfies: t2 is more than or equal to 50 ℃ and less than or equal to 55 ℃. For example, in some embodiments, T2 can be 52 ℃, 53 ℃, 54 ℃, 55 ℃, and the like. After the flue gas is desulfurized by the calcium method, the temperature is reduced from T1 to T2.
According to some embodiments of the utility model, the calcium-carbon method flue gas desulfurization and denitration device 100 further comprises a cooling device 50. The cooling device 50 is arranged between the first flue gas outlet 102 and the inlet 301 of the first heat exchange channel, flue gas is discharged from the first flue gas outlet 102 after being desulfurized by the wet calcium desulphurization device 10, and the flue gas contains water vapor which contains more pollutants. If the flue gas is directly discharged from a chimney, water vapor in the flue gas can be condensed to form wet smoke plume, so that the pollution to the atmosphere is caused. Therefore, by providing the temperature reducing device 50, the temperature reducing device 50 can remove dust and moisture contained in the flue gas discharged from the first flue gas outlet 102.
In some embodiments, the flue gas temperature after being cooled by the cooling device 50 is T3, and T3 satisfies: t3 is more than or equal to 40 ℃ and less than or equal to 60 ℃. For example, in some embodiments, T3 can be 42 ℃, 45 ℃, 50 ℃, 53 ℃, 58 ℃, etc. The temperature of the smoke is reduced from T2 to T3, so that the absolute moisture content of the white smoke can be reduced by the cooled smoke, and the preparation for the absolute moisture content removal of the white smoke is made.
Further, in some embodiments, the temperature T3 of the flue gas after being cooled by the cooling device 50 may satisfy: t3 is more than or equal to 45 ℃ and less than or equal to 50 ℃. Within the temperature range, dust and water vapor carried in the flue gas can be better removed.
In some embodiments, the temperature of the flue gas discharged from the outlet 304 of the second heat exchange channel is T4, and T4 satisfies: t4 is more than or equal to 70 ℃ and less than or equal to 120 ℃. For example, in some embodiments, T4 can be 75 ℃, 80 ℃, 85 ℃, 90 ℃, 98 ℃, 100 ℃, 105 ℃, 110 ℃, 115 ℃, etc. The heat exchange device 30 recovers the heat of the first heat exchange channel, transfers the heat to the second heat exchange channel, and increases the temperature of the flue gas in the second heat exchange channel, so that the temperature of the flue gas is increased from T3 to T4. Guarantee the flue gas temperature when getting into carbon-based catalyst denitrification facility 20, can more be close the temperature that the flue gas carries out the denitration reaction, better improvement the denitration effect of flue gas. Meanwhile, the absolute moisture content of the white smoke is reduced through the cooled smoke, and the temperature of the smoke is raised through the heat exchange device 30, so that the white smoke is always not in a saturated state in the ambient air and the diffusion process, water vapor in the white smoke cannot be separated out and condensed, and the white smoke elimination is effectively realized.
Further, in some embodiments, the temperature T4 of the flue gas exiting the outlet 304 of the second heat exchange channel may satisfy: t3 is more than or equal to 80 ℃ and less than or equal to 110 ℃. In the temperature range, the denitration effect of the flue gas is further improved.
In some embodiments of the present invention, the calcium-carbon flue gas desulfurization and denitration apparatus 100 further comprises: and a temperature increasing device 51. The temperature increasing device 51 is arranged between the outlet 304 of the second heat exchange channel and the second flue gas inlet 201. The flue gas discharged from the outlet 304 of the second heat exchange channel enters the temperature raising device 51 to raise the temperature of the flue gas, so that the flue gas reaches the optimal temperature for denitration reaction, and the flue gas can have better denitration efficiency during denitration. For example, the temperature increasing device 51 may be a heating furnace, a heat exchanger, or the like. The heating furnace adopts gas for heating, the temperature of furnace gas is higher, and the flue gas can be rapidly heated.
In some embodiments, the temperature of the flue gas after being heated by the heating device 51 is T5, and T5 satisfies: t5 is more than or equal to 80 ℃ and less than or equal to 120 ℃. For example, in some embodiments, T5 can be 85 ℃, 90 ℃, 98 ℃, 100 ℃, 105 ℃, 110 ℃, 115 ℃, etc. The temperature rising device 51 raises the temperature of the flue gas from T4 to T5, and the flue gas is subjected to medium-low temperature denitration at the temperature of T5, so that the operation is stable, and the denitration efficiency is high. In addition, the flue gas passes through heating device 51 and heats up the flue gas, and the flue gas temperature reaches T5, and the relative moisture content in the flue gas reduces, and when the flue gas was discharged to the external world, the flue gas can not become saturated state to can not form white cigarette.
Further, in some embodiments, the temperature T5 of the flue gas after being heated by the heating device 51 may satisfy: t3 is more than or equal to 85 ℃ and less than or equal to 110 ℃. In the above temperature range, the denitration efficiency of the flue gas in the carbon-based catalyst denitration device 20 can be made higher, and the denitration is more efficient.
In some embodiments, the calcium-carbon flue gas desulfurization and denitration device 100 further comprises an ammonia injection device 52. The ammonia injection device 52 is arranged between the temperature rising device 51 and the second flue gas inlet 201, so that the problems of blockage, corrosion and the like of the temperature rising device 51 caused by the ammonium bisulfite formed by ammonia injection are avoided. The ammonia spraying device 52 is used for spraying ammonia to the flue gas, the flue gas is discharged from the temperature rising device 51 and enters the ammonia spraying device 52, and the ammonia water and the flue gas are fully mixed. Then, the flue gas enters the carbon-based catalyst denitration device 20 through the second flue gas inlet 201, and the flue gas reacts with ammonia water in the presence of the carbon-based catalyst to perform denitration, so that purified gas can be obtained.
According to some embodiments of the utility model, carbon-based catalyst denitrification facility 20 still has analytic outlet 203, and wet calcium desulphurization unit 10 still has analytic gas inlet 103 with first exhanst gas outlet 102 intercommunication. The calcium-carbon flue gas desulfurization and denitrification device 100 further comprises an analysis device 60. The desorption device 60 is provided between the desorption outlet 203 and the desorption gas inlet 103. The carbon-based catalyst in the carbon-based catalyst denitration device 20 is periodically discharged through the desorption outlet 203 and enters the desorption device 60. The desorption device 60 is capable of desorbing and regenerating the carbon-based catalyst, discharging the sulfur-rich gas generated by desorption into the wet calcium desulfurization device 10 through the desorption gas inlet 103, desulfurizing the desorption gas by the wet calcium desulfurization device 10, and discharging the desulfurized desorption gas through the desorption gas inlet 103.
Of the remaining carbon-based catalyst in the analyzer 60, the carbon powder satisfying the particle size requirement can be returned to the carbon-based catalyst denitration device 20 for continuous use, and the carbon powder having a particle size smaller than that can be used as a fuel. For example, the analysis device 60 may be an analysis furnace. The resolving device 60 effectively solves the problem of the resolution of the carbon-based catalyst, and simultaneously retains the capability of the carbon-based catalyst to efficiently remove dioxin.
The following describes in detail the flue gas desulfurization and denitration apparatus 100 by calcium-carbon method according to an embodiment of the present invention with reference to the drawings, and it should be understood that the following description is only exemplary and should not be construed as limiting the present invention.
Referring to fig. 1, a calcium-carbon flue gas desulfurization and denitration apparatus 100 includes a wet calcium desulfurization apparatus 10, a carbon-based catalyst denitration apparatus 20, a heat exchange apparatus 30, a temperature reduction apparatus 50, a temperature increase apparatus 51, an ammonia injection apparatus 52, and an analysis apparatus 60.
The wet calcium desulfurization apparatus 10 has a first flue gas inlet 101 and a first flue gas outlet 102 that communicate with each other. The carbon-based catalyst denitration device 20 is used for denitration of flue gas, and the carbon-based catalyst denitration device 20 has a second flue gas inlet 201 and a second flue gas outlet 202 which are communicated with each other. The heat exchange device 30 has a first heat exchange channel and a second heat exchange channel, and the heat of the flue gas in the first heat exchange channel can be transferred to the flue gas in the second heat exchange channel. The outlet 302 of the first heat exchange channel is communicated with the first flue gas inlet 101, the inlet 303 of the second heat exchange channel is communicated with the first flue gas outlet 102, and the outlet 304 of the second heat exchange channel is communicated with the second flue gas inlet 201. The temperature reduction device 50 is disposed between the first flue gas outlet 102 and the inlet 301 of the first heat exchange channel. The temperature increasing device 51 is arranged between the outlet 304 of the second heat exchange channel and the second flue gas inlet 201. The ammonia injection device 52 is arranged between the temperature rising device 51 and the second flue gas inlet 201. The carbon-based catalyst denitration device 20 has a desorption outlet 203, the wet calcium desulfurization device 10 has a desorption gas inlet 103 communicating with the first flue gas outlet 102, and the desorption device 60 is provided between the desorption outlet 203 and the desorption gas inlet 103.
In the desulfurization and denitrification treatment process of the flue gas by the calcium-carbon flue gas desulfurization and denitrification device 100, the raw flue gas enters the first heat exchange channel through the inlet 301 of the first heat exchange channel to be cooled, and is discharged through the outlet 302 of the first heat exchange channel, and the flue gas discharge temperature is T1: t1 is more than or equal to 80 ℃ and less than or equal to 120 ℃. Flue gas through heat transfer device 30 cooling gets into wet calcium method desulphurization unit 10 through first flue gas inlet 101 to use wet calcium method to carry out desulfurization treatment to the flue gas in wet calcium method desulphurization unit 10, discharge by first exhanst gas outlet 102 again, flue gas exhaust temperature is T2: t1 is more than or equal to 50 ℃ and less than or equal to 55 ℃. The flue gas after desulfurization enters the temperature reduction device 50, the temperature reduction device 50 is used for reducing the temperature of the flue gas discharged from the first flue gas outlet 102, and the temperature after temperature reduction of the temperature reduction device 50 is T3: t3 is more than or equal to 40 ℃ and less than or equal to 60 ℃. Flue gas after the cooling of heat sink 50 gets into second heat transfer passageway from the import 303 of second heat transfer passageway to carry out the heat exchange with the flue gas in the first heat transfer passageway, realize rising temperature, the flue gas after the intensification is discharged by the export 304 of second heat transfer passageway again, and the temperature of exhaust flue gas is T4: t4 is more than or equal to 70 ℃ and less than or equal to 120 ℃. The flue gas after temperature rise enters the temperature rising device 51, the temperature rising device 51 is used for further raising the temperature of the flue gas discharged from the outlet 304 of the second heat exchange channel, and the temperature of the flue gas after temperature rise by the temperature rising device 51 is T5: t5 is more than or equal to 80 ℃ and less than or equal to 120 ℃. The flue gas heated by the temperature raising device 51 enters the ammonia spraying device 52 under the driving of the wind power of the fan, and the ammonia spraying treatment is carried out on the flue gas. The flue gas enters the carbon-based catalyst denitration device 20 through the second flue gas inlet 201 after being treated by ammonia spraying, activated carbon is selected as a carbon-based catalyst in the carbon-based catalyst denitration device 20, and the flue gas is subjected to denitration treatment by using an activated carbon catalytic denitration method to obtain purified gas. The cleaned gas is discharged from the second flue gas outlet 202 through a stack. The activated carbon in the carbon-based catalyst denitration device 20 is periodically discharged from the desorption outlet 203, enters the desorption furnace for desorption, sulfur-rich gas generated by desorption enters the wet calcium desulfurization device 10 through the desorption gas inlet 103 for treatment, and the treated gas can be discharged out of the wet calcium desulfurization device 10 through the first flue gas outlet 102. The carbon powder with small particle size can be used as fuel, and can be continuously returned to the carbon-based catalyst denitration device 20 for continuous use when the particle size requirement is met by processing the activated carbon analyzed in the analyzer 60.
Other configurations and operations of the calcium-carbon flue gas desulfurization and denitration apparatus 100 according to the embodiment of the present invention are known to those skilled in the art, and will not be described in detail herein.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In the description herein, references to the description of the terms "embodiment," "specific embodiment," "example," etc., mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
While embodiments of the present invention have been shown and described, it will be understood by those of ordinary skill in the art that: various changes, modifications, substitutions and alterations can be made to the embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the claims and their equivalents.

Claims (5)

1. The utility model provides a calcium charcoal method flue gas desulfurization denitrification facility which characterized in that includes:
the wet calcium desulphurization device is used for desulphurization of the flue gas and is provided with a first flue gas inlet and a first flue gas outlet which are communicated with each other;
the carbon-based catalyst denitration device is used for denitration of flue gas and is provided with a second flue gas inlet and a second flue gas outlet which are communicated with each other;
the heat exchange device is provided with a first heat exchange channel and a second heat exchange channel, wherein raw flue gas enters the first heat exchange channel through an inlet of the first heat exchange channel, an outlet of the first heat exchange channel is communicated with the first flue gas inlet, an inlet of the second heat exchange channel is communicated with the first flue gas outlet, an outlet of the second heat exchange channel is communicated with the second flue gas inlet, the second flue gas outlet is communicated with the outside so as to discharge treated flue gas, and the heat exchange device is arranged to transmit heat of the flue gas in the first heat exchange channel to the flue gas in the second heat exchange channel.
2. The calcium-carbon method flue gas desulfurization and denitrification apparatus according to claim 1, further comprising:
the cooling device is arranged between the first smoke outlet and the inlet of the first heat exchange channel, and is used for reducing the temperature of the smoke exhausted from the first smoke outlet.
3. The calcium-carbon method flue gas desulfurization and denitrification apparatus according to claim 1, further comprising:
and the temperature rising device is arranged between the outlet of the second heat exchange channel and the second flue gas inlet and is used for rising the temperature of the flue gas discharged from the outlet of the second heat exchange channel.
4. The calcium-carbon method flue gas desulfurization and denitrification apparatus according to claim 3, further comprising:
and the ammonia spraying device is arranged between the temperature rising device and the second flue gas inlet and is used for spraying ammonia to the flue gas.
5. The calcium-carbon flue gas desulfurization and denitration device according to claim 1, wherein the carbon-based catalyst denitration device further has a desorption outlet, the wet calcium desulfurization device further has a desorption gas inlet communicated with the first flue gas outlet, and the calcium-carbon flue gas desulfurization and denitration device further comprises:
and the analysis device is arranged between the analysis outlet and the analysis gas inlet and is used for analyzing the carbon base discharged from the analysis outlet and discharging the gas generated by analysis into the wet calcium desulphurization device through the analysis gas inlet to carry out calcium desulphurization.
CN202021663058.1U 2020-08-11 2020-08-11 Calcium-carbon method flue gas desulfurization and denitrification device Active CN214287485U (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115318081A (en) * 2022-08-12 2022-11-11 北京天地融创科技股份有限公司 Flue gas purification device and combustion device

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115318081A (en) * 2022-08-12 2022-11-11 北京天地融创科技股份有限公司 Flue gas purification device and combustion device

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