CN218741200U - Semi-dry treatment system for flue gas desulfurization and denitrification - Google Patents
Semi-dry treatment system for flue gas desulfurization and denitrification Download PDFInfo
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- CN218741200U CN218741200U CN202221936793.4U CN202221936793U CN218741200U CN 218741200 U CN218741200 U CN 218741200U CN 202221936793 U CN202221936793 U CN 202221936793U CN 218741200 U CN218741200 U CN 218741200U
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Abstract
The utility model relates to a system that semi-dry process was handled for flue gas desulfurization denitration belongs to flue gas purification technical field, including the denitration reaction tower that is arranged in making the nitrogen oxide reaction in the high temperature flue gas for make the generate liquid that contains ammonium sulfite form the concentrated tower of the supersaturated solution of ammonium sulfite, and be arranged in making the desulfurization absorption tower of the oxysulfide reaction in the low temperature flue gas, the lower part of denitration reaction tower and the I intercommunication of flue of high temperature flue gas, the well lower part of denitration reaction tower and the liquid outlet intercommunication of concentrated tower, the top of denitration reaction tower and the well lower part intercommunication of concentrated tower, the top of concentrated tower with desulfurization absorption tower intercommunication, the liquid outlet of desulfurization absorption tower with the well upper portion intercommunication of concentrated tower. Through adopting denitration reaction tower, concentrating tower and desulfurization absorption tower cooperation to use, realize that the high temperature flue gas satisfies the requirement of discharging after denitration and desulfurization.
Description
Technical Field
The utility model belongs to the technical field of flue gas purification, concretely relates to system that semi-dry process was handled for flue gas desulfurization denitration.
Background
With the rapid development of industrialization, the problem of atmospheric pollution is gradually highlighted. For example, flue gas generated in furnaces such as steel, cement, building materials, glass, metallurgy and the like contains a large amount of pollutants such as sulfur dioxide, nitrogen oxides, smoke dust and the like, which cause great harm to human health and ecological environment.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem that a system for semi-dry process treatment of flue gas desulfurization denitration is provided. The system does not use a catalyst during denitration, does not generate waste water, is beneficial to environmental protection and safety, can be used for other industries by the generated ammonium sulfate, and has higher efficiency and difficult blockage of equipment compared with wet desulphurization.
The utility model provides a solve above-mentioned technical problem and provide a system that semi-dry process was handled for flue gas desulfurization denitration, including the denitration reaction tower that is arranged in making the nitrogen oxide reaction in the high temperature flue gas, be used for making the concentration tower that contains the supersaturated solution of ammonium sulfite's formation liquid formation ammonium sulfite, be used for making the desulfurization absorption tower of the oxysulfide reaction in the low temperature flue gas, and be used for providing the urea of urea solution and join in marriage the liquid device, the lower part of denitration reaction tower and the I intercommunication of flue of high temperature flue gas, the well lower part of denitration reaction tower and the liquid outlet of concentration tower communicate, the top of denitration reaction tower and the well lower part of concentration tower intercommunication, the top of concentration tower with desulfurization absorption tower intercommunication, the liquid outlet of desulfurization absorption tower with the well upper portion of concentration tower intercommunication, urea joins in marriage liquid device (5) and desulfurization absorption tower (6) intercommunication.
The beneficial effect who adopts above-mentioned scheme is: through adopting denitration reaction tower, concentrating tower and desulfurization absorption tower cooperation to use, realize that the high temperature flue gas satisfies the requirement of discharging after denitration and desulfurization.
The denitration reaction tower is characterized by further comprising a cyclone separator, the top of the denitration reaction tower is communicated with the middle lower part of the concentration tower through a flue II, and the flue II is provided with the cyclone separator.
The beneficial effect of adopting the above further scheme is: most of ammonium sulfate and a small part of unreacted large solid particles of ammonium sulfite generated by denitration in the denitration reaction tower are removed from the medium-temperature flue gas through a cyclone separator.
Further, cyclone includes recovery feed bin and blanking storehouse, the recovery feed bin sets up the below of blanking storehouse, the top of blanking storehouse is through II and concentrated tower middle and lower part intercommunications of flue, the lateral wall of blanking storehouse is through II and denitration reaction tower middle and lower part intercommunications of flue.
The beneficial effect of adopting the further scheme is that: the recovery bin is arranged below the blanking bin, so that the ammonium sulfate and unreacted large solid particles of the ammonium sulfite can be collected.
Further, the denitration reaction tower comprises a denitration tower body, a tower bottom swirler and a solution atomizer; a tower bottom swirler is mounted at the middle lower part of the inner cavity of the denitration tower body, one end of the pipeline I extending to the inner cavity of the denitration tower body above the tower bottom swirler is connected with a solution atomizer, and the denitration tower body below the tower bottom swirler is communicated with a flue I; the top of the denitration tower body is communicated with the cyclone separator through a flue II.
The beneficial effect of adopting the further scheme is that: the denitration reaction tower adopts gas-liquid parallel flow contact, high-temperature flue gas and supersaturated solution of ammonium sulfite atomized by the solution atomizer flow upwards from the lower part of the tower, sufficient contact time and area of the gas and the liquid are ensured, the cyclone plate is arranged at the bottom of the tower, and the high-temperature flue gas generates rotation and centrifugal motion after passing through the cyclone plate, so that the gas and the liquid are fully contacted, and mass transfer reaction is carried out at the same time. The solution atomizer in the tower adopts a centrifugal pressure type atomizer, which is beneficial to the mass transfer reaction between the high-temperature flue gas and the solution and the water evaporation of liquid drops.
Further, the concentrating tower includes concentrated liquid pump, concentrated circulating pump, concentrate nozzle and concentrating tower body, the bottom of the inner chamber of concentrating tower body is provided with the concentrate chamber, the concentrate intracavity is provided with the pH meter, the liquid outlet of concentrating tower body passes through pipeline I and denitration tower body intercommunication, be provided with concentrated liquid pump on the pipeline I, the concentrating tower body passes through flue III and desulfurization absorption tower intercommunication, the concentrate chamber is connected with the one end of circulating pipe I, the other end of circulating pipe I extends to concentrate chamber top the intracavity of concentrating tower body, the other end of circulating pipe I is provided with the concentrate nozzle, be provided with the circulating pump on the circulating pipe I.
The beneficial effect of adopting the above further scheme is: the flow is adjusted through a circulating pump, and the concentration of the solution in the concentration tower is controlled to be saturated; the concentration tower adopts gas-liquid countercurrent contact, medium-temperature flue gas flows downwards from the upper part of the tower from bottom to top, and the gas-liquid has enough contact time and area; the gas and liquid phases may be strongly disturbed.
Further, the desulfurization absorption tower comprises a desulfurization liquid outlet pump, a desulfurization circulating pump, a packing layer, a demister, an absorption tower body and an absorption nozzle, a desulfurization liquid storage chamber, the packing layer and the demister are arranged on the inner cavity of the absorption tower body from bottom to top, the desulfurization liquid storage chamber is communicated with the concentration tower body through a pipeline II, the desulfurization liquid outlet pump is arranged on the pipeline II, the absorption tower body between the desulfurization liquid storage chamber and the packing layer is communicated with the concentration tower body through a flue III, the desulfurization liquid storage chamber is connected with one end of a circulating pipe II, the other end of the circulating pipe II extends to the inner cavity of the absorption tower body between the packing layer and the demister and is connected with the absorption nozzle, the top of the absorption tower body is connected with a flue IV, and a sulfur dioxide and nitrogen oxide analyzer is arranged on the flue IV.
The beneficial effect of adopting the further scheme is that: the absorption tower adopts gas-liquid pure two countercurrent contact, the low-temperature flue gas flows downwards from the upper part of the tower from bottom to top, and the urea solution is dispersed in a gas phase in a liquid drop shape; ensuring sufficient contact time and area of gas and liquid; gas-liquid two phases can be disturbed strongly, the operation range is wide, the operation is stable, and the resistance is small.
Furthermore, a booster fan is arranged on the flue I between the denitration reaction tower and the high-temperature flue gas, and another sulfur dioxide and nitrogen oxide analyzer is arranged on the flue I between the booster fan and the high-temperature flue gas inlet.
The urea solution preparation device comprises a solution tank, a conveying pump, a urea storage bin, a weighing machine and a stirrer, wherein the solution tank is communicated with the concentration tower and the desulfurization absorption tower through conveying pipelines respectively, the conveying pipeline is provided with the conveying pump, the solution tank is communicated with the urea storage bin through the weighing machine, and the stirrer is arranged in the solution tank.
The beneficial effect of adopting the above further scheme is: the flow is adjusted by a delivery pump, and the pH value in the solution of the concentration tower and the desulfurization absorption tower is controlled.
Furthermore, a sulfur dioxide and nitrogen oxide analyzer, a thermometer, a pressure gauge and an air gauge are installed at the inlet of the booster fan. And a thermometer, a pressure gauge and an air gauge are arranged on the flue I, the flue II, the flue III and the flue IV as required.
Drawings
FIG. 1 is a general schematic view of the present invention;
FIG. 2 is a schematic view of a bottom swirler of the present invention;
fig. 3 is a central blocking plate diagram of the tower bottom swirler of the utility model;
fig. 4 is a schematic view of the solution atomizer of the present invention.
In the drawings, the reference numbers indicate the following list of parts:
1-booster fan, 2-denitration reaction tower, 201-tower bottom cyclone, 202-solution atomizer, 203-denitration tower body, 3-cyclone separator, 301-recovery bin, 302-blanking bin, 4-concentration tower, 401-concentrated liquid pump, 402-concentrated circulating pump, 403-concentrated liquid nozzle, 404-concentration tower body, 405-circulating pipe I, 406-concentrated liquid cavity, 5-urea liquid distribution device, 501-solution tank, 502-conveying pump, 503-urea bin, 504-weighing machine, 505-stirrer, 506-conveying pipeline, 6-desulfuration absorption tower, 601-desulfuration liquid pump, 602-desulfuration circulating pump, 603-packing layer, 604-demister, 605-circulating pipe II, 606-absorption nozzle, 607-absorption tower body, 608-desulfuration liquid storage chamber, 7-desulfuration flue I, 8-flue II, 9-flue III, 10-IV flue, 11-pipeline I, 12-pipeline II.
Detailed Description
The principles and features of the present invention are described below, with the examples being given only for the purpose of illustration and not for the purpose of limiting the scope of the invention.
Example 1
The semi-dry treatment method for desulfurization and denitrification of flue gas in the embodiment comprises the following steps:
step 1: reacting sulfur oxides in the low-temperature flue gas with a urea solution to generate a generated liquid containing ammonium sulfite;
step 2: reacting the generated liquid containing ammonium sulfite in the step 1 with medium-temperature flue gas to form supersaturated solution of ammonium sulfite, and converting the medium-temperature flue gas into low-temperature flue gas for reuse in the step 1;
and step 3: and (3) in the step (2), the supersaturated solution of ammonium sulfite and the high-temperature flue gas are in parallel flow and mutually contacted, the supersaturated solution of ammonium sulfite is evaporated into solid particles, the ammonium sulfite in the solid particles reacts with nitric oxide in the high-temperature flue gas to generate ammonium sulfate solid particles, and the high-temperature flue gas is converted into medium-temperature flue gas to be reused in the step (2).
The sulfur oxide in the low-temperature flue gas reacts with the urea solution to generate a generated liquid containing ammonium sulfite, which meets the emission standardThe quasi low-temperature flue gas reaction is discharged; the generated liquid containing ammonium sulfite interacts with the medium-temperature flue gas and exchanges heat, water in the generated liquid containing ammonium sulfite is evaporated to improve the concentration of the solution, a supersaturated solution of ammonium sulfite is formed, the medium-temperature flue gas is further cooled and converted into low-temperature flue gas, and Nitrogen Oxides (NO) in the high-temperature flue gas X ) And in parallel with the sprayed supersaturated solution of the atomized ammonium sulfite, the liquid is rapidly evaporated in the high-temperature flue gas, is dried into solid particles, and simultaneously reacts with nitric oxide in the high-temperature flue gas to generate ammonium sulfate particles. Compared with the traditional desulfurization and denitrification processes, the process does not use a catalyst during denitrification, no waste water is generated, the process is beneficial to environmental protection and safety, the generated ammonium sulfate can be used in other industries, and the process has higher efficiency and is difficult to block equipment compared with wet desulfurization. The reaction involved in the whole process is as follows:
the main reaction equation for desulfurization absorption:
CO(NH) 2 +2H 2 O＝(NH 4 ) 2 CO 3 ；
(NH 4 ) 2 CO 3 +SO 2 ＝(NH 4 ) 2 SO 3 +CO 2 ；
(NH 4 ) 2 SO 3 +H 2 O+SO 2 ＝2NH 4 HSO 3 ；
2NH 4 HSO 3 +(NH 4 ) 2 CO 3 ＝2(NH 4 ) 2 SO 3 +CO 2 +H 2 O；
the main reaction equation of the denitration reaction:
2(NH 4 ) 2 SO 3 +2NO＝2(NH 4 ) 2 SO 4 +N 2 ；
4(NH 4 ) 2 SO 3 +2NO 2 ＝4(NH 4 ) 2 SO 4 +N 2 。
wherein the pH value in the urea solution in the step 1 is 6-7; in the step 2, the pH of the supersaturated solution of ammonium sulfite is adjusted by urea, and the pH is 7-8. The pH value of the urea solution is 6-7, so that the desulfurization absorption can be completely carried out, and partial sulfur oxides in the medium-temperature flue gas can be absorbed by adopting the pH value of the supersaturated solution of the urea ammonium sulfite.
Wherein the flow velocity of the high-temperature flue gas in the step 3 is 0.5-1m/s, the temperature is 80-100 ℃, and the time for the supersaturated solution of ammonium sulfite to contact with the high-temperature flue gas is 3-10s. By setting the flow speed of the high-temperature flue gas to be 0.5-1m/s, the temperature to be 80-100 ℃, and the time for the supersaturated solution of the ammonium sulfite to be in mutual contact with the high-temperature flue gas to be 3-10s, the supersaturated solution of the ammonium sulfite is evaporated into solid particles, and meanwhile, nitrogen oxides in the high-temperature flue gas are fully reacted with the ammonium sulfate solid particles.
Example 2
A system for semi-dry process treatment of flue gas desulfurization and denitration, as shown in fig. 1-4, comprising a denitration reaction tower 2 for reacting nitrogen oxides in high-temperature flue gas, a concentration tower 4 for forming supersaturated solution of ammonium sulfite from the generated liquid containing ammonium sulfite, a desulfurization absorption tower 6 for reacting sulfur oxides in low-temperature flue gas, and a urea solution preparation device 5 for providing urea solution, wherein the lower part of the denitration reaction tower 2 is communicated with a flue i 7 of high-temperature flue gas, the middle lower part of the denitration reaction tower 2 is communicated with a liquid outlet of the concentration tower 4, the top of the denitration reaction tower 2 is communicated with the middle lower part of the concentration tower 4, the top of the concentration tower 4 is communicated with the desulfurization absorption tower 6, the liquid outlet of the desulfurization absorption tower 6 is communicated with the middle upper part of the concentration tower 4, and the urea solution preparation device 5 is communicated with the desulfurization absorption tower 6.
As shown in fig. 1, the denitration reactor further comprises a cyclone separator 3, the top of the denitration reactor 2 is communicated with the middle lower part of the concentrating tower 4 through a flue II 8, the flue II 8 is provided with the cyclone separator 3, the cyclone separator 3 comprises a recovery bin 301 and a blanking bin 302, and the recovery bin 301 is arranged below the blanking bin 302. The cyclone 3 is used for removing large particle dust in the flue gas, and collecting part of unreacted raw materials. The collected material is sent to the recovery silo 301 through a star valve at the outlet of the blanking silo 302.
As shown in fig. 1 to 4, the denitration reaction tower 2 includes a denitration tower body 203, a tower bottom cyclone 201 and a solution atomizer; a tower bottom cyclone 201 is installed at the middle lower part of the inner cavity of the denitration tower body 203, one end of the pipeline I11 extending to the inner cavity of the denitration tower body 203 above the tower bottom cyclone 201 is connected with a solution atomizer 202, and the denitration tower body 203 below the tower bottom cyclone 201 is communicated with a flue I7; the top of the denitration tower body 203 is communicated with the cyclone separator 3 through a flue II 8. The supersaturated solution of ammonium sulfite sprayed into the denitration reaction tower 2 is atomized into fine droplets by the solution atomizer 202, and the fine droplets are rapidly evaporated in the high-temperature flue gas to form small crystals, and the small crystals are dried by the high-temperature flue gas to form solid particles containing ammonium sulfite, and simultaneously react with NOx in the high-temperature flue gas in the evaporation process to generate particles containing ammonium sulfate.
The concentration tower 4 adopted by the system adopts gas-liquid countercurrent contact, medium-temperature flue gas flows downwards from the upper part of the tower from bottom to top, and the concentration tower 4 has the basic requirements: ensuring sufficient contact time and area of gas and liquid; the gas phase and the liquid phase can be disturbed strongly, the operation range is wide, the operation is stable, and the resistance is small; has sufficient mechanical strength and corrosion resistance. It should be anticorrosive in the bottom of concentration tower body 404, the bottom links to each other with concentrated circulating pump 402 and concentrated liquid pump 401, adopts pressure type toper nozzle in the concentration tower body 404, keeps great liquid drop, prevents to form the mist, causes to be carried by the flue gas after the crystallization is appeared. The flow is adjusted by a concentration circulating pump 402, and the concentration of the solution in the concentration tower 4 is controlled to be saturated to form a supersaturated solution of ammonium sulfite; in addition, the flow is adjusted by a desulfurization liquid outlet pump 601, and the liquid level of the concentration tower 4 is controlled; the PH value of the solution in the concentration tower 4 is controlled between 7 and 8 by adjusting the flow rate through the delivery pump 502.
As shown in fig. 1, the concentration tower 4 includes a concentrated liquid outlet pump 401, a concentrated circulating pump 402, a concentrated liquid nozzle 403 and a concentration tower body 404, a concentrated liquid cavity 406 is provided at the bottom of an inner cavity of the concentration tower body 404, a pH meter and a thermometer are provided in the concentrated liquid cavity 406, a liquid outlet of the concentration tower body 404 is communicated with the denitration tower body 203 through a pipeline i 11, the concentrated liquid outlet pump 401 is provided on the pipeline i 11, the concentration tower body 404 is communicated with the desulfurization absorption tower 6 through a flue iii 9, the concentrated liquid cavity 406 is connected with one end of a circulating pipe i 405, the other end of the circulating pipe i 405 extends into the cavity of the concentration tower body 404 above the concentrated liquid cavity 406, the concentrated liquid nozzle 403 is provided at the other end of the circulating pipe i 405, and the circulating pump is provided on the circulating pipe i 405. The medium temperature flue gas containing a small amount of small particle dust enters a concentration tower 4, the medium temperature flue gas directly exchanges heat with a generated liquid containing ammonium sulfite, the temperature of the generated liquid containing ammonium sulfite in the concentration tower 4 is increased, the temperature of the medium temperature flue gas is reduced, ammonium sulfate and small ammonium sulfite particles in the medium temperature flue gas are condensed, cooled and dissolved in the generated liquid containing ammonium sulfite, the concentration of the concentrated liquid is increased to a saturated solution, and a supersaturated solution of ammonium sulfite is formed. The sulfur oxides in the flue gas can react with the generated solution containing ammonium sulfite, and urea is added to adjust the pH value to be 7-8, so that the ammonium sulfite has higher content.
The desulfurization absorption tower 6 adopted by the system adopts gas-liquid pure two countercurrent contacts, low-temperature flue gas flows downwards from the upper part of the tower from bottom to top and is dispersed in a gas phase in a liquid drop shape, and the desulfurization absorption tower 6 has the basic requirements: ensuring sufficient contact time and area of gas and liquid; the gas phase and the liquid phase can be disturbed strongly, the operation range is wide, the operation is stable, and the resistance is small; has sufficient mechanical strength and corrosion resistance. The bottom links to each other with desulfurization circulating pump 602 and desulfurization play liquid pump 601, adopts the multilayer to spout in the desulfurization absorption tower 6, and absorption nozzle 606 adopts pressure type toper nozzle, and the angle of spraying is big, even and difficult the jam, sends into absorption nozzle 606 department through the absorption liquid that desulfurization circulating pump 602 will contain the urea. The demister 604 is arranged at the top of the tower, and the integrated tubular dust and mist removing demister 604 is adopted, so that liquid drop carrying is reduced, the content of sulfate in clean low-temperature flue gas is reduced, and the demister 604 needs to be periodically washed by process water. The PH value of the solution in the concentration tower 4 is controlled between 7 and 8 by adjusting the flow rate through the delivery pump 502.
As shown in fig. 1, the desulfurization absorption tower 6 includes a desulfurization liquid pump 601, a desulfurization circulating pump 602, a packing layer 603, a demister 604, an absorption tower body 607 and an absorption nozzle 606, a desulfurization liquid storage chamber 608 is provided at the bottom of an inner cavity of the absorption tower body 607, another pH meter is provided in the desulfurization liquid storage chamber 608, the packing layer 603 is sequentially provided in the inner cavity of the absorption tower body 607 above the desulfurization liquid storage chamber 608, the desulfurization liquid storage chamber 608 is communicated with the concentration tower body 404 through a pipeline ii 12, the desulfurization liquid pump 601 is provided on the pipeline ii 12, the absorption tower body 607 between the desulfurization liquid storage chamber 608 and the packing layer 603 is communicated with the concentration tower body 404 through a flue iii 9, the desulfurization liquid storage chamber 608 is connected with one end of a circulating pipe 605 ii, the other end of the circulating pipe 605 ii extends to the inner cavity of the absorption tower body 607 between the packing layer 603 and the demister 604, and the other end of the circulating pipe 605 ii is connected with the absorption nozzle 606. The desulfurization absorption tower 6 further comprises a demister 604, the demister 604 is located in the inner cavity of the absorption tower body 607 above the packing layer 603, the top of the desulfurization absorption tower 6 is connected with a flue IV 10, and a sulfur dioxide and nitrogen oxide analyzer is arranged on the flue IV 10. The low-temperature flue gas after preliminary desulfurization and temperature reduction enters a desulfurization absorption tower 6 to be further desulfurized, the main component of desulfurization absorption liquid is mixed liquid containing ammonium sulfite and urea, an adsorption device is not arranged in the desulfurization absorption tower 6, the concentration and the pH value of the absorption liquid are controlled to be 7-8, and the desulfurization efficiency and ammonia escape qualification are ensured.
As shown in fig. 1, a booster fan 1 is arranged on a flue i 7 between the denitration reaction tower 2 and the high-temperature flue gas, and another sulfur dioxide and nitrogen oxide analyzer is arranged on the flue i 7 between the booster fan 1 and the high-temperature flue gas inlet. An outlet of the booster fan 1 is connected with an inlet air chamber of the denitration reaction tower 2 through a flue I7, and an inlet of the booster fan 1 is provided with a sulfur dioxide and nitrogen oxide analyzer, a thermometer, a pressure gauge and an air gauge.
As shown in fig. 1, the system for the semi-dry treatment method for flue gas desulfurization and denitration further includes a urea solution preparation device 5, the urea solution preparation device 5 includes a solution tank 501, a delivery pump 502, a urea bin 503, a weighing machine 504 and a stirrer 505, the solution tank 501 is respectively communicated with the concentration tower 4 and the desulfurization absorption tower 6 through a delivery pipe 506, the delivery pipe 506 is provided with the delivery pump 502, the solution tank 501 is communicated with the urea bin 503 through the weighing machine 504, and the stirrer 505 is arranged in the solution tank 501.
As shown in figure 1, a temperature meter, a pressure meter and an air gauge are further arranged on the flue I7, the flue II 8, the flue III 9 and the flue IV 10 as required.
The working process of the system for semi-dry treatment of flue gas desulfurization and denitrification comprises the following steps:
(1) After the system is ready, 30-40% of urea solution is prepared in the urea solution tank 501, the urea solution with a certain liquid level is fed into the desulfurization absorption tower 6, and then the desulfurization circulating pump 602 is started to start the circulation of the absorption liquid formed by the urea solution.
(2) And starting the booster fan 1, introducing high-temperature flue gas to carry out system temperature rise, and simultaneously adjusting the air quantity and pressure of the system to ensure that the micro-positive pressure in the denitration reaction tower 2 is 2-5KPa and the flow rate is 0.5-1m/s.
(3) When the pH of the absorption liquid in the desulfurization absorption tower 6 is 6-7, a desulfurization liquid outlet pump 601 of the desulfurization absorption tower 6 is started to send the solution to the concentration tower 4, a concentration circulating pump 402 is started after the liquid level reaches, the pH of the concentration tower 4 is controlled to be 7-8, when the solution is close to saturation or has solid content, a supersaturated solution of ammonium sulfite is formed, a concentration discharge pump is started to feed the liquid into the denitration reaction tower 2, and the temperature in the denitration reaction tower 2 is controlled to be 80-100 ℃.
(4) According to the nitrogen oxide concentration of the clean flue gas at the outlet of the system, the feeding amount of the denitration reaction tower 2 is adjusted, and meanwhile, a material dropping port star valve of the material dropping bin 302 of the cyclone separator 3 is started to discharge the materials.
To sum up, the utility model discloses a flue gas processing system can detach the harmful substance that contains sulphur and nitrogen in the flue gas effectively, and the sulfur dioxide clearance reaches more than 99%, and the nitrogen oxide clearance is more than 70%, reduces the risk that the fume emission harmed the environment from this. The utility model discloses a processing system's simple structure, it is easy to make, uses safe and reliable, and the implementation of being convenient for is popularized and applied. The process can be shortened, the investment cost is reduced, the product sodium sulfate of desulfurization and denitrification can be used for other industrial raw materials without evaporation, crystallization and filtration, no wastewater is discharged, and the method has certain practical application prospect.
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 orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description of the present invention and to simplify the description, but 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 present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly, e.g., as being fixedly connected, detachably connected, or integrated; can be mechanically or electrically connected; they may be directly connected or indirectly connected through intervening media, or they may be connected internally or in any other suitable relationship, unless expressly stated otherwise. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.
Although embodiments of the present invention have been shown and described, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art without departing from the scope of the present invention.
Claims (8)
1. The system for semi-dry treatment of the flue gas desulfurization and denitrification is characterized by comprising a denitrification reaction tower (2) for reacting nitrogen oxides in high-temperature flue gas, a concentration tower (4) for enabling a generated liquid containing ammonium sulfite to form a supersaturated solution of the ammonium sulfite, a desulfurization absorption tower (6) for reacting the sulfur oxides in low-temperature flue gas, and a urea solution preparation device (5) for providing a urea solution, wherein the lower part of the denitrification reaction tower (2) is communicated with a flue I (7) of the high-temperature flue gas, the middle lower part of the denitrification reaction tower (2) is communicated with a liquid outlet of the concentration tower (4), the top of the denitrification reaction tower (2) is communicated with the middle lower part of the concentration tower (4), the top of the concentration tower (4) is communicated with the desulfurization absorption tower (6), the liquid outlet of the desulfurization absorption tower (6) is communicated with the middle upper part of the concentration tower (4), and the urea solution preparation device (5) is communicated with the desulfurization absorption tower (6).
2. The system for semi-dry treatment of desulfurization and denitrification of flue gas according to claim 1, further comprising a cyclone separator (3), wherein the top of the denitrification tower (2) is communicated with the middle lower part of the concentration tower (4) through a flue II (8), and the cyclone separator (3) is arranged on the flue II (8).
3. The system for semi-dry treatment of desulfurization and denitrification of flue gas according to claim 2, wherein the cyclone separator (3) comprises a recovery bin (301) and a blanking bin (302), the recovery bin (301) is arranged below the blanking bin (302), the top of the blanking bin (302) is communicated with the middle lower part of the concentration tower (4) through a flue II (8), and the side wall of the blanking bin (302) is communicated with the middle lower part of the denitrification reaction tower (2) through the flue II (8).
4. The system for semi-dry process treatment of desulfurization and denitrification of flue gas according to claim 2, wherein the denitrification reaction tower (2) comprises a denitrification tower body (203), a tower bottom cyclone (201) and a solution atomizer (202); a tower bottom swirler (201) is installed at the middle lower part of the inner cavity of the denitration tower body (203), one end of a pipeline I (11) extending to the inner cavity of the denitration tower body (203) above the tower bottom swirler (201) is connected with a solution atomizer (202), and the denitration tower body (203) below the tower bottom swirler (201) is communicated with a flue I (7); the top of the denitration tower body (203) is communicated with the cyclone separator (3) through a flue II (8).
5. The system for semi-dry treatment of desulfurization and denitrification of flue gas according to claim 4, wherein the concentration tower (4) comprises a concentration liquid outlet pump (401), a concentration circulating pump (402), a concentration liquid nozzle (403) and a concentration tower body (404), a concentration liquid cavity (406) is arranged at the bottom of an inner cavity of the concentration tower body (404), a liquid outlet of the concentration tower body (404) is communicated with the denitrification tower body (203) through a pipeline I (11), the concentration liquid outlet pump (401) is arranged on the pipeline I (11), the concentration tower body (404) is communicated with the desulfurization absorption tower (6) through a flue III (9), the concentration liquid cavity (406) is connected with one end of a circulating pipe I (405), the other end of the circulating pipe I (405) extends into the cavity of the concentration tower body (404) above the concentration liquid cavity (406), the concentration liquid nozzle (403) is arranged at the other end of the circulating pipe I (405), and the concentration circulating pump (402) is arranged on the circulating pipe (405).
6. The system for semi-dry treatment of flue gas desulfurization and denitration according to claim 5, wherein the desulfurization absorption tower (6) comprises a desulfurization liquid outlet pump (601), a desulfurization circulating pump (602), a packing layer (603), a demister (604), an absorption tower body (607) and an absorption nozzle (606), a desulfurization liquid storage chamber (608), the packing layer (603) and the demister (604) are arranged in the inner cavity of the absorption tower body (607) from bottom to top, the desulfurization liquid storage chamber (608) is communicated with the concentration tower body (404) through a pipeline II (12), the desulfurization liquid outlet pump (601) is arranged on the pipeline II (12), the absorption tower body (607) between the desulfurization liquid storage chamber (608) and the packing layer (603) is communicated with the concentration tower body (404) through a flue III (9), the desulfurization liquid storage chamber (608) is connected with one end of a circulating pipe II (605), the other end of the circulating pipe II (605) extends to the inner cavity of the absorption tower body (607) between the packing layer (603) and the packing layer (603), the absorption nozzle (606) is connected with an absorption tower body (607), and a nitrogen oxide analyzer (10) and a flue IV) are arranged on the top of the absorption tower (607).
7. The system for semi-dry treatment of flue gas desulfurization and denitration according to claim 6, wherein a pH meter is disposed in the concentrate chamber (406), and another pH meter is disposed in the desulfurization liquid storage chamber (608).
8. The semi-dry treatment system for desulfurization and denitrification of flue gas according to any one of claims 1 to 7, wherein a booster fan (1) is arranged on the flue I (7), and another sulfur dioxide and nitrogen oxide analyzer is arranged on the flue I (7) on the side of the booster fan (1) far away from the denitrification reaction tower (2).
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| CN115055035A (en) * | 2022-07-26 | 2022-09-16 | 北京清新环境技术股份有限公司 | Semi-dry treatment method and system for flue gas desulfurization and denitrification |
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