CN209828700U - Wet deacidification device for incineration flue gas - Google Patents
Wet deacidification device for incineration flue gas Download PDFInfo
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- CN209828700U CN209828700U CN201822233835.8U CN201822233835U CN209828700U CN 209828700 U CN209828700 U CN 209828700U CN 201822233835 U CN201822233835 U CN 201822233835U CN 209828700 U CN209828700 U CN 209828700U
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Abstract
The utility model relates to an incineration flue gas wet deacidification device, which comprises a cooling tower, a wet washing tower, an acid mist condenser and a flue gas reheater, wherein the cooling tower, the wet washing tower, the acid mist condenser and the flue gas reheater are connected in sequence through pipelines; the wet washing tower is provided with an inner tower circulating liquid tank, a gas inlet, a gas distributor, a filler, a spraying system, a gas distributor, a demisting layer and a gas outlet from bottom to top; the spraying system and the tower internal circulation liquid tank are respectively communicated with the tower external circulation liquid tank; the cooling tower is a double-layer falling film wet wall tower; the acid mist condenser is a horizontal tower, and is provided with a spraying system capable of spraying relatively. The utility model realizes high-efficiency wet deacidification through stable absorption and dehumidification and demisting of the filler, has emission reduction effect on water vapor, acid mist, salt mist and solid particles, and contributes to reducing haze; in addition, the aim of not generating white smoke at the discharge port is achieved through the cooling and dehumidifying of the wet washing tower, the small liquid drop condensation of the acid mist condenser and the heating of the flue gas reheater.
Description
Technical Field
The utility model relates to an environmental protection field especially relates to an burn flue gas wet process deacidification device.
Background
The traditional mode of solid waste (including garbage or hazardous waste) incineration plants is a semidry method, a dry method and a smoke white elimination device to remove harmful substances to reach the emission standard and eliminate white smoke during emission. However, as the environmental protection requirements become more stringent, the method cannot meet the process requirements. The important pollutant in the flue gas of solid waste incineration is SO2And other acid substances such as HCL and HF. In recent years, wet deacidification technology is applied more and more in the aspect of burning and harming solid wastes (garbage and hazardous wastes), but the wet deacidification technology is mostly applied in the initial application stage, and the emission effect and the white smoke elimination (white smoke discharge) effect are both required to be improved. Therefore, the utility model aims to solve the problem of providing an incineration flue gas wet deacidification device with high emission standard and good whitening effect.
Disclosure of Invention
The utility model aims to overcome the weak point of prior art, provide a flue gas wet process deacidification device burns that emission standard is high, white effectual disappears.
In order to achieve the above purpose, the utility model adopts the technical scheme that: the utility model provides an incineration flue gas wet process deacidification device which characterized in that: the system comprises a cooling tower, a wet-type washing tower, an acid mist condenser and a flue gas reheater which are sequentially connected through pipelines; the wet washing tower is internally provided with an inner circulating liquid tank, a gas inlet, a primary gas distributor, a filler, a first spraying system, a secondary gas distributor, a primary demisting layer, a secondary demisting layer and a gas outlet from bottom to top; the first-stage gas distributor and the second-stage gas distributor respectively comprise a permeable cylinder body with a cover umbrella at the top and a tower plate, and the tower plate partitions the tower body and is provided with a water outlet; the water outlet of the primary gas distributor is communicated with a circulating liquid tank outside the tower through a pipeline; the tower external circulation liquid tank is also respectively communicated with the first spraying system and the tower internal circulation liquid tank through a circulation pipeline, and a heat exchanger is arranged on the circulation pipeline; the cooling tower is a double-layer falling film wet wall tower and comprises an outer wall, an inner wall, a second spraying system and a gas cooling cavity; the gas cooling cavity is arranged in the inner wall; an auxiliary cooling cavity is arranged in an interlayer between the outer wall and the inner wall, and at least one overflow port is arranged at the upper end of the inner wall; the second spraying system is communicated with a tower internal circulation liquid tank of the wet washing tower through a pipeline; the lower part of the auxiliary cooling cavity is communicated with a tower internal circulation liquid tank of the wet scrubber tower through a pipeline; the acid mist condenser is a horizontal tower and is provided with a plurality of main demisters; the main demister comprises a demisting layer and a third spraying system which is arranged on the left side and the right side of the demisting layer and points to the demisting layer.
As a preferable scheme, the cooling tower comprises a high-temperature gas inlet communicated with the top of the gas cooling cavity and a low-temperature gas-liquid outlet communicated with the bottom of the gas cooling cavity; and an inverted cone-shaped maintenance emptying port is also arranged at the bottom of the auxiliary cooling cavity of the cooling tower.
As a preferable scheme, a terminal demister is further arranged at the position, close to the outlet, of the acid mist condenser; the terminal demister comprises a demisting layer and a third spraying system which is arranged on one side of the terminal demister, is far away from the outlet of the acid mist condenser and is directed to the demisting layer.
Preferably, the packing is composed of a plurality of structured packing units, and the packing units are provided with a plurality of fine columnar protrusions extending towards the interior of the packing units.
More preferably, the protrusions are cones having hemispherical ends.
Preferably, the hollow parts of the cylinders of the primary gas distributor and the secondary gas distributor penetrate through the corresponding tower plates and are communicated with the inner space of the tower body.
As a preferred scheme, the primary defogging layer is a PP folded plate, and the secondary defogging layer is a PP wire mesh; and reverse spraying systems are arranged at the lower parts of the first-stage demisting layer and the second-stage demisting layer.
As a preferred scheme, the system also comprises an induced draft fan arranged between the acid mist condenser and the flue gas reheater.
The utility model discloses a theory of operation:
1. firstly, burning flue gas with high temperature is put into a cooling tower to be contacted with alkaline circulating liquid for cooling, so that the temperature is reduced to 70-80 ℃; then carrying out alkali neutralization absorption and cooling dehumidification on the filler in the wet washing tower and sprayed alkaline circulating liquid (such as 30wt% NaOH solution), neutralizing acidic substances in the wet washing tower and preliminarily removing water mist (removing liquid drops more than 10 mu m); then, condensing in an acid mist condenser outside the tower through a main demister to remove liquid drop particles and solid particles with the size less than 10 um; sending the purified low-temperature low-humidity flue gas into a flue gas reheater, heating to above acid dew point, and finally discharging from an exhaust pipe, wherein the discharged flue gas contains SO2Less than 50mg/M3HCL content of less than 10mg/M3Containing less than 1mg/M of HF3And the functions of ultralow emission and no white smoke are realized.
2. The utility model discloses set up tower inner loop liquid case and tower outer loop liquid case. Wherein, the alkaline circulating liquid in the circulating liquid tank of the wet-type washing tower is conveyed to a second spraying system and an auxiliary cooling cavity of the cooling tower through a circulating pump; the spraying system sprays out the alkaline circulating liquid and cools the high-temperature incineration flue gas; the alkaline circulating liquid in the auxiliary cooling cavity overflows from the overflow port, and a continuously flowing and updated protective wet film is formed on the inner side of the inner wall of the cooling tower to assist in cooling the incineration flue gas and protect the tower body of the cooling tower; then the alkaline circulating liquid enters a wet washing tower together with the flue gas through a pipeline and falls into a circulating liquid tank in the tower again; the alkaline circulating liquid can be cooled and radiated through the pipeline when passing through the pipeline, so that the burden of subsequent cooling is reduced.
After the temperature of the alkaline circulating liquid in the tower external circulating liquid tank is controlled to be 45-50 ℃ through the heat exchanger, the alkaline circulating liquid is sprayed down through a first spraying system of the wet washing tower to wash and cool the flue gas, then the alkaline circulating liquid and the moisture condensed due to the temperature reduction of the flue gas flow back to the tower external circulating liquid tank from the tower plate, then the alkaline circulating liquid is cooled through the heat exchanger, one part of the alkaline circulating liquid is conveyed to the first spraying system again, the other part of the alkaline circulating liquid is conveyed to the tower internal circulating liquid tank, and the proportion of the alkaline circulating liquid and the moisture can be flexibly controlled according to actual.
The utility model has the advantages of: provides a wet deacidification device for incineration flue gas with high emission standard and good whitening effect.
1. The utility model discloses a stable absorption and dehumidification defogging of filler realize high efficiency wet process deacidification, and the row's mouth ultralow emission: containing SO2Less than 50mg/M3HCL content of less than 10mg/M3Containing less than 1mg/M of HF3Can reach the European Union emission standard and is far lower than the domestic standard.
2. The utility model discloses desorption SO2The efficiency of the method is more than 99.5 percent, the method has emission reduction effect on water vapor, acid mist, salt mist and solid particles, and the substances are not measured in the current emission standard but are also important causes of environmental pollution. The event the utility model discloses contribute to reducing the haze, be favorable to the protection of environment.
3. The utility model discloses a wet scrubbing tower's cooling dehumidification, acid mist condenser's little drop condense and the heating of flue gas reheater, reach the purpose that the discharge port does not produce white cigarette.
4. The device skillfully connects the tower internal circulation liquid tank of the wet washing tower with the cooling device of the cooling tower, so that the whole structure is more compact and simpler.
5. The utility model discloses wet-type scrubbing tower's cooling dehumidification effect is obvious to obtain a large amount of dehumidification water, and supply alkaline circulation liquid, reduce the addition of external make-up water, practiced thrift the water resource.
Drawings
The present invention will be further explained with reference to the drawings and examples.
Fig. 1 is a schematic structural diagram of a preferred embodiment of the present invention.
Fig. 2 is a schematic structural diagram of a cooling tower according to a preferred embodiment of the present invention.
Fig. 3 is a schematic structural view of a wet scrubber tower according to a preferred embodiment of the present invention.
Fig. 4 is a schematic structural diagram of an acid mist condenser according to a preferred embodiment of the present invention.
Fig. 5 is a schematic front view of a packing unit according to a preferred embodiment of the present invention.
Fig. 6 is a schematic top view of the packing unit according to the preferred embodiment of the present invention.
Fig. 7 is an external view schematically showing a thin columnar protrusion according to a preferred embodiment of the present invention.
In the figure: 1 is a cooling tower, 10 is an emergency spray system, 11 is an outer wall, 12 is an inner wall, 13 is a second spray system, 14 is a gas cooling cavity, 15 is an auxiliary cooling cavity, 151 is a liquid inlet, 16 is an overflow port, 17 is a high-temperature gas inlet, 18 is a low-temperature gas-liquid outlet, 19 is a maintenance evacuation port, 2 is a wet washing tower, 21 is an in-tower circulation liquid tank, 22 is a gas inlet, 23 is a primary gas distributor, 24 is a filler, 241 is a filler unit, 241a is a columnar protrusion, 241b is a hollowed-out sheet layer, 25 is a first spray system, 26 is a secondary gas distributor, 27 is a primary demisting layer, 28 is a secondary demisting layer, 29 is a gas outlet, 3 is an acid mist condenser, 31 is a main demister, 311 is a demisting layer of the acid mist condenser, 312 is a third spray system, 32 is a terminal demister, 4 is a flue gas demister, 5 is a draft fan, 6 is an exhaust pipe, and, 71 is a cylinder, 72 is a tower plate, 73 is a water outlet, 74 is a reverse spraying system, 8 is an external circulating liquid tank of the tower, 91 is a circulating pipeline, 911 is a first circulating pump, 912 is a heat exchanger, 92 is a conveying pipeline, and 921 is a second circulating pump.
Detailed Description
The present invention will now be described in further detail with reference to the accompanying drawings and examples, which are given by way of illustration only, not limitation, and are not intended to limit the scope of the invention. The structures, connections and methods not described in detail in the present application are all understood to be common general knowledge in the art.
As shown in fig. 1-7, a wet deacidification device for incineration flue gas is characterized in that: the device comprises a cooling tower 1, a wet type washing tower 2, an acid mist condenser 3, a draught fan 5, a flue gas reheater 4 and an exhaust pipe 6, wherein the six are sequentially connected through pipelines.
The cooling tower 1 is an FRP hollow cylinder. By adopting the FRP high temperature resistant and acid and alkali resistant glass fiber reinforced plastics, the high temperature resistant and acid and alkali resistant effects of the cooling tower 1 are improved.
The cooling tower 1 is a double-layer falling film wet wall tower and comprises an outer wall 11, an inner wall 12, a second spraying system 13, a gas cooling cavity 14, an auxiliary cooling cavity 15, a high-temperature gas inlet 17 and a low-temperature gas-liquid outlet 18; the space surrounded by the inner wall 12 is a gas cooling cavity 14, and an auxiliary cooling cavity 15 is arranged in an interlayer between the outer wall 11 and the inner wall 12; at least one overflow opening 16 is provided at the upper end of the inner wall 12. The high-temperature gas inlet 17 is communicated with the top of the gas cooling cavity 14, and the low-temperature gas-liquid outlet 18 is communicated with the bottom of the gas cooling cavity 14. The auxiliary cooling chamber 15 is provided to assist the cooling of the second spraying system 13 and protect the tower body of the cooling tower 1. The lower part of the auxiliary cooling cavity 15 is provided with a liquid inlet 151 for injecting alkaline circulating liquid for cooling and washing incineration flue gas; with the increase of the injection amount, the liquid level rises, and finally the alkaline circulating liquid fills the auxiliary cooling cavity 15 and overflows from the overflow port 16 to enter the gas cooling cavity 14; the alkaline circulating liquid flows downwards along the inner side of the inner wall 12 to form a constantly flowing and renewed protective wet film. This protection wet film can assist second spraying system 13 to cool down and wash the flue gas with burning the flue gas contact, reduces the spraying dead angle that second spraying system 13 probably produced, increases the time of alkaline circulation liquid and high temperature burning flue gas contact to improve refrigerated effect and efficiency. Meanwhile, the tower body of the cooling tower 1 can be protected from being damaged by high temperature, and the service life of the cooling tower 1 is prolonged.
The bottom of the auxiliary cooling cavity 15 of the cooling tower 1 is provided with an inverted cone-shaped maintenance evacuation port 19. The maintenance of the cooling tower 1 is facilitated through the maintenance evacuation port 19, the maintenance of daily equipment is facilitated, and the service life of the equipment is further prolonged; the maintenance emptying port 19 adopts an inverted cone design, which is not only beneficial to sealing the maintenance emptying port 19 when the maintenance emptying port 19 is not used, but also does not influence the emptying efficiency of the maintenance emptying port 19 during maintenance. In addition, the cooling tower 1 is also provided with an emergency spraying system 10 communicated with an external water source for increasing the cooling force when the gas temperature is overhigh or in other emergency situations.
The wet scrubber tower 2 is internally provided with a tower internal circulation liquid tank 21, a gas inlet 22, a primary gas distributor 23, a filler 24, a first spraying system 25, a secondary gas distributor 26, a primary demisting layer 27, a secondary demisting layer 28 and a gas outlet 29 from bottom to top. The gas inlet 22 of the wet scrubber tower 2 is communicated with the low-temperature gas-liquid port 18 of the cooling tower 1 through a pipeline.
The first-stage gas distributor 23 and the second-stage gas distributor 26 both comprise a permeable cylinder 71 and a tower plate 72, the tops of which are provided with cover umbrellas, and the side walls of which are provided with gas outlets, and the hollow parts of the cylinder 71 penetrate through the reserved openings of the corresponding tower plate 72 and are communicated with the inner space of the tower body. The tray 72 is fixed to the tower wall to partition the wet scrubber tower 2, and the tray 72 is provided with a drain opening 73. The arrangement of the first-stage gas distributor 23 and the second-stage gas distributor 26 can ensure that the incineration flue gas passing through the structure is distributed more uniformly in the tower, thereby being more beneficial to the contact of alkaline circulating liquid and the incineration flue gas and improving the alkaline washing and cooling effects of the incineration flue gas.
The first-stage defogging layer 27 is a PP folded plate, and the second-stage defogging layer 28 is a PP wire mesh. The lower parts of the first and the second demisting layers are provided with a reverse second spraying system 134 communicated with an external water source and used for spraying the liquid drops condensed by the first-stage demisting layer 27 and the second-stage demisting layer 28.
The packing 24 is composed of a plurality of regular packing units 241, and the material of the packing units 241 is polyvinylidene fluoride. The packing unit 241 has a rectangular frame structure, and a plurality of hollow sheets 241b are disposed at the top, bottom and inside of the packing unit. A plurality of thin columnar protrusions 241a are arranged on the lower surface of the hollowed-out sheet layer 241b at the top of the filling unit 241; a plurality of thin columnar protrusions 241a are arranged on the upper surface of the hollowed-out sheet layer 241b at the bottom of the filling unit 241; the upper surface and the lower surface of the hollow sheet layer 241b inside the packing unit 241 are both provided with a plurality of thin columnar protrusions 241a (that is, the hollow sheet layer 241b is provided with a plurality of thin columnar protrusions 241a extending towards the inside of the packing unit 241). The protrusion 241a is a cone having a hemispherical end (i.e., a thick end at the bottom is thin). The design of the packing unit 241 increases the contact area of gas and liquid, so that the packing 24 has a high surface area and a high open volume, greatly reduces pressure drop, and increases mass transfer efficiency, thereby improving washing and cooling efficiency, reducing the tower diameter of the wet-type washing tower 2, reducing energy consumption, and saving energy and cost. In addition, the rectangular frame structure is more beneficial to the stacking of the packing units 241, so that the packing 24 can not be nested with each other after the equipment is operated, and the efficiency can not be reduced or short flow can not be generated. Meanwhile, the vinylidene fluoride material is selected to enable the filler 24 to be more resistant to high temperature and chemical substances. The end of the thin cylindrical protrusion 241a is designed to be semi-spherical, which is more beneficial to increase the gas/liquid contact area.
The device is also provided with an external tower circulating liquid tank 8, and the external tower circulating liquid tank 8 is communicated with an external water source and an alkali liquor source. Meanwhile, the tower external circulation liquid tank 8 is also communicated with the first spraying system 25 and the tower internal circulation liquid tank 21 through a circulation pipeline 91, and a first circulation pump 911 and a heat exchanger 912 are arranged on the circulation pipeline 91. The water outlet 73 of the other stage gas distributor 23 is also communicated with the tower external circulation liquid tank 8 through a pipeline. Set up outer circulation liquid case 8 of tower and store the alkaline circulating liquid that is used for wet scrubbing tower 2, compare in conventional design, because pipeline cooling effect is better than in the tower/in the device cooling effect, so alkaline circulating liquid once has carried out the cooling when getting back to outer circulation liquid case 8 of tower through the pipeline to the burden of heat exchanger 912 has been alleviateed.
The second spraying system 13 and the auxiliary cooling cavity 15 of the cooling tower 1 are respectively communicated with the internal circulation liquid tank 21 of the wet scrubber tower 2 through a conveying pipeline 92, and the conveying pipeline 92 is provided with a second circulation pump 921. The auxiliary cooling chamber 15 is communicated with the circulating liquid tank 21 in the tower through a liquid inlet 151 arranged at the lower part of the auxiliary cooling chamber. The alkaline circulating liquid is provided for the cooling tower 1 by utilizing the tower internal circulating liquid tank 21, the equipment structure is fully utilized, the cooling tower 1 and the wet type washing tower 2 are more closely connected, and the whole device is simpler and more compact in structure. In addition, the maintenance emptying port 19 can also be communicated with an internal tower circulating liquid tank 21 of the wet washing tower 2 through a pipeline and is used for emptying alkaline circulating liquid during maintenance.
The acid mist condenser 3 is a horizontal tower and is provided with a two-stage main demister 31; the main demister 31 comprises a demisting layer 311 and third spraying systems 312 which are arranged at the left and right sides of the demisting layer 311 and point to the demisting layer 311; the spray system 312 of the main mist eliminator 31 can spray relatively clean water, thereby increasing the humidity near the mist elimination layer 311, creating an oversaturated environment in the region. When the incineration flue gas passes through the demisting layer 311 of the main demister 31, tiny acid mist droplets in the incineration flue gas grow into 10-micron-level tiny acid mist droplets due to the nuclear condensation and aggregation process, so that the tiny acid mist droplets are easily intercepted and condensed by the demisting layer 311; meanwhile, along with the increase of the relative humidity of the environment, the gibbs energy corresponding to the solid particulate matter solution in the incineration flue gas becomes smaller, so that the solid particles absorb the moisture in the environment and become larger (the moisture absorption of the particles is increased), and the particulate matters with the larger sizes are easily condensed on the defogging layer 311.
A terminal demister 32 is also arranged at the position, close to the outlet, of the acid mist condenser 3; the terminal mist eliminator 32 comprises a mist eliminating layer 311 and a third spraying system 312 which is arranged on the side thereof away from the outlet of the acid mist condenser 3 and directed to the mist eliminating layer 311. The end mist eliminator 32 can be used to further coalesce, remove, and enhance the removal of acid mist droplets and solid particles. The third spray system 312 is connected to an outside water source. The defogging layer 311 is a wire mesh defogging layer.
The flue gas reheater 4 is a conventional device for flue gas heating, such as a steam heater or the like.
A flue gas deacidification process using the incineration flue gas wet deacidification device comprises the following steps:
1. under the action of the induced draft fan 5, the high-temperature incineration flue gas (the temperature is more than 180 ℃ and the SO is contained)2HCL, HF) enters the cooling tower 1 from the high-temperature gas inlet 17 and moves from top to bottom, and the flow rate entering the cooling tower 1 is 5 m/s.
Meanwhile, the second circulation pump 921 delivers the alkaline circulation liquid (e.g., a 30% NaOH solution) of the in-tower circulation liquid tank 21 of the wet scrubber tower 2 to the second spraying system 13 and the auxiliary cooling chamber 15 through the delivery pipe 92. The second spraying system 13 sprays out the alkaline circulating liquid, contacts with the high-temperature incineration flue gas, cools the high-temperature incineration flue gas, and performs primary washing; meanwhile, alkaline circulation liquid is injected into the auxiliary cooling cavity 15, the liquid level rises along with the increase of the injection amount, and finally the alkaline circulation liquid is filled in the auxiliary cooling cavity 15 and overflows from the overflow port 16 to enter the gas cooling cavity 14; the alkaline circulating liquid flows downwards along the inner side of the inner wall 12 to form a constantly flowing and renewed protective wet film. This protection wet film can assist second spraying system 13 to cool down and wash the flue gas with burning the flue gas contact, reduces the second spraying system 13 and probably sprays the dead angle in the 1 lateral wall production of cooling tower, increases the time that alkaline circulation liquid and high temperature burned the flue gas contact to improve refrigerated effect and efficiency, just can obviously cool off the burning flue gas of high temperature in short time. The cooled incineration flue gas and the alkali circulating liquid are discharged from a low-temperature gas-liquid port 18 of the cooling tower 1, and the residence time of the incineration flue gas in the cooling tower 1 is 1 s.
The method mainly comprises the steps of cooling the high-temperature incineration flue gas and simultaneously carrying out primary deacidification; after the step, the incineration flue gas is cooled to be saturated wet flue gas with the temperature of 70-80 ℃ and the moisture content of 30-35%.
2. The incineration flue gas after temperature reduction treatment enters the wet scrubber tower 2 from the gas inlet 22 and moves from bottom to top, and the flow rate of the incineration flue gas entering the wet scrubber tower 2 is 2.5 m/s; and the alkaline circulation liquid which has cooled the incineration flue gas is refluxed from the cooling tower 1 into the tower internal circulation liquid tank 21 of the wet scrubber tower 2.
The incineration flue gas enters the hollow part of the cylinder 71 through the bottom of the cylinder 71 of the primary gas distributor 23 and is discharged from the air outlet of the cylinder 71 to continue moving upwards; the burning flue gas is distributed more uniformly after passing through the primary gas distributor 23, so that the contact between the alkaline circulating liquid and the burning flue gas is facilitated, and the alkaline washing effect of the burning flue gas is improved.
The first circulating pump 911 controls the temperature of the alkaline circulating liquid in the tower external circulating liquid tank 8 through the heat exchanger 912, and then the alkaline circulating liquid is conveyed to the first spraying system 25 to be sprayed, and the temperature of the alkaline circulating liquid is controlled at 45 ℃ during spraying.
The flue gas and the alkaline circulating liquid are in countercurrent contact at the position of the filler 24 for washing, cooling and dehumidifying, acidic substances in the flue gas and the alkaline circulating liquid are subjected to neutralization reaction, and meanwhile, the temperature of the flue gas is reduced to condense water vapor in the flue gas, so that the humidity in the flue gas is reduced, and a large amount of moisture is obtained; the washed smoke continues to move upwards; the washed alkaline circulation liquid and condensed water drop onto the tray 72 and flow back to the external circulation liquid tank 8 through the pipe by the water discharge port 73, and then are cooled by the heat exchanger 912, and a part of the cooled alkaline circulation liquid and condensed water is sent to the first sprinkling system 25 again, and the other part of the cooled alkaline circulation liquid and condensed water is sent to the internal circulation liquid tank 21. So as to replenish the water lost when the cooling tower 1 cools the incineration flue gas, realize the approximate balance of the system water, and do not need to replenish a large amount of water. Because the pipeline cooling effect is better than the cooling effect in the tower or the device, the alkaline circulating liquid is cooled once when returning to the circulating liquid tank 8 outside the tower through the pipeline, thereby reducing the burden of the heat exchanger 912.
Then the incineration flue gas is distributed again through the secondary gas distributor 26, the temperature of the flue gas is further reduced, water vapor in the flue gas is further condensed through the primary demisting layer 27 and the secondary demisting layer 28, so that liquid drops above 10um in the flue gas are removed, and finally the incineration flue gas is discharged from the gas outlet 29, and the retention time of the incineration flue gas in the wet washing tower 2 is 2 s. The liquid drops condensed on the first-stage demisting layer 27 and the second-stage demisting layer 28 fall onto the tower plate 72 of the second-stage gas distributor 26 through the showering of the reverse spraying system 74, and finally enter the sewage tank.
The method mainly comprises the steps of neutralizing acidic substances in incineration flue gas, condensing water vapor in the flue gas through cooling, and removing large-particle liquid drops in the incineration flue gas. The temperature of the flue gas discharged from the tower after the step is 55 ℃.
3. The incineration flue gas enters an acid mist condenser 3, the flow rate is 3m/s when the incineration flue gas enters, and the incineration flue gas passes through a two-stage main demister 31; the spraying system 312 of each stage of the main demister 31 sprays clean water relatively, the spraying flow rate is 3m/s, the humidity near the demisting layer 311 is improved, and the supersaturated environment of the region is caused. When the incineration flue gas passes through the demisting layer 311 of the main demister 31, tiny acid mist droplets in the incineration flue gas grow into 10-micron-level tiny acid mist droplets due to the nuclear condensation and aggregation process, and are intercepted and condensed by the demisting layer 311; meanwhile, with the increase of the relative humidity of the environment, the solid particles in the incineration flue gas absorb the moisture in the environment and become larger (the moisture absorption of the particles is increased), and the particles with the larger size are condensed on the defogging layer 311; the condensed liquid drops and solid particles are finally washed away by clear water, and the washed water is discharged into a sewage pool; the treated incineration flue gas is discharged out of the acid mist coagulator 3 after further coagulation of acid mist liquid drops and solid particles through the terminal demister 32, and the residence time of the flue gas in the acid mist coagulator 3 is 1.5 s.
The step is mainly to remove liquid drop particles and solid particles with the size smaller than 10um, further improve the cleanliness of the incineration flue gas and simultaneously realize the purpose of eliminating white smoke.
4. The purified low-temperature low-humidity flue gas is heated to above 135 ℃ (dew point) in a flue gas reheater 4 to further remove white smoke, and is finally discharged from an exhaust pipe 6, wherein the discharged flue gas contains SO2Less than 50mg/M3HCL content of less than 10mg/M3Containing less than 1mg/M of HF3。
In light of the foregoing, it is to be understood that various changes and modifications may be made by those skilled in the art without departing from the spirit and scope of the invention. The technical scope of the present invention is not limited to the content of the specification, and must be determined according to the scope of the claims.
Claims (8)
1. The utility model provides an incineration flue gas wet process deacidification device which characterized in that: the system comprises a cooling tower, a wet-type washing tower, an acid mist condenser and a flue gas reheater which are sequentially connected through pipelines; the wet washing tower is internally provided with an inner circulating liquid tank, a gas inlet, a primary gas distributor, a filler, a first spraying system, a secondary gas distributor, a primary demisting layer, a secondary demisting layer and a gas outlet from bottom to top; the first-stage gas distributor and the second-stage gas distributor respectively comprise a permeable cylinder body with a cover umbrella at the top and a tower plate, and the tower plate partitions the tower body and is provided with a water outlet; the water outlet of the primary gas distributor is communicated with a circulating liquid tank outside the tower through a pipeline; the tower external circulation liquid tank is also respectively communicated with the first spraying system and the tower internal circulation liquid tank through a circulation pipeline, and a heat exchanger is arranged on the circulation pipeline; the cooling tower is a double-layer falling film wet wall tower and comprises an outer wall, an inner wall, a second spraying system and a gas cooling cavity; the gas cooling cavity is arranged in the inner wall; an auxiliary cooling cavity is arranged in an interlayer between the outer wall and the inner wall, and at least one overflow port is arranged at the upper end of the inner wall; the second spraying system is communicated with a tower internal circulation liquid tank of the wet washing tower through a pipeline; the lower part of the auxiliary cooling cavity is communicated with a tower internal circulation liquid tank of the wet scrubber tower through a pipeline; the acid mist condenser is a horizontal tower and is provided with a plurality of main demisters; the main demister comprises a demisting layer and a third spraying system which is arranged on the left side and the right side of the demisting layer and points to the demisting layer.
2. The incineration flue gas wet deacidification device according to claim 1, characterized in that: the cooling tower comprises a high-temperature gas inlet communicated with the top of the gas cooling cavity and a low-temperature gas-liquid outlet communicated with the bottom of the gas cooling cavity; and an inverted cone-shaped maintenance emptying port is also arranged at the bottom of the auxiliary cooling cavity of the cooling tower.
3. The incineration flue gas wet deacidification device according to claim 1, characterized in that: a terminal demister is also arranged at the position, close to the outlet, of the acid mist condenser; the terminal demister comprises a demisting layer and a third spraying system which is arranged on one side of the terminal demister, is far away from the outlet of the acid mist condenser and is directed to the demisting layer.
4. The incineration flue gas wet deacidification device according to claim 1, characterized in that: the packing is composed of a plurality of regular packing units, and the packing units are provided with a plurality of fine columnar bulges extending towards the interior of the packing units.
5. The incineration flue gas wet deacidification device according to claim 4, wherein: the protrusion is a cone with a hemispherical end.
6. The incineration flue gas wet deacidification device according to claim 1, characterized in that: the hollow parts of the cylinders of the first-stage gas distributor and the second-stage gas distributor penetrate through the corresponding tower plates and are communicated with the inner space of the tower body.
7. The incineration flue gas wet deacidification device according to claim 1, characterized in that: the first-stage defogging layer is a PP folded plate, and the second-stage defogging layer is a PP wire mesh; and reverse spraying systems are arranged at the lower parts of the first-stage demisting layer and the second-stage demisting layer.
8. The incineration flue gas wet deacidification device according to claim 1, characterized in that: still including setting up the draught fan between acid mist condenser and flue gas reheater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201822233835.8U CN209828700U (en) | 2018-12-28 | 2018-12-28 | Wet deacidification device for incineration flue gas |
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| CN109794157A (en) * | 2018-12-28 | 2019-05-24 | 苏州艾特斯环保设备有限公司 | A kind of incineration flue gas wet process deacidifying device and deacidifying flue gas technique |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109794157A (en) * | 2018-12-28 | 2019-05-24 | 苏州艾特斯环保设备有限公司 | A kind of incineration flue gas wet process deacidifying device and deacidifying flue gas technique |
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