CN218033169U - Flue gas treatment system of waste liquid incinerator - Google Patents
Flue gas treatment system of waste liquid incinerator Download PDFInfo
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- CN218033169U CN218033169U CN202221177723.5U CN202221177723U CN218033169U CN 218033169 U CN218033169 U CN 218033169U CN 202221177723 U CN202221177723 U CN 202221177723U CN 218033169 U CN218033169 U CN 218033169U
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Abstract
The utility model discloses a flue gas treatment system of a waste liquid incinerator, which comprises a waste liquid incinerator, wherein a first heat exchanger, a dust and denitration integrated device, a second heat exchanger, a desulfurizing tower and a wet electric precipitator are sequentially arranged on a flue connected with a flue gas outlet end of the waste liquid incinerator, wherein the first heat exchanger is arranged close to the flue gas outlet end; the first heat exchanger is used for controlling the temperature of the flue gas entering the dedusting and denitration integrated device within a first set temperature range, and the first set temperature range is in an active temperature interval of the denitration catalyst; and the second heat exchanger is used for controlling the temperature of the flue gas entering the desulfurizing tower within a second set temperature range. The system has the advantages of short process flow, compact structure and small occupied area, and can remove main pollutants in the flue gas and meet the emission standard.
Description
Technical Field
The utility model relates to a chemical waste liquid burns burning furnace gas cleaning technical field, especially relates to a waste liquid burns burning furnace gas treatment system.
Background
Chemical products can generate waste liquid in the production process, along with the high-speed development of chemical industry, the discharge amount of the waste liquid is increased day by day, the components of the waste liquid are more and more complex, a large amount of harmful substances are contained in the waste liquid, and in order to avoid the pollution to the surrounding environment caused by direct discharge, the waste liquid needs to be subjected to harmless, quantitative reduction and recycling treatment before discharge.
At present, the waste liquid incineration method is a relatively effective waste liquid treatment technology, the waste liquid and combustion-supporting air are subjected to high-temperature combustion reaction and high-temperature pyrolysis in an incinerator, and dust and NO are inevitably generated in the waste liquid incineration process x 、SO x And the tail gas generated by the waste liquid incinerator needs to be treated to be discharged after reaching the standard.
As the tail gas generated by the waste liquid incinerator contains various pollutants, the tail gas treatment of the waste liquid incinerator is mostly separated, so that the treatment process flow is long, the number of equipment is large, the occupied area is large, and the operation and maintenance cost is high; other centralized treatment methods have the problem of incomplete removal of the major contaminants.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a waste liquid incinerator flue gas processing system, this system's process flow is short, compact structure, and area is little, and can the desorption main pollutants in the flue gas, satisfies emission standard.
In order to solve the technical problem, the utility model provides a flue gas treatment system of a waste liquid incinerator, which comprises a waste liquid incinerator, wherein a first heat exchanger, a dust and denitration integrated device, a second heat exchanger, a desulfurizing tower and a wet type electric precipitator are sequentially arranged on a flue connected with a flue gas outlet end of the waste liquid incinerator, wherein the first heat exchanger is arranged close to the flue gas outlet end;
the first heat exchanger is used for controlling the temperature of the flue gas entering the dedusting and denitration integrated device within a first set temperature range, and the first set temperature range is in an active temperature interval of the denitration catalyst;
and the second heat exchanger is used for controlling the temperature of the flue gas entering the desulfurizing tower within a second set temperature range.
This waste liquid incinerator flue gas processing system, flue gas outlet end at waste liquid incinerator is connected with first heat exchanger in order, dust removal denitration integrated device, the second heat exchanger, desulfurizing tower and wet-type electrostatic precipitator, so, flue gas that waste liquid incinerator produced is discharged from flue gas outlet end, carry out waste heat recovery through first heat exchanger earlier and utilize, reduce the flue gas temperature, in order to control the flue gas temperature between the active temperature region at the denitration catalyst, the flue gas that reduces the temperature gets into dust removal denitration integrated device, remove dust and desorption NO in dust removal denitration integrated device x The flue gas passing through the dedusting and denitration integrated device is cooled by the second heat exchanger, and the cooled flue gas enters the desulfurizing tower to remove SO 2 Then the mixture enters a wet-type electric precipitator for fine dust removal, and particularly can remove harmful substances such as dust, acid mist, water drops, aerosol and the like and can also assist in removing SO 3 Heavy metal and other pollutants, so that the flue gas discharged by the waste liquid incinerator can be effectively removed of dust and NO generated by the waste liquid incinerator after being treated by the system x 、SO x And the system has relatively short process flow and compact structure, thereby ensuring that the whole equipment occupies small area and is convenient to operate and maintain.
In the flue gas treatment system of the waste liquid incinerator, the dedusting and denitration integrated device comprises a pre-adsorption area, a dedusting area and a denitration area which are sequentially connected in series along the flow direction of flue gas; the pre-suctionThe adsorption zone is used for adsorbing part of moisture, dust and NO in the flue gas x And SO x (ii) a The dust removal zone is used for removing dust in the flue gas, and the denitration zone is used for removing NO in the flue gas x 。
According to the flue gas treatment system of the waste liquid incinerator, the dust removal area comprises an electric dust removal area and a bag type filter dust removal area which are sequentially connected in series along the flow direction of flue gas.
In the above waste liquid incinerator flue gas treatment system, the filter bag of the bag type dust filtering area is a metal filter bag; and a gas purifying chamber is arranged above the bag type dust filtering and filtering area, and the denitration area is arranged above the gas purifying chamber.
According to the flue gas treatment system of the waste liquid incinerator, the pre-adsorption area comprises a plurality of carrier beds which are arranged at intervals along the height direction, the carrier beds are of a net structure, and adsorption particles are laid on the carrier beds; the dust removal device comprises two adjacent load beds, wherein an interlayer partition plate is arranged between the two adjacent load beds, two side partition plates are arranged at two ends of each load bed along the flow direction of flue gas, and the flue gas can only flow to the dust removal area after passing through adsorption particles on the load beds due to the arrangement of the interlayer partition plates.
According to the flue gas treatment system of the waste liquid incinerator, the pre-adsorption area further comprises a replacement mechanism, and the replacement mechanism is used for replacing the adsorption particles on the carrier bed.
According to the waste liquid incinerator flue gas treatment system, the replacing mechanism comprises a storage bin, a collecting hopper and a driving part;
the carrying bed is of an annular structure, the driving part is used for driving the carrying bed to circularly move along the annular structure, and the moving direction of the carrying bed is vertical to the flowing direction of the flue gas;
the collecting hopper is used for collecting the adsorption particles falling from the loading bed;
the feed bin is used for holding the adsorbent particle of unadsorbed, all be equipped with the feed pipe between feed bin and every year bed, the feed pipe be used for with adsorbent particle in the feed bin carry extremely carry the bed.
According to the flue gas treatment system of the waste liquid incinerator, the moving directions of the carrying beds are the same, the feeding pipe is arranged at the head end of the carrying bed, the tail end of the carrying bed is provided with the blanking baffle, and the blanking baffle is used for guiding the adsorption particles on the carrying bed to the collecting hopper.
According to the flue gas treatment system of the waste liquid incinerator, the replacing mechanism further comprises a regeneration bin; the collecting hopper is connected with the regeneration bin to convey the collected adsorbed adsorption particles to the regeneration bin; the regeneration bin is used for carrying out regeneration treatment on the adsorbed adsorption particles; the regeneration bin is also connected with the bin so as to convey the regenerated adsorption particles to the bin.
According to the flue gas treatment system of the waste liquid incinerator, the tail end side of the carrier bed is provided with the nozzle, and the nozzle is used for removing adsorption particles and/or dust adhered to the carrier bed.
According to the flue gas treatment system of the waste liquid incinerator, each carrying bed is tensioned on two driven wheels, the driving part comprises a driving source and a transmission mechanism, the transmission mechanism comprises a driving wheel and a transmission part, the driving wheel is in transmission connection with all the driven wheels on the same side through the transmission part, and the driving source is used for driving the driving wheel to rotate so as to drive the driven wheels to rotate.
According to the flue gas treatment system of the waste liquid incinerator, the diameter of the adsorption particles is 2-4 times of the aperture of the meshes of the carrier bed.
According to the flue gas treatment system of the waste liquid incinerator, the top of the dust removal and denitration integrated device is provided with the air inlet, the dust removal and denitration integrated device further comprises an inlet horn and uniformly distributed flow guide pieces, and the inlet horn is located at the upstream of the pre-adsorption area and is communicated with the air inlet; the utility model discloses a bed of bending machine, including the equipartition water conservancy diversion spare, including the first board and the second board of bending, the opening of the board of bending is down, the first board is kept away from carry the bed setting, just be the second setting angle between first board and the horizontal direction.
According to the flue gas treatment system of the waste liquid incinerator, the first set angle is 70-90 degrees, and the second set angle is 50-70 degrees.
According to the flue gas treatment system of the waste liquid incinerator, the catalyst in the denitration area is a honeycomb type catalyst, and the catalyst layer in the denitration area is provided with the sound wave soot blower.
According to the flue gas treatment system of the waste liquid incinerator, an ammonia spraying device is further arranged between the first heat exchanger and the dust removal and denitration integrated device and comprises an ammonia spraying grid and an ammonia source, the ammonia spraying grid is arranged in a flue which is connected with the first heat exchanger and the dust removal and denitration integrated device, and the ammonia source is connected with the ammonia spraying grid.
The flue gas treatment system of the waste liquid incinerator, the ammonia spraying device further comprises an air source and a mixer, the mixer is arranged between the ammonia source and the flue, the air source is connected with the mixer, and the mixer is used for mixing ammonia gas from the ammonia source and air from the air source.
According to the flue gas treatment system of the waste liquid incinerator, the waste liquid incinerator is connected with a fresh air source, an air preheater is connected between the fresh air source and the waste liquid incinerator, and the air preheater is further arranged in a flue connected between the second heat exchanger and the dust removal and denitration integrated device.
As above waste liquid incinerator flue gas processing system, wet-type electrostatic precipitator's exit linkage has the chimney, the desulfurizing tower wet-type electrostatic precipitator with the chimney is established as an organic whole structure.
Drawings
FIG. 1 is a schematic structural view of an embodiment of a flue gas treatment system of a waste liquid incinerator;
FIG. 2 is a schematic structural diagram of the integrated dedusting and denitration apparatus in FIG. 1;
FIG. 3 isbase:Sub>A schematic view of the pre-adsorption zone of FIG. 2 in the direction A-A;
FIG. 4 is a schematic view of the orientation of the flue gas in the pre-adsorption zone of FIG. 2.
Description of the reference numerals:
a waste liquid incinerator 10, a first heat exchanger 20;
the device comprises a dedusting and denitration integrated device 30, an air inlet 31, an inlet horn 32, a uniform distribution flow guide member 33, a bending plate 331, a first plate 3311, a second plate 3312, a pre-adsorption area 34, a loading bed 341, an interlayer partition 342, a side partition 343, a storage bin 344, a feeding pipe 3441, a collecting hopper 345, a blanking baffle 346, a nozzle 347, a speed reducing motor 3481, a driving wheel 3482, a driven wheel 3483, a transmission chain 3484, a regeneration bin 349, a dedusting area 35, an electric dedusting area 351, a bag type filtering and dedusting area 352, an air purifying chamber 36, a denitration area 37, an outlet flue 38 and an ash bucket 39;
a second heat exchanger 40, an induced draft fan 45, a desulfurizing tower 50, a wet electric dust collector 60 and a chimney 70;
an ammonia injection grid 81, a mixer 82, an evaporator 83 and a fan 84;
a blower 91, and an air preheater 92.
Detailed Description
In order to make the technical field better understand the solution of the present invention, the following detailed description of the present invention is provided with reference to the accompanying drawings and the detailed description.
Referring to fig. 1, fig. 1 is a schematic structural diagram of an embodiment of a flue gas treatment system of a waste liquid incinerator according to the present invention.
In this embodiment, the flue gas treatment system of the waste liquid incinerator comprises a waste liquid incinerator 10, a first heat exchanger 20, a dust and denitration integrated device 30, a second heat exchanger 40, a desulfurizing tower 50 and a wet electric dust remover 60.
Wherein, the top of the waste liquid incinerator 10 is provided with a flue gas outlet, and high-temperature flue gas generated after the waste liquid and the auxiliary fuel in the waste liquid incinerator 10 are combusted can be discharged from the flue gas outlet.
The aforementioned first heat exchanger 20, the dust and denitration integrated device 30, the second heat exchanger 40, the desulfurizing tower 50 and the wet electric dust remover 60 are sequentially arranged on the flue connected with the flue gas outlet end of the waste liquid incinerator 10, wherein the first heat exchanger 20 is arranged close to the flue gas outlet end of the waste liquid incinerator 10, that is, the flue gas discharged from the waste liquid incinerator 10 sequentially flows through the first heat exchanger 20, the dust and denitration integrated device 30, the second heat exchanger 40, the desulfurizing tower 50 and the wet electric dust remover 60.
It should be noted that, the above-mentioned relative positional relationship between the first heat exchanger 20, the dust and denitration integrated device 30, the second heat exchanger 40, the desulfurizing tower 50 and the wet electric dust remover 60, which is only indicated in the above-mentioned order, does not exclude that other devices are further arranged between the two adjacent devices on the basis of the basic scheme.
Wherein, first heat exchanger 20 is used for carrying out waste heat recovery to waste liquid incinerator 10 exhaust high temperature flue gas, reduces the temperature of flue gas simultaneously, with flue gas temperature control in first settlement temperature range, this first settlement temperature range is in the active temperature interval of denitration catalyst to can carry out denitration treatment betterly after the flue gas gets into dust removal denitration integrated device 30.
Specifically, the first set temperature may be 300 to 400 ℃.
The second heat exchanger 40 is used for controlling the temperature of the flue gas entering the desulfurizing tower 50 within a second set temperature range, so as to improve the desulfurization treatment effect of the flue gas in the desulfurizing tower 50.
Specifically, the second set temperature may be below 60 ℃.
This waste liquid incinerator flue gas processing system during operation, the flue gas that waste liquid incinerator produced carries out waste heat recovery through first heat exchanger 20 earlier after the flue gas exit end discharges, reduces the flue gas temperature to with flue gas temperature control at the active temperature interval of denitration catalyst, the flue gas entering dust removal denitration integrated device 30 of reduce temperature removes dust and desorption NO in dust removal denitration integrated device 30 x The flue gas passing through the dedusting and denitration integrated device 30 is cooled by the second heat exchanger 40, and the cooled flue gas enters the desulfurizing tower 50 to remove SO 2 Then the wet-type electric dust collector 60 is used for fine dust removal, which can specifically remove harmful substances such as dust, acid mist, water drops, aerosol and the like and can also assist in removing SO 3 Heavy metals and the like, so that after the system is used for treatment, waste liquid incineration can be effectively removedDust and NO generated from the furnace 10 x 、 SO x And the system has relatively short process flow and compact structure, thereby ensuring small occupied area of the whole equipment and convenient operation and maintenance.
Referring to fig. 2, fig. 2 is a schematic structural diagram of the integrated dust removal and denitration apparatus shown in fig. 1.
In this embodiment, the integrated dust and denitration device 30 includes a pre-adsorption region 34, a dust removal region 35 and a denitration region 37 connected in series in sequence along the flow direction of the flue gas, wherein the pre-adsorption region 34 performs a pre-adsorption treatment on the flue gas to adsorb a part of moisture, dust and NO in the flue gas x And SO x (ii) a The dust removal zone 35 is used for removing dust in the flue gas, and the denitration zone 37 is used for removing NO in the flue gas x 。
This dust removal denitration integrated device 30 will adsorb district 34, dust removal district 35 and denitration district 37 in advance and be integrated as an organic whole, is favorable to improving compact structure degree, reduces area, adsorbs the processing in advance to the flue gas in the district 34 in advance, can improve the operating mode condition of back level flue gas, is favorable to promoting back level dust removal, denitration, desulfurization and defogging efficiency, ensures the effect of handling the flue gas. In a specific scheme, the dust removing region 35 includes an electric dust removing region 351 and a bag-type dust filtering region 352 which are sequentially connected in series along the flow direction of the flue gas, that is, the flue gas passes through the pre-adsorption region 34, enters the dust removing region 35, passes through the electric dust removing region 351, and passes through the bag-type dust filtering region 352; the electric dust removal area 351 and the bag type dust filtering area 352 are both high-temperature dust removal areas, the working temperature of the electric dust removal area 351 and the bag type dust filtering area 352 is generally 300-400 ℃, obviously, the component materials of the electric dust removal area 351 and the bag type dust filtering area 352 are high-temperature resistant materials, for example, a filter bag of the bag type dust filtering area 352 can be a high-temperature resistant metal filter bag, the metal filter bag can be specifically formed by sintering micron-sized metal fibers after gradient layering of a fine fiber layer and a coarse fiber layer, so that a filter felt with high filtering precision, low resistance and good dust cleaning performance is formed, and then the filter felt is manufactured into a cylindrical structure with a certain length and an opening at the upper end and a closed lower end; the metal filter bag is high temperature resistant, long in service life, recyclable and beneficial to reducing investment cost and maintenance cost. In practical application, different metal fibers can be selected according to specific requirements, and the mode of manufacturing the metal filter bag is not limited to the above.
The dust removal and denitration integrated device 30 is provided with the air purifying chamber 36 above the bag-type dust filtering area 352, so that flue gas dedusted by the pre-adsorption area 34, the electric dust removal area 351 and the bag-type dust filtering area 352 can be buffered in the air purifying chamber 36, the denitration area 37 is specifically arranged above the air purifying chamber 36, and the flue gas subjected to dust removal is subjected to denitration treatment through the denitration area 37.
After the flue gas is pre-adsorbed and dedusted, the dust concentration of the flue gas is greatly reduced, the adverse effect of fly ash is basically eliminated, the denitration catalyst in the denitration zone 37 can be ensured to have good catalytic activity, the denitration efficiency of the catalyst can be effectively improved, the service life of the catalyst is prolonged, the consumption of the catalyst is reduced, the ammonia escape is reduced, and therefore the investment and the operation cost are reduced.
Specifically, the denitration region 37 specifically adopts an SCR denitration reaction, and the catalyst also adopts an SCR denitration catalyst, and the SCR denitration reaction is a mature technology in the prior art, and is not described in detail here.
In specific application, the catalyst in the denitration region 37 can be a honeycomb catalyst, and the pitch of the honeycomb catalyst can be relatively small, for example, 4.3mm or 3.7mm, so that the specific surface area of the catalyst can be increased, and the using amount of the catalyst can be reduced; further, an acoustic soot blower may be disposed on the catalyst layer of the denitration region 37 to prevent dust from depositing on the catalyst layer and affecting the activity of the catalyst.
The integrated dedusting and denitrating device 30 is further provided with an outlet flue 38 above the denitrating area 37, so that the flue gas treated by the integrated dedusting and denitrating device 30 can be discharged.
In this embodiment, the ash hoppers 39 are disposed below the pre-adsorption region 34 and the dust removal region 35, a part of coarse dust particles in the flue gas entering the dust removal and denitration integrated device 30 can be settled in the ash hoppers 39 under the action of gravity and inertia, and the dust can also be settled in the ash hoppers 39 after the ash removal is performed on the relevant equipment of the dust removal region 35.
The electric dust removing region 351 and the bag-type dust filtering region 352 in the integrated dust and nitrogen removing and removing device 30 can both adopt the existing mature electric dust removing structure and filter bag structure, which are not described in detail herein, and the structure of the pre-adsorption region 34 is designed in the focus here, which is described below with reference to fig. 3 and 4, wherein fig. 3 isbase:Sub>A schematic structural diagram of the pre-adsorption region in the direction ofbase:Sub>A-base:Sub>A in fig. 2, and fig. 4 isbase:Sub>A schematic structural diagram of the flue gas in the pre-adsorption region in fig. 2.
In this embodiment, the pre-adsorption region 34 includes a plurality of loading beds 341 arranged at intervals in the height direction, the loading beds 341 are in a mesh structure, adsorption particles (not shown in the figure) are laid on the loading beds 341, an interlayer partition 342 is disposed between two adjacent loading beds 341, each loading bed 341 has a side partition 343 at both ends in the flow direction of the flue gas, and the interlayer partition 342 and the side partition 343 are disposed so that the flue gas can flow to the dust-removing region 35 only after passing through the adsorption particles of the loading bed 341.
As can be understood by referring to fig. 4, in the view shown in fig. 4, the flue gas flows from the left side to the right side, the side partition plates 343 at both ends of each carrier bed 341 are located at the upper and lower sides of the carrier bed 341 and do not extend to the adjacent carrier bed 341, so that the flue gas can flow to the carrier bed 341, as indicated by the solid black arrows in fig. 4, when the flue gas flows into the space between one interlayer partition plate 342 and one carrier bed 341, the flue gas can only flow to the dust removing area 35 from the space below the carrier bed 341 after passing through the adsorbed particles on the carrier bed 341 due to the blocking of the side partition plates 343 at the right end of the carrier bed 341 and the blocking of the interlayer partition plates 342, and thus the flue gas can be adsorbed by the adsorbed particles on the carrier bed 341 when passing through the carrier bed 341, and the flow path of the flue gas in the area where the carrier bed 341 can be simply understood as a Z-shape.
Still referring to fig. 4, one interlayer partition 342 and two side partitions 343 may be provided as an integrated structure, the left side partition 343 being connected to the upper carrying bed 341, the interlayer partition 342 being provided between the upper carrying bed 341 and the lower carrying bed 341, and the right side partition 343 being connected to the lower carrying bed 341.
Of course, in addition to the above-mentioned arrangement of the partition plates, the partition plates may be arranged in other manners as long as it can be ensured that the flue gas flowing through the upper part of the load bed 341 must pass through the adsorption particles before flowing to the dust-removing area 35.
In this embodiment, the pre-adsorption region 34 is further provided with a replacement mechanism for replacing the adsorption particles on the carrier bed 341, so as to ensure the adsorption performance of the adsorption particles on the carrier bed 341 and ensure the treatment effect on the flue gas.
Specifically, the replacement mechanism includes a bin 344, a collection hopper 345, and a drive portion.
In order to facilitate the replacement of the adsorbed particles, the carrier bed 341 is designed to be of an annular structure, the driving portion is used to drive the carrier bed 341 to circularly move along the annular structure, in order to facilitate the arrangement of the relevant structures, the moving direction of the carrier bed 341 is perpendicular to the flowing direction of the flue gas, and similarly, in order to simplify the structure, in this example, all the carrier beds 341 of the pre-adsorption region 34 move towards the same direction, and in the view angle shown in fig. 3, the carrier bed 341 rotates clockwise.
The collection hopper 345 is located below all the beds 341 and collects the adsorption particles falling from the beds 341.
Specifically, the feeding pipe 3411 is provided at a head end of the loading bed 341, where the head end is based on a moving direction of the loading bed 341, and an orientation shown in fig. 3 is taken as a reference, that is, a left end of the loading bed 341 is a head end, and a right end is a tail end, and a part of the loading bed 341 carrying the adsorption particles moves from the left end to the right end, and since the loading bed 341 is annular, when the loading part moves to the right end and turns, the adsorption particles thereon fall off, and the collection hopper 345 falling below is collected. The feed pipe 3411 is provided at the head end of the bed 341 to ensure that the adsorbent particles having the adsorption capacity are maximally contacted with the flue gas during the rotation of the bed 341.
Specifically, in order to save space and provide a large number of the loading beds 341, the loading beds 341 are in a flat ring structure, and the height of the loading beds 341 is reduced as much as possible, so that the loading beds 341 can be arranged as much as possible in a limited height space.
In practical arrangement, the number of layers and the size of the carrier bed 341 enable the filtering wind speed of the carrier bed 341 to be not higher than 3m/min, so as to ensure the contact time of the flue gas and the adsorption particles.
As shown in fig. 3, a blanking baffle 346 is provided at the end of each carrier bed 341, and the blanking baffle 346 is used for guiding the adsorption particles on the carrier bed 341 to the collection hopper 345 so as to prevent the adsorption particles from falling onto the carrier bed 341 on the next layer during the falling process. It is understood that the lowermost carry bed 341 may not be disposed with the blanking baffles 346.
Specifically, a nozzle 347 may be provided at the rear end side of each of the beds 341, and the nozzle 347 may remove the adsorbed particles and/or dust adhering to the bed 341, so that the bed 341 is kept clean, and the filtration resistance can be kept stable after the adsorption particles are newly laid. The air source of the nozzle 347 may specifically employ compressed air.
In this embodiment, the driving portion includes a driving source and a transmission mechanism, each carrying bed 341 is tensioned on two driven wheels 3483, the transmission mechanism includes a driving wheel 3482 and a transmission portion, the driving wheel 3482 is in transmission connection with all driven wheels 3483 on the same side through the transmission portion, the driving source is used for driving the driving wheel 3482 to rotate so as to drive all driven wheels 3483 to rotate, thereby driving each carrying bed 341 to rotate circularly, wherein the transmission portion may specifically select a form of a transmission chain 3484 or a transmission belt, the driving source may select a reduction motor 3481, of course, a common motor may also be selected, and a reduction mechanism is further provided to facilitate adjustment of the moving speed of the carrying bed 341. In the illustration, the driving wheel 3482 is drivingly connected to all the driven wheels 3483 on the right side for the convenience of structural arrangement.
In practical application, the adsorption particles can be activated carbon and other particles, and the adsorption particles with relatively uniform particle size can be used, and the particle size of the adsorption particles can be 2-4 times of the aperture of the meshes of the carrier bed 341, so that the adsorption effect on the flue gas can be improved.
In this embodiment, the replacing mechanism further includes a regeneration bin 349, the collecting hopper 345 is connected to the regeneration bin 349 to transport the collected adsorbed adsorption particles to the regeneration bin 349, and the regeneration bin 349 is used to perform a regeneration treatment on the adsorbed adsorption particles, where a device for performing the regeneration treatment on the adsorption particles is also an existing mature technology, and details thereof are not described here. The regeneration bin 349 is also connected to the bin 344 so as to transport the regenerated adsorbent particles to the bin 344 and re-lay the adsorbent particles on the carrier bed 341 for recycling, which is favorable for cost saving.
After the flue gas enters the dust removal and denitration integrated device 30, in order to enable the flue gas to uniformly pass through the loading beds 341 of each layer as much as possible so as to ensure the pre-adsorption effect on all the flue gas, the dust removal and denitration integrated device 30 is further provided with an inlet horn 32 and uniformly distributed flow guide pieces 33 at the upstream of the pre-adsorption area 34.
Referring to fig. 2 specifically, the dust removal and denitration integrated device 30 is provided with an air inlet 31 at the top thereof, that is, flue gas cooled by the first heat exchanger 20 enters the dust removal and denitration integrated device 30 from the air inlet 31 at the top, an inlet of an inlet horn 32 is connected with the air inlet 31, an outlet is connected with the pre-adsorption region 34, and the uniform distribution guide member 33 is arranged at the upstream of the loading bed 341 so as to uniformly distribute the flue gas entering the multi-layer loading bed 341.
The evenly distributed flow guide pieces 33 comprise a plurality of bending plates 331 which are arranged at intervals along the height direction, each bending plate 331 comprises a first plate 3311 and a second plate 3312 which are bent to form a first set angle, the opening of each bending plate 331 faces downwards, the first plate 3311 is far away from the direction of the carrying bed 341, the first plate 3311 and the horizontal direction form a second set angle, specifically, the first set angle is 70-90 degrees, and the second set angle is 50-70 degrees. As shown in fig. 2, the bent plates 331 are arranged to separate the outlet of the inlet horn 32 near the pre-adsorption area into a plurality of flow channels, and the flue gas enters through the air inlet 31, is diffused and buffered in the inlet horn 32, is rectified by the bent plates 331, and then flows to the pre-adsorption area 34; wherein, when diffusion buffering in import loudspeaker 32, during the part coarse grain dust in the flue gas can fall into the ash bucket of below under gravity and inertia effect, when evenly distributed water conservancy diversion piece 33, part dust also can be collided with board 331 of bending and is intercepted, later falls into in ash bucket 39, like this, has also reduced the dust concentration who gets into adsorption zone 34 in advance, can prevent effectively that the coarse grain dust from to carrying the washing away of bed 341, ensures carrying the effective absorption of the last adsorbed particle of bed 341.
The number and the spacing distance of the plurality of bending plates 331 arranged in the height direction can be set according to actual requirements, and are not limited herein.
After the dust removal and denitration integrated device 30 is arranged, the pollutant-containing flue gas generated by the waste liquid incinerator 10 passes through the air inlet 31, the inlet horn 32 and the uniformly distributed guide plates 33 and then enters the pre-adsorption area 34, and most of moisture, dust and NO in the flue gas can be pre-adsorbed by the adsorption particles of the load bed 341 x And SO x And the residual dust enters a bag type dust filtering and filtering area 352 along with the flue gas flow and is filtered and collected by a filter bag, the flue gas without dust flows into a gas purifying chamber 36 and then upwards enters a denitration area 37, and NO of the flue gas is removed in the denitration area 37 x 。
NO removal from flue gas in denitration zone 37 x In this embodiment, the flue gas treatment system of the waste liquid incinerator is further provided with an ammonia spraying device, referring to fig. 1, the ammonia spraying device comprises an ammonia spraying grid 81 and an ammonia gas source, the ammonia spraying grid 81 is arranged in a flue connecting the first heat exchanger 20 and the dust removal and denitration integrated device 30, and the ammonia gas source is connected with the ammonia spraying grid 81, so that ammonia gas provided by the ammonia gas source can be sprayed into the flue through the ammonia spraying grid 81 and enter the dust removal and denitration integrated device 30 along with flue gas, so that the ammonia gas and the flue gas are fully and uniformly mixed before entering the denitration area 37, and can be fully and uniformly mixed with NO in the denitration area 37 x Catalytic reaction takes place to better complete NO x And (4) removing. Specifically, the ammonia injection device further comprises an air source and a mixer 82, the mixer is arranged between the ammonia source and the flue, the air source is connected with the mixer 82, namely, the air of the air source and the ammonia gas of the ammonia source enter the mixer 82 to be mixed, and then the diluted ammonia gas is injected into the flue through the ammonia injection grid 81.
The ammonia source can adopt the form of ammonia water evaporation, the ammonia water is comparatively easy to store and obtain, and the ammonia water is sent into the mixer 82 after obtaining the ammonia gas through the evaporator 83.
Dust and NO are removed by the dust removal and denitration integrated device 30 x The flue gas is discharged from the outlet flue 38, enters the desulfurizing tower 50 after being subjected to heat exchange and temperature reduction by the second heat exchanger 40, reacts with the sprayed ammonia water in the desulfurizing tower 50,to remove SO 2 (ii) a As described above, in this example, ammonia desulfurization is used, and the desulfurizing agent is ammonia water, and unreacted NH is passed through the denitration zone 37 3 And can be fully utilized when passing through the desulfurizing tower 50, thus effectively reducing the escape rate of ammonia. SO absorption by desulfurizing agent 2 And the formed substances such as ammonium bisulfate and the like are discharged from the desulfurizing tower 50 and then used in the form of nitrogen fertilizer, so that the air pollution caused by harmful substances can be prevented, the cyclic and effective utilization of the substances can be realized, and the resources are saved.
Specifically, an induced draft fan 45 may be disposed on the flue between the second heat exchanger 40 and the desulfurization tower 50, so as to feed the flue gas into the desulfurization tower 50.
After the flue gas is desulfurized by the ammonia method, harmful substances such as ammonia salt-containing aerosol and the like can be generated to form a blue smoke phenomenon, so a wet electric dust remover 60 is arranged behind the desulfurizing tower 50 to perform fine dust removal on the flue gas. The wet electric precipitator 60 is a dust removal device for treating dust containing trace amount and fine particles, and can efficiently remove harmful substances such as dust (containing PM 2.5), acid mist, water drop, aerosol (containing ammonia salt) and the like in moisture-containing gas, and cooperatively remove SO in the flue gas 3 And heavy metals and the like, and the ultralow emission is realized.
In this embodiment, the outlet of the wet electric dust collector 60 is connected to a chimney 70, and the clean flue gas after being subjected to fine dust removal by the wet electric dust collector 60 can be discharged through the chimney 70.
As shown in fig. 1, in practical implementation, the desulfurization tower 50, the wet electric dust collector 60 and the chimney 70 may be integrated to further improve the compactness of the system structure.
Through tests, the flue gas purified by the flue gas treatment system of the waste liquid incinerator can achieve ultralow emission, and the dust in the purified flue gas is less than 5mg/Nm 3 ，NO x ＜50mg/Nm 3 ， SO 2 ＜35mg/Nm 3 。
In addition, when the waste liquid in the waste liquid incinerator 10 burns, fresh air is needed, the waste liquid incinerator 10 is further connected with an air inlet pipeline, so that air is sent into the waste liquid incinerator 10 through the blower 91, in the embodiment, an air preheater 92 can be arranged on the air inlet pipeline, so that the air is preheated, specifically, the air preheater 92 can be arranged in a flue connected between the second heat exchanger 40 and the dust removal and denitration integrated device 30, the fresh air is heated by utilizing the waste heat of the discharged flue gas, and the waste heat recycling is realized. Of course, it is understood that it is also possible to arrange the air preheater 92 in the flue between the second heat exchanger 40 and the integrated dust and nox removal device 30.
It is right above the utility model provides a waste liquid incinerator flue gas processing system has carried out detailed introduction. The principles and embodiments of the present invention have been explained herein using specific examples, and the above description of the embodiments is only used to help understand the method and its core idea of the present invention. It should be noted that, for those skilled in the art, without departing from the principle of the present invention, the present invention can be further modified and modified, and such modifications and modifications also fall within the protection scope of the appended claims.
Claims (19)
1. The flue gas treatment system of the waste liquid incinerator is characterized by comprising the waste liquid incinerator, wherein a first heat exchanger, a dedusting and denitration integrated device, a second heat exchanger, a desulfurizing tower and a wet electric dust remover are sequentially arranged on a flue connected with a flue gas outlet end of the waste liquid incinerator, wherein the first heat exchanger is arranged close to the flue gas outlet end;
the first heat exchanger is used for controlling the temperature of the flue gas entering the dedusting and denitration integrated device within a first set temperature range, and the first set temperature range is in an active temperature interval of the denitration catalyst;
and the second heat exchanger is used for controlling the temperature of the flue gas entering the desulfurizing tower within a second set temperature range.
2. The flue gas treatment system of a waste liquid incinerator according to claim 1, wherein said dust removal and denitration integrated device comprises a pre-adsorption zone, a dust removal zone and denitration zone connected in series in sequence along the flow direction of flue gasA zone; the pre-adsorption area is used for adsorbing part of moisture, dust and NO in the flue gas x And SO x (ii) a The dust removal zone is used for removing dust in the flue gas, and the denitration zone is used for removing NO in the flue gas x 。
3. The liquid waste incinerator flue gas treatment system of claim 2, wherein the dust removal zone comprises an electric dust removal zone and a bag-type filtered dust zone connected in series in sequence in the flue gas flow direction.
4. The waste liquid incinerator flue gas treatment system of claim 3 wherein said bag filter in said bag type dust filtration zone is a metal filter bag; and a gas purifying chamber is arranged above the bag type dust filtering and filtering area, and the denitration area is arranged above the gas purifying chamber.
5. The flue gas treatment system of a waste liquid incinerator according to claim 2, wherein the pre-adsorption region comprises a plurality of carrier beds arranged at intervals in the height direction, the carrier beds are of a net structure, and adsorption particles are laid on the carrier beds; the dust removal device comprises two adjacent load beds, wherein an interlayer partition plate is arranged between the two adjacent load beds, two side partition plates are arranged at two ends of each load bed along the flow direction of flue gas, and the flue gas can only flow to the dust removal area after passing through adsorption particles on the load beds due to the arrangement of the interlayer partition plates.
6. The liquid waste incinerator flue gas treatment system of claim 5 wherein said pre-adsorption zone further includes a replacement mechanism for replacing adsorbent particles on said carrier bed.
7. The liquid waste incinerator flue gas treatment system of claim 6, wherein the replacement mechanism includes a bin, a collection hopper, and a drive section;
the carrying bed is of an annular structure, the driving part is used for driving the carrying bed to circularly move along the annular structure, and the moving direction of the carrying bed is vertical to the flowing direction of the flue gas;
the collecting hopper is used for collecting the adsorption particles falling from the loading bed;
the feed bin is used for holding the adsorbent particle of unadsorbed, all be equipped with the feed pipe between feed bin and every year bed, the feed pipe be used for with adsorbent particle in the feed bin carry extremely carry the bed.
8. The flue gas treatment system of a waste liquid incinerator according to claim 7, wherein said plurality of said carrier beds are moved in the same direction, said feed pipe is disposed at the head end of said carrier bed, and said carrier bed is provided at the tail end thereof with a blanking baffle for guiding the adsorbent particles on said carrier bed to said collection hopper.
9. The liquid waste incinerator flue gas treatment system of claim 7 wherein said replacement mechanism further includes a regeneration bin; the collecting hopper is connected with the regeneration bin to convey the collected adsorbed adsorption particles to the regeneration bin; the regeneration bin is used for carrying out regeneration treatment on the adsorbed adsorption particles; the regeneration bin is also connected with the bin so as to convey the regenerated adsorption particles to the bin.
10. The liquid waste incinerator flue gas treatment system of claim 7 wherein said carrier bed is provided at its trailing end side with nozzles for removing adsorbed particles and/or dust adhering to said carrier bed.
11. The flue gas treatment system of a waste liquid incinerator, as claimed in claim 7, wherein each said carrying bed is tensioned on two driven wheels, said driving section includes a driving source and a transmission mechanism, said transmission mechanism includes a driving wheel and a transmission section, said driving wheel is in transmission connection with all driven wheels on the same side through said transmission section, said driving source is used to drive said driving wheel to rotate so as to drive said driven wheels to rotate.
12. The flue gas treatment system of a waste liquid incinerator according to claim 5, wherein the diameter of said adsorbent particles is 2 to 4 times the mesh aperture of said bed.
13. The waste liquid incinerator flue gas treatment system of any one of claims 5 to 12, wherein an air inlet is formed in the top of the dust removal and denitration integrated device, the dust removal and denitration integrated device further comprises an inlet horn and uniformly distributed guide pieces, and the inlet horn is located on the upstream of the pre-adsorption area and is communicated with the air inlet; the utility model discloses a bed of bending machine, including the equipartition water conservancy diversion spare, including the first board and the second board of bending, the opening of the board of bending is down, the first board is kept away from carry the bed setting, just be the second setting angle between first board and the horizontal direction.
14. The flue gas treatment system of a waste liquid incinerator according to claim 13 wherein said first set angle is 70 to 90 degrees and said second set angle is 50 to 70 degrees.
15. The liquid waste incinerator flue gas treatment system of any one of claims 2 to 12, wherein said denitration zone catalyst is a honeycomb type catalyst, and said denitration zone catalyst layer is provided with an acoustic wave soot blower.
16. The flue gas treatment system of a waste liquid incinerator according to any one of claims 1 to 12, wherein an ammonia injection device is further provided between the first heat exchanger and the integrated dust and denitration device, the ammonia injection device includes an ammonia injection grid and an ammonia source, the ammonia injection grid is provided in a flue connecting the first heat exchanger and the integrated dust and denitration device, and the ammonia source is connected to the ammonia injection grid.
17. The liquid waste incinerator flue gas treatment system of claim 16 wherein said ammonia injection means further comprises an air source and a mixer, said mixer being disposed between said ammonia source and said flue, said air source being connected to said mixer, said mixer being adapted to mix ammonia gas from said ammonia source with air from said air source.
18. The flue gas treatment system of a waste liquid incinerator according to any one of claims 1 to 12 wherein said waste liquid incinerator is connected to a fresh air source, an air preheater is connected between said fresh air source and said waste liquid incinerator, said air preheater is further provided in a flue connected between said second heat exchanger and said dust removal and denitration integrated apparatus.
19. The flue gas treatment system of a waste liquid incinerator according to any one of claims 1 to 12, wherein the outlet of the wet electric precipitator is connected to a chimney, and the desulfurizing tower, the wet electric precipitator and the chimney are integrated.
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| CN202221177723.5U CN218033169U (en) | 2022-05-16 | 2022-05-16 | Flue gas treatment system of waste liquid incinerator |
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| CN202221177723.5U CN218033169U (en) | 2022-05-16 | 2022-05-16 | Flue gas treatment system of waste liquid incinerator |
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