CN110917863A - Sintering flue gas is treatment system in coordination - Google Patents
Sintering flue gas is treatment system in coordination Download PDFInfo
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- CN110917863A CN110917863A CN201911376140.8A CN201911376140A CN110917863A CN 110917863 A CN110917863 A CN 110917863A CN 201911376140 A CN201911376140 A CN 201911376140A CN 110917863 A CN110917863 A CN 110917863A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/005—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by heat treatment
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
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- B01D53/265—Drying gases or vapours by refrigeration (condensation)
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D—SEPARATION
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- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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Abstract
A sintering flue gas cooperative treatment system belongs to the technical field of industrial waste gas treatment. The device comprises an electric dust collector, a first fan, a desulfurization device, a flue gas condensation dehydrator, a flue gas preheater, a denitration device, a bag-type dust remover, a pipeline and a second fan which is connected with a chimney, wherein the electric dust collector, the first fan, the desulfurization device, the flue gas condensation dehydrator, the flue gas preheater, the denitration device, the bag-type dust remover, the second fan and the chimney are sequentially arranged along a sintering flue gas treatment process. Compared with the prior art, the invention has the advantages of small floor area, low investment cost, low corrosivity to equipment and high desulfurization, denitrification and dust removal efficiency, and ensures that sulfur dioxide, particulate matters and nitric oxide in sintering flue gas meet the requirements of ultralow emission standards. The invention efficiently recovers and utilizes the waste heat of the sintering flue gas, reduces the energy consumption in the treatment process, reduces the operation cost, can realize the long-term stable low-energy consumption operation, and has stronger practicability on the sintering flue gas.
Description
Technical Field
The invention belongs to the technical field of industrial waste gas treatment, and particularly relates to a sintering flue gas cooperative treatment system.
Background
In industrial production, particularly in the working process of chemical plants, steel plants, pharmaceutical plants and oil refineries, a large amount of waste gas is generated, and if the waste gas is not treated, the phenomena of acid rain, global warming, haze and the like are caused, so that the environment is seriously polluted, and the human health is harmed.
Sintering flue gas is one of waste gases, and the main pollution components are sulfur dioxide, nitric oxide and dust. The sintering flue gas emission is large, the initial flue gas temperature is low, and the desulfurization, denitrification and dust removal method is generally adopted for treatment at present in China. At present, the desulfurization, denitrification and dust removal method has more processes, and can be divided into a wet process, a dry process and a semi-dry and semi-wet process according to the dry and wet state in the treatment process, wherein the wet process generally has the problems of serious corrosion, high operation and maintenance cost, easy secondary pollution, corrosion blockage of a flue gas heat exchanger and the like; the dry process has the problems of low desulfurization and denitrification efficiency, slow reaction speed, large equipment and the like; the semi-dry semi-wet process has the problems of byproduct treatment, poor operation stability, active coke treatment and the like. Therefore, the desulfurization, denitrification and dust removal process should be innovated continuously.
The sintering flue gas multi-pollutant cooperative treatment means that a plurality of pollutants are comprehensively removed by unit links or unit environment-friendly equipment linking and matching coupling through one technology or a plurality of technical combinations, and the problems of equipment corrosion, blockage, poor system operation stability, low utilization rate of byproducts and the like are solved.
Disclosure of Invention
The invention mainly solves the technical problems in the prior art and provides a sintering flue gas cooperative treatment system.
The technical problem of the invention is mainly solved by the following technical scheme: a sintering flue gas cooperative treatment system comprises an electric dust collector, a first fan, a desulfurization device, a flue gas condensation dehydrator, a flue gas preheater, a denitration device, a bag-type dust remover, a pipeline and a second fan connected with a chimney, wherein the output end of the electric dust collector is connected with the input end of the first fan through the pipeline, the output end of the first fan is connected with the input end of the desulfurization device through the pipeline, the output end of the desulfurization device is connected with the input end of the flue gas condensation dehydrator through the pipeline, the output end of the flue gas condensation dehydrator is connected with the input end of the flue gas preheater through the pipeline, the output end of the flue gas preheater is connected with the input end of the denitration device through the pipeline, the output end of the denitration device is connected with the input end of the bag-type dust remover through the pipeline, the output end of the bag-type dust remover is connected with, and the output end of the second fan is connected with the chimney through a pipeline.
Preferably, the desulfurization equipment comprises a desulfurization tower, a flue gas inlet is formed in the side wall of the desulfurization tower, a slurry pool for containing desulfurization absorbent is arranged at the bottom in the desulfurization tower below the flue gas inlet, a first spray layer, a second spray layer and a third spray layer are arranged in the desulfurization tower from bottom to top at intervals above the slurry pool, the first spray layer, the second spray layer and the third spray layer respectively comprise a spray pipe and an atomizing spray head arranged on the spray pipe, a defogging device is arranged in the desulfurization tower above the third spray layer, an oxidation fan and a circulating pump are arranged outside the desulfurization tower, the output end of the oxidation fan is communicated with the slurry pool, the input end of the circulating pump is communicated with the slurry pool, the output end of the circulating pump is connected with the spray pipe, a stirring device is further arranged on the side wall of the desulfurization tower, and extends into the slurry pool, and a flue gas outlet is formed in the top of the desulfurizing tower.
Preferably, airflow choked flow devices are arranged between the first spraying layer and the second spraying layer and between the second spraying layer and the third spraying layer, each airflow choked flow device comprises a fixing plate fixedly connected with the inner wall of the desulfurization tower, a through hole is formed in each fixing plate, and the edge of each through hole is turned over at an angle of 30 degrees downwards.
Preferably, the stirring device comprises a stirring motor arranged outside the desulfurization tower and a stirring blade extending into the slurry pool, and the stirring motor is connected with the stirring blade.
Preferably, the defogging device includes the motor frame that links to each other with the desulfurizing tower inner wall, installs the net twine dish motor on the motor frame and the net twine dish that links to each other with the net twine dish motor, the net twine dish includes intranet plate rail and outer net plate rail, intranet plate rail and net twine dish motor link to each other, fixed mounting has a plurality of radial spokes that are between intranet plate rail and the outer net plate rail, the periphery of net twine dish is equipped with the baffle, the baffle links to each other with the inner wall of desulfurizing tower.
Preferably, the desulfurization absorbent is one of limestone solution, magnesium oxide solution, ammonia water solution and sodium hydroxide solution.
Preferably, the denitration equipment comprises a denitration tower internally provided with three layers of denitration catalysts, and an air inlet flue and an exhaust flue which are connected with the denitration tower, wherein a flue gas heat exchanger for heat exchange is connected between the air inlet flue and the exhaust flue, the air inlet flue is connected with a reducing agent conveying device and a flue combustor for heating sintering flue gas flowing through the air inlet flue, the reducing agent conveying device is positioned at the downstream of the flue combustor, a drainage plate for draining the sintering flue gas is arranged in the air inlet flue, and the drainage plate is positioned at the downstream of the reducing agent conveying device.
Preferably, the flue combustor has four output ends, namely a first output end, a second output end, a third output end and a fourth output end, the first output end of the flue combustor is connected with a primary heat-supplementing pipeline, the other end of the primary heat-supplementing pipeline is communicated with the air inlet flue, the second output end of the flue combustor is connected with a secondary heat-supplementing pipeline, the other end of the secondary heat-supplementing pipeline is communicated with the air inlet flue, the secondary heat-supplementing pipeline is located at the downstream of the primary heat-supplementing pipeline, the third output end of the flue combustor is connected with a tertiary heat-supplementing pipeline, and the other end of the tertiary heat-supplementing pipeline is connected with the flue gas preheater; and a fourth output end of the flue combustor is connected with a heat conveying pipeline, and the other end of the heat conveying pipeline is connected with a reducing agent conveying device.
Preferably, reductant conveyor includes aqueous ammonia holding vessel, aqueous ammonia pipeline, spray gun, high temperature dilution fan, high temperature pipeline, aqueous ammonia gasifier, ammonia pipeline and ammonia distributor, the aqueous ammonia holding vessel passes through aqueous ammonia pipeline and links to each other with the spray gun, the spray gun sets up in the aqueous ammonia gasifier, high temperature dilution fan passes through high temperature pipeline and links to each other with the aqueous ammonia gasifier, the aqueous ammonia gasifier passes through the ammonia pipeline and links to each other with the ammonia distributor, the ammonia distributor sets up in the flue that admits air, the ammonia distributor includes connecting portion and a plurality of radial outlet duct that is, connecting portion are linked together with the ammonia pipeline, the outlet duct is linked together with connecting portion, just be equipped with a plurality of ventholes on the outlet duct.
Preferably, the flue gas heat exchanger is a regenerative heat exchanger or a dividing wall type heat exchanger.
The invention has the following beneficial effects: compared with the prior art, the invention has the advantages of small floor area, low investment cost, low corrosivity to equipment and high desulfurization, denitrification and dust removal efficiency, and ensures that sulfur dioxide, particulate matters and nitric oxide in sintering flue gas meet the requirements of ultralow emission standards. The invention efficiently recovers and utilizes the waste heat of the sintering flue gas, reduces the energy consumption in the treatment process, reduces the operation cost, can realize the long-term stable low-energy consumption operation, and has stronger practicability on the sintering flue gas.
Drawings
FIG. 1 is a schematic diagram of an embodiment of the present invention;
FIG. 2 is a schematic view of a constitution of a desulfurization apparatus of the present invention;
FIG. 3 is a schematic view of an arrangement of the airflow blocking device of the present invention;
FIG. 4 is a schematic cross-sectional view of an airflow blocking device of the present invention;
FIG. 5 is a schematic view of a connection structure of the net disk motor and the net disk of the present invention;
FIG. 6 is an enlarged schematic view of portion A of FIG. 5;
FIG. 7 is a schematic diagram of one configuration of a reductant delivery device of the present invention;
FIG. 8 is a schematic diagram of an ammonia gas distributor according to the present invention.
In the figure: 1. an electric dust collector; 2. a first fan; 3. a desulfurization unit; 4. a flue gas condensation dehydrator; 5. a flue gas preheater; 6. denitration equipment; 7. a bag-type dust collector; 8, pipelines; 9. a second fan; 10. a chimney; 11. a desulfurizing tower; 12. a flue gas inlet; 13. a slurry tank; 14. a first spray layer; 15. a second spray layer; 16. a third spray layer; 17. a shower pipe; 18. an atomizing spray head; 19. a dust removal device; 20. an oxidation fan; 21. a circulation pump; 22. a flue gas outlet; 23. an airflow choking device; 24. a fixing plate; 25. a through hole; 26. a stirring motor; 27. a stirring blade; 28. a motor frame; 29. a net disk motor; 30. a net disk; 31. an internal net plate frame; 32. an outer network disk frame; 33. spokes; 34. a baffle plate; 35. a denitration catalyst; 36. a denitration tower; 37. an air intake flue; 38. an exhaust flue; 39. a flue gas heat exchanger; 40. a reductant delivery device; 41. a flue burner; 42. a drainage plate; 43. a primary heat-supplementing pipeline; 44. a secondary heat supplementing pipeline; 45. a third heat supplementing pipeline; 46. a heat delivery conduit; 47. an ammonia storage tank; 48. an ammonia water transfer line; 49. a spray gun; 50. a high temperature dilution fan; 51. a high temperature pipeline; 52. an ammonia water gasification furnace; 53. an ammonia gas line; 54. an ammonia gas distributor; 55. a connecting portion; 56. an air outlet pipe; 57. and an air outlet.
Detailed Description
The technical scheme of the invention is further specifically described by the following embodiments and the accompanying drawings.
Example (b): a sintering flue gas cooperative treatment system is shown in figures 1-8 and comprises an electric dust collector 1, a first fan 2, a desulfurization device 3, a flue gas condensation dehydrator 4, a flue gas preheater 5, a denitration device 6, a bag-type dust collector 7, a pipeline 8 and a second fan 9 connected with a chimney 10, wherein the electric dust collector 1, the first fan 2, the desulfurization device 3, the flue gas condensation dehydrator 4, the flue gas preheater 5, the denitration device 6, the bag-type dust collector 7, the second fan 9 and the chimney 10 are sequentially arranged along a sintering flue gas treatment process, the input end of the electric dust collector 1 is used for introducing sintering flue gas, the output end of the electric dust collector 1 is connected with the input end of the first fan 2 through the pipeline 8, the output end of the first fan 2 is connected with the input end of the desulfurization device 3 through the pipeline 8, the output end of the desulfurization device 3 is connected with the input end of the flue gas condensation dehydrator 4 through the pipeline 8, the output end of the flue gas condensation dehydrator 4 is connected with the input end of the flue gas preheater 5 through a pipeline 8, the output end of the flue gas preheater 5 is connected with the input end of the denitration device 6 through the pipeline 8, the output end of the denitration device 6 is connected with the input end of the bag-type dust collector 7 through the pipeline 8, the bag-type dust collector 7 adopts a three-time bag-type dust collector, the output end of the bag-type dust collector 7 is connected with the input end of the second fan 9 through the pipeline 8, and the output end of the second fan 9 is connected with the chimney 10 through the pipeline 8.
The electrostatic precipitator 1 removes dust to the sintering flue gas, will wherein solid-state particulate matter detach to prevent flue gas dust to follow-up firing equipment's adverse effect, more can block up the pipeline if the dust, the dust also can influence the heating effect in follow-up firing equipment deposits, and shortens the firing equipment life-span.
The desulfurization equipment 3 comprises a desulfurization tower 11, a flue gas inlet 12 is formed in the side wall of the desulfurization tower 11, a slurry pool 13 for containing a desulfurization absorbent is arranged at the bottom in the desulfurization tower 11 below the flue gas inlet 12, a first spraying layer 14, a second spraying layer 15 and a third spraying layer 16 are arranged in the desulfurization tower 11 above the slurry pool 13 at intervals from bottom to top, the first spraying layer 14, the second spraying layer 15 and the third spraying layer 16 respectively comprise a spraying pipe 17 and an atomizing nozzle 18 arranged on the spraying pipe 17, a defogging device is arranged in the desulfurization tower 11 above the third spraying layer 16, an oxidation fan 20 and a circulating pump 21 are arranged outside the desulfurization tower 11, the output end of the oxidation fan 20 is communicated with the slurry pool 13, the input end of the circulating pump 21 is communicated with the slurry pool 13, the output end of the circulating pump is connected with the spraying pipe 17, and a stirring device is further arranged on the side wall of the desulfurization tower 11, the stirring device extends into the slurry pool 13, and the top of the desulfurizing tower 11 is provided with a flue gas outlet 22.
The desulfurization absorbent adopts an absorbent with good sulfur absorption effect, fast reaction and low cost, such as any one of limestone solution, magnesium oxide solution, ammonia water solution and sodium hydroxide solution. The stirring device comprises a stirring motor 26 arranged outside the desulfurizing tower 11 and a stirring blade 27 extending into the slurry pool 13, and the stirring motor 26 is connected with the stirring blade 27.
The desulfurization absorbent in the slurry pool 13 enters each spray pipe 17 through a circulating pump 21, and is sprayed out through an atomizing nozzle 18 arranged on each spray pipe 17 to react with sulfur dioxide in the sintering flue gas. Through set up a plurality of layers that spray in desulfurizing tower 11, make the desulfurization reaction of sintering flue gas more thorough, first layer 14, the second sprays layer 15 and the third sprays layer 16 and links to each other with thick liquid pond 13 through circulating pump 21 separately simultaneously, and independent work each other can adjust the operating condition on each layer that sprays at any time according to the site work condition, plays the effect of energy saving. The oxidation fan 20 introduces air into the slurry tank 13 to promote oxidation of the desulfurization absorbent absorbing sulfur dioxide, and the stirring device is used to prevent precipitation of oxidized solid particles.
Airflow choked flow devices 23 are arranged between the first spraying layer 14 and the second spraying layer 15 and between the second spraying layer 15 and the third spraying layer 16, each airflow choked flow device 23 comprises a fixing plate 24 fixedly connected with the inner wall of the desulfurization tower 11, a through hole 25 is formed in each fixing plate 24, and the edge of each through hole 25 is turned over by 30 degrees downwards. The airflow blocking device 23 is used for blocking sintering flue gas from rapidly passing through the desulfurizing tower 11, so that sulfur dioxide in the sintering flue gas and the desulfurizing absorbent can fully react.
The flue gas condensation dehydrator 4 is used for further removing water vapor from the desulfurized sintering flue gas, and the heat exchanger in the flue gas condensation dehydrator 4 is made of corrosion-resistant alloy materials or non-metal materials, so that the flue gas condensation dehydrator has the characteristics of high heat exchange efficiency and good corrosion resistance. The water condensed by the flue gas condensation dehydrator 4 can be used as the supplementary water of the desulfurization equipment 3.
The defogging device includes the motor frame 28 that links to each other with desulfurizing tower 11 inner wall, installs net dish motor 29 on motor frame 28 and the net dish 30 that links to each other with net dish motor 29, net dish 30 includes interior net dish rail 31 and outer net dish rail 32, interior net dish rail 31 and net dish motor 29 link to each other, fixed mounting has a plurality of radial spokes 33 that are between interior net dish rail 31 and the outer net dish rail 32, the periphery of net dish 30 is equipped with baffle 34, baffle 34 links to each other with desulfurizing tower 11's inner wall. After desulfurization, the sintering flue gas containing water mist moves upwards to a demisting device, then a net disc motor 29 drives a net disc 30 to rotate, the net disc 30 rotates at a high speed to form a shield with a certain gap, the gap on the shield appears, when the sintering flue gas containing water mist passes through the gap, the water mist is larger due to the fact that the rotating speed of the net disc is fast, the water mist cannot collide with the spokes 33 and is intercepted, and the air particles are smaller in size and can easily pass through the gap, so that the separation of the water mist and the sintering flue gas is achieved; meanwhile, under the action of centrifugal force, the water mist is thrown onto the baffle 34 and is converged on the baffle 34 to form a liquid state, and the liquid state flows back to the slurry pool 13 along the inner wall of the desulfurizing tower 11.
The denitration device 6 comprises a denitration tower 36 internally provided with a three-layer denitration catalyst 35, and an air inlet flue 37 and an exhaust flue 38 connected with the denitration tower 36, wherein the denitration catalyst 35 comprises any one or a combination of at least two of a vanadium-based activated carbon honeycomb catalyst, a vanadium-tungsten-titanium honeycomb catalyst or a vanadium-tungsten-titanium plate catalyst, a flue gas heat exchanger 39 for heat exchange is connected between the air inlet flue 37 and the exhaust flue 38, the flue gas heat exchanger 39 is a heat accumulating type heat exchanger or a dividing wall type heat exchanger, the flue gas heat exchanger 39 is loaded with an ash cleaning device 19, the ash cleaning device 19 can adopt an acoustic wave soot blower which is used for cleaning accumulated ash on the flue gas heat exchanger 39 and preventing the flue gas heat exchanger 39 from being blocked, the air inlet flue 37 is connected with a reducing agent conveying device 40 and a flue combustor 41 for heating sintered flue gas flowing through the air inlet flue, reducing agent conveyor 40 is located the low reaches of flue combustor 41, be equipped with the drainage plate 42 that is used for the drainage to sintering flue gas in the flue 37 of admitting air, drainage plate 42 is located reducing agent conveyor 40's low reaches, and drainage plate 42 can carry out the drainage to sintering flue gas, can effectively avoid sintering flue gas because inertia direct impact flue wall, can make the reducing agent and the sintering flue gas intensive mixing of reducing agent conveyor 40 output simultaneously.
The reducing agent delivery device 40 comprises an ammonia water storage tank 47 loaded with ammonia water solution, an ammonia water delivery pipeline 48, a spray gun 49, a high-temperature dilution fan 50, a high-temperature pipeline 51, an ammonia water gasification furnace 52, an ammonia gas pipeline 53 and an ammonia gas distributor 54, the ammonia water storage tank 47 is connected with a spray gun 49 through an ammonia water delivery pipeline 48, the spray gun 49 is arranged in an ammonia water gasification furnace 52, the high-temperature dilution fan 50 is connected with an ammonia water gasification furnace 52 through a high-temperature pipeline 51, the ammonia water gasification furnace 52 is connected with an ammonia distributor 54 through an ammonia pipeline 53, the ammonia distributor 54 is arranged in the air inlet flue 37, the ammonia distributor 54 comprises a connecting part 55 and a plurality of radial outlet pipes 56, the connecting part 55 is communicated with the ammonia pipeline 53, the gas outlet pipe 56 is communicated with the connecting part 55, and a plurality of gas outlet holes 57 are formed in the gas outlet pipe 56.
The flue combustor 41 is provided with four output ends which are respectively a first output end, a second output end, a third output end and a fourth output end, the first output end of the flue combustor 41 is connected with a primary heat-supplementing pipeline 43, the other end of the primary heat-supplementing pipeline 43 is communicated with an air inlet flue 37, the second output end of the flue combustor 41 is connected with a secondary heat-supplementing pipeline 44, the other end of the secondary heat-supplementing pipeline 44 is communicated with the air inlet flue 37, the secondary heat-supplementing pipeline 44 is positioned at the downstream of the primary heat-supplementing pipeline 43, the third output end of the flue combustor 41 is connected with a tertiary heat-supplementing pipeline 45, and the other end of the tertiary heat-supplementing pipeline 45 is connected with the flue gas preheater 5; a heat conveying pipe 46 is connected to a fourth output end of the flue burner 41, and the other end of the heat conveying pipe 46 is connected to a high-temperature pipeline 51.
The sintering flue gas enters the denitration device 6 through the gas inlet flue 37, the flue burner 41 heats the sintering flue gas to a proper temperature, and then the sintering flue gas is mixed with ammonia gas output by the reducing agent conveying device 40 and then introduced to the surface of the denitration catalyst 35 together for catalytic reaction to remove nitrogen oxides; then, when the high-temperature sintering flue gas is discharged through the exhaust flue 38, the high-temperature sintering flue gas in the exhaust flue 38 and the low-temperature sintering flue gas in the air inlet flue 37 are subjected to heat exchange treatment by using the flue gas heat exchanger 39, and the heat of the high-temperature sintering flue gas is recovered to heat the low-temperature sintering flue gas, so that the energy consumption of the flue combustor 41 is reduced by the arrangement of the flue gas heat exchanger 39, and the effect of saving energy is achieved. The flue combustor 41 has four output ends, a first output end of the flue combustor 41 is connected with the air inlet flue 37 through a first heat supplementing pipeline 43, a second output end of the flue combustor 41 is connected with the air inlet flue 37 through a second heat supplementing pipeline 44, and the flue combustor 41 can selectively perform primary heating or secondary heating on sintering flue gas according to site working conditions. The third output end of the flue combustor 41 is connected with the flue gas preheater 5 through the tertiary heat supplementing pipeline 45, so that redundant heat can be transmitted to the flue gas preheater 5, and the energy consumption of the flue gas preheater 5 is reduced. A fourth output of the flue burner 41 is connected to a high temperature line 51 by means of a superheat delivery conduit 46 for transferring heat to vaporize the aqueous ammonia solution.
The working process of the reducing agent delivery device 40 is as follows: the ammonia water storage tank 47 is loaded with ammonia water solution, the spray gun 49 atomizes the ammonia water solution and then uniformly sprays the ammonia water solution into the ammonia water gasification furnace 52, the flue burner 41 conveys heat to the high-temperature pipeline 51 through the heat conveying pipeline 46, the high-temperature dilution fan 50 conveys the heat into the ammonia water gasification furnace 52, the ammonia water solution is diluted and gasified into ammonia gas, and the ammonia gas enters the air inlet flue 37 through the ammonia gas distributor 54 and is fully mixed with the heated sintering flue gas. Through the design that adopts ammonia distributor 54, can effectual improvement ammonia and the misce bene degree of sintering flue gas, improve the denitration effect.
The method for treating the sintering flue gas comprises the following steps:
(1) dust removal: introducing the sintering flue gas into an electric dust remover, and removing dust from the sintering flue gas by using the electric dust remover to remove solid particles in the sintering flue gas;
(2) and (3) desulfurization: introducing the sintering flue gas obtained in the step into desulfurization equipment, and removing sulfur dioxide by utilizing the reaction of a desulfurization absorbent and sulfur dioxide in the sintering flue gas;
(3) dewatering: after desulfurization, the sintering flue gas obtained in the above steps contains a small amount of water vapor, the water vapor is condensed into a liquid state by using a flue gas condensation dehydrator, and the water vapor is separated from the flue gas;
(4) heating: after condensation, the temperature of the sintering flue gas obtained in the step is low, and a flue gas preheater is used for preheating the sintering flue gas;
(5) denitration: introducing the sintering flue gas obtained in the step and a reducing agent into the surface of a denitration catalyst together to perform a catalytic reaction to remove nitrogen oxides;
(6) and (3) dedusting again: carrying out dust removal treatment on the sintering flue gas obtained in the step by using a bag-type dust remover so as to enable the sintering flue gas to meet the emission standard;
(7) discharging: and discharging the sintering flue gas obtained in the step into the atmosphere through a chimney.
Compared with the prior art, the invention has the advantages of small occupied area, low investment cost, low corrosivity on equipment and high desulfurization, denitrification and dust removal efficiency, and ensures that sulfur dioxide, particulate matters and nitrogen oxides in the sintering flue gas meet the requirements of ultralow emission standards. The invention efficiently recovers and utilizes the waste heat of the sintering flue gas, reduces the energy consumption in the treatment process, reduces the operation cost, can realize the long-term stable low-energy consumption operation, and has stronger practicability on the sintering flue gas.
Finally, it should be noted that the above embodiments are merely representative examples of the present invention. It is obvious that the invention is not limited to the above-described embodiments, but that many variations are possible. Any simple modification, equivalent change and modification made to the above embodiments in accordance with the technical spirit of the present invention should be considered to be within the scope of the present invention.
Claims (10)
1. A sintering flue gas cooperative treatment system is characterized by comprising an electric precipitator, a first fan, a desulfurization device, a flue gas condensation dehydrator, a flue gas preheater, a denitration device, a bag-type dust remover, a pipeline and a second fan connected with a chimney, wherein the output end of the electric precipitator is connected with the input end of the first fan through the pipeline, the output end of the first fan is connected with the input end of the desulfurization device through the pipeline, the output end of the desulfurization device is connected with the input end of the flue gas condensation dehydrator through the pipeline, the output end of the flue gas condensation dehydrator is connected with the input end of the flue gas preheater through the pipeline, the output end of the flue gas preheater is connected with the input end of the denitration device through the pipeline, the output end of the denitration device is connected with the input end of the bag-type dust remover through the pipeline, the output end of the bag-type dust remover is connected with the input end, and the output end of the second fan is connected with the chimney through a pipeline.
2. The system of claim 1, wherein the desulfurization equipment comprises a desulfurization tower, a flue gas inlet is formed in a side wall of the desulfurization tower, a slurry pool for containing a desulfurization absorbent is arranged at the bottom in the desulfurization tower below the flue gas inlet, a first spray layer, a second spray layer and a third spray layer are arranged above the slurry pool in the desulfurization tower from bottom to top at intervals, each of the first spray layer, the second spray layer and the third spray layer comprises a spray pipe and an atomizing nozzle arranged on the spray pipe, a defogging device is arranged in the desulfurization tower above the third spray layer, an oxidation fan and a circulating pump are arranged outside the desulfurization tower, an output end of the oxidation fan is communicated with the slurry pool, an input end of the circulating pump is communicated with the slurry pool, an output end of the circulating pump is connected with the spray pipe, and a stirring device is further arranged on the side wall of the desulfurization tower, the stirring device extends into the slurry pool, and the top of the desulfurizing tower is provided with a flue gas outlet.
3. The system of claim 2, wherein airflow chokes are disposed between the first spraying layer and the second spraying layer, and between the second spraying layer and the third spraying layer, and each airflow chokes comprises a fixing plate fixedly connected to an inner wall of the desulfurization tower, a through hole is formed in the fixing plate, and an edge of the through hole is turned over by 30 degrees downward.
4. The system of claim 2, wherein the stirring device comprises a stirring motor disposed outside the desulfurization tower and a stirring blade extending into the slurry pool, and the stirring motor is connected to the stirring blade.
5. The system of claim 2, wherein the defogging device comprises a motor frame connected with the inner wall of the desulfurization tower, a net disk motor installed on the motor frame, and a net disk connected with the net disk motor, the net disk comprises an inner net disk frame and an outer net disk frame, the inner net disk frame is connected with the net disk motor, a plurality of radial spokes are fixedly installed between the inner net disk frame and the outer net disk frame, and a baffle is arranged on the periphery of the net disk and connected with the inner wall of the desulfurization tower.
6. The system for the cooperative treatment of sintering flue gas as claimed in claim 2, wherein the desulfurization absorbent is one of limestone solution, magnesium oxide solution, ammonia water solution and sodium hydroxide solution.
7. The system of claim 1, wherein the denitration device comprises a denitration tower provided with three layers of denitration catalysts, and an air inlet flue and an air outlet flue connected with the denitration tower, a flue gas heat exchanger for heat exchange is connected between the air inlet flue and the air outlet flue, the air inlet flue is connected with a reducing agent conveying device and a flue combustor for heating sintering flue gas flowing through the air inlet flue, the reducing agent conveying device is located at the downstream of the flue combustor, a flow guide plate for guiding the sintering flue gas is arranged in the air inlet flue, and the flow guide plate is located at the downstream of the reducing agent conveying device.
8. The system of claim 7, wherein the flue combustor has four output ends, namely a first output end, a second output end, a third output end and a fourth output end, the first output end of the flue combustor is connected with a primary heat-supplementing pipeline, the other end of the primary heat-supplementing pipeline is communicated with the air inlet flue, the second output end of the flue combustor is connected with a secondary heat-supplementing pipeline, the other end of the secondary heat-supplementing pipeline is communicated with the air inlet flue, the secondary heat-supplementing pipeline is located at the downstream of the primary heat-supplementing pipeline, the third output end of the flue combustor is connected with a tertiary heat-supplementing pipeline, and the other end of the tertiary heat-supplementing pipeline is connected with the flue gas preheater; and a fourth output end of the flue combustor is connected with a heat conveying pipeline, and the other end of the heat conveying pipeline is connected with a reducing agent conveying device.
9. The system of claim 7, wherein the reducing agent delivery device comprises an ammonia storage tank, an ammonia delivery line, a spray gun, a high-temperature dilution fan, a high-temperature line, an ammonia gasifier, an ammonia line and an ammonia distributor, the ammonia storage tank is connected with the spray gun through the ammonia delivery line, the spray gun is arranged in the ammonia gasifier, the high-temperature dilution fan is connected with the ammonia gasifier through the high-temperature line, the ammonia gasifier is connected with the ammonia distributor through the ammonia line, the ammonia distributor is arranged in the air inlet flue, the ammonia distributor comprises a connecting portion and a plurality of radial outlet pipes, the connecting portion is communicated with the ammonia line, the outlet pipes are communicated with the connecting portion, and a plurality of outlet holes are formed in the outlet pipes.
10. The system of claim 7, wherein the flue gas heat exchanger is a regenerative heat exchanger or a dividing wall heat exchanger.
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| CN201911376140.8A CN110917863A (en) | 2019-12-27 | 2019-12-27 | Sintering flue gas is treatment system in coordination |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112915760A (en) * | 2021-01-21 | 2021-06-08 | 绍兴越信环保科技有限公司 | Solid waste pyrolysis flue gas cooperative treatment system |
| CN115591393A (en) * | 2022-12-07 | 2023-01-13 | 北京天中方环保科技有限公司（Cn） | Desulfurization and denitrification combined equipment and use method thereof |
-
2019
- 2019-12-27 CN CN201911376140.8A patent/CN110917863A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112915760A (en) * | 2021-01-21 | 2021-06-08 | 绍兴越信环保科技有限公司 | Solid waste pyrolysis flue gas cooperative treatment system |
| CN115591393A (en) * | 2022-12-07 | 2023-01-13 | 北京天中方环保科技有限公司（Cn） | Desulfurization and denitrification combined equipment and use method thereof |
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