CN112742178A - Flue gas desulfurization and SCR denitration combined system and flue gas treatment process - Google Patents
Flue gas desulfurization and SCR denitration combined system and flue gas treatment process Download PDFInfo
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- CN112742178A CN112742178A CN202110003090.XA CN202110003090A CN112742178A CN 112742178 A CN112742178 A CN 112742178A CN 202110003090 A CN202110003090 A CN 202110003090A CN 112742178 A CN112742178 A CN 112742178A
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- 239000003546 flue gas Substances 0.000 title claims abstract description 426
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 418
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 135
- 230000023556 desulfurization Effects 0.000 title claims abstract description 135
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000007788 liquid Substances 0.000 claims abstract description 53
- 238000001816 cooling Methods 0.000 claims abstract description 44
- 239000000779 smoke Substances 0.000 claims abstract description 34
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 26
- 238000005406 washing Methods 0.000 claims abstract description 22
- 230000003009 desulfurizing effect Effects 0.000 claims description 46
- 238000012856 packing Methods 0.000 claims description 24
- 238000005507 spraying Methods 0.000 claims description 19
- 238000006243 chemical reaction Methods 0.000 claims description 17
- 230000000630 rising effect Effects 0.000 claims description 15
- 238000002156 mixing Methods 0.000 claims description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 206010015137 Eructation Diseases 0.000 claims 1
- 239000011148 porous material Substances 0.000 claims 1
- 239000000243 solution Substances 0.000 description 39
- 239000007789 gas Substances 0.000 description 19
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 239000000571 coke Substances 0.000 description 8
- 238000011049 filling Methods 0.000 description 8
- 239000000463 material Substances 0.000 description 8
- 239000003054 catalyst Substances 0.000 description 7
- 238000003795 desorption Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 238000005245 sintering Methods 0.000 description 5
- 229910000831 Steel Inorganic materials 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 4
- 150000001412 amines Chemical class 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 4
- 239000000945 filler Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 239000010959 steel Substances 0.000 description 4
- 239000004471 Glycine Substances 0.000 description 3
- DHMQDGOQFOQNFH-UHFFFAOYSA-N Glycine Natural products NCC(O)=O DHMQDGOQFOQNFH-UHFFFAOYSA-N 0.000 description 3
- 239000000110 cooling liquid Substances 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- -1 hydroxyalkyl diamine compounds Chemical class 0.000 description 3
- 239000004071 soot Substances 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000005034 decoration Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000008235 industrial water Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000008188 pellet Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000003963 antioxidant agent Substances 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000007791 dehumidification Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000004401 flow injection analysis Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000002608 ionic liquid Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- GFNGCDBZVSLSFT-UHFFFAOYSA-N titanium vanadium Chemical group [Ti].[V] GFNGCDBZVSLSFT-UHFFFAOYSA-N 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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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
- B01D53/14—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 absorption
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
-
- 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
- B01D53/14—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 absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- 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
- B01D53/14—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 absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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
- B01D53/74—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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a flue gas desulfurization and SCR denitration combined system and a process, wherein the flue gas desulfurization system comprises a desulfurization tower, and the desulfurization tower comprises a flue gas washing section, a flue gas desulfurization section, a desulfurization liquid capturing section, a flue gas cooling section, a demisting section and a flue gas preheating section which are sequentially arranged from bottom to top; the smoke rotation accelerating device in the collecting section is provided with an air lifting hole, and the smoke is accelerated after passing through the air lifting hole; the opening degree of the air lifting hole is more than or equal to 25% and less than 100%; the flue gas heat exchange unit is connected with the flue gas preheating section; the flue gas mixer is sequentially connected with the flue gas heat exchange unit; SCR denitration reactor and heat exchanger. The desulfurization solution trapping section is arranged, SO that the desulfurization agent entrained in the flue gas can be trapped and recovered, the escape of the desulfurization agent and secondary pollution caused by the escape of the desulfurization agent are reduced, and SO is generated2And NOxThe emission concentration of (2) is low.
Description
Technical Field
The invention belongs to the field of metallurgical waste gas treatment and resource utilization, and particularly relates to a flue gas desulfurization and SCR denitration combined system and a flue gas treatment process.
Background
The organic amine method flue gas desulfurization technology is a common desulfurization technology applied at present, and organic amine is used as a desulfurizer to circularly absorb SO in flue gas2The process technology is applied to the fields of sintering flue gas desulfurization, nonferrous smelting flue gas desulfurization, sulfuric acid tail gas and the like.
The traditional organic amine method or ionic liquid method flue gas desulfurization technology mainly comprises a flue gas washing system, a desulfurization absorption system, a desulfurization solution regeneration system and a solution purification and impurity removal system. The process technology has the problems of serious escaping of the desulfurizer, high impurity ions in the solution, difficult solution regeneration and the like in engineering application.
Chinese patent No. CN202146708U discloses a flue gas desulfurization system, which comprises a flue gas washing section, an absorption section, and a desulfurization solution capturing and recovering section, which are sequentially arranged along the flow direction of flue gas. The system solves a series of problems of high content of suspended impurities in the desulfurization solution, system blockage, low desulfurization rate and the like in the conventional desulfurization system.
Chinese patent document No. CN103706237A discloses a flue gas desulfurization system, which includes a flue gas desulfurization tower, and is divided into a washing section, an absorption section and a recovery section along the flow direction of flue gas in the flue gas desulfurization tower, wherein a desulfurization combination of a filler layer desulfurization and a spray desulfurization device is provided in the absorption section in the flue gas desulfurization tower, and the desulfurization efficiency is improved.
Chinese patent No. CN104587820A discloses a desulfurization solution negative pressure desorption process, in which a desorption tower is evacuated to negative pressure by a pressure reduction device to realize negative pressure desorption of rich liquid, and the temperature for desorption of the rich liquid is reduced, thereby reducing the desorption energy consumption, and reducing the escape loss of the desulfurization solution accompanying with acid gas entrainment during regeneration desorption, but the process has the disadvantage of high emission concentration of sulfur dioxide at the flue gas outlet.
Disclosure of Invention
In view of the above, the present invention provides a flue gas desulfurization and SCR denitration combined system and a flue gas treatment process, wherein the combined system can reduce the entrainment rate of the desulfurizing agent in the flue gas, and the SO is2And NOxThe emission concentration of (2) is low.
The invention provides a flue gas desulfurization and SCR denitration combined system which is characterized by comprising a desulfurization tower, wherein the desulfurization tower comprises a flue gas washing section, a flue gas desulfurization section, a desulfurization solution capturing section, a flue gas cooling section, a demisting section and a flue gas preheating section which are sequentially arranged from bottom to top;
the desulfurization liquid trapping section comprises a wire mesh packing layer, a liquid breaking disc, an air rising cap, a smoke rotation accelerating device, a high-pressure spraying device and a baffle plate which are arranged from bottom to top in sequence; the smoke rotation accelerating device is provided with an air lifting hole, and smoke passes through the air lifting hole and then is accelerated; the opening degree of the air lifting hole is more than or equal to 25% and less than 100%;
the flue gas heat exchange unit is connected with the flue gas preheating section;
the flue gas mixer is connected with the flue gas heat exchange unit;
the SCR denitration reactor is connected with the flue gas mixer and is provided with an ammonia gas inlet;
and the heat exchanger is connected with the SCR denitration reactor.
Preferably, the aperture of the air lifting hole is 40 cm-80 cm;
the hole spacing of the air lifting holes is 30-60 cm;
the inclination angle of the baffle plate is 0-60 degrees.
Preferably, the flue gas cooling section sets up liquid-break dish, liter gas cover, packing layer and liquid distribution layer from bottom to top in proper order.
Preferably, the demister section comprises an assembly of a ridge demister and a flat plate demister;
the flat plate demister comprises blades with parallel baffling; the blade pitch is 28-32 mm.
Preferably, the height of the silk screen packing layer is 0.3-0.5 m;
the resistance of the silk screen packing layer is 200-300 Pa.
The invention provides a method for performing desulfurization and denitrification on flue gas by adopting the combined system in the technical scheme, which comprises the following steps:
washing the flue gas to be treated, and then desulfurizing by adopting a desulfurizing agent to obtain desulfurized flue gas mixed with the desulfurizing agent;
roughly trapping the desulfurizer in the desulfurization flue gas mixed with the desulfurizer, accelerating the desulfurization flue gas through an air lifting hole, reversely contacting atomized liquid drops, colliding to a baffle plate, and then finely trapping to obtain the flue gas without the desulfurizer;
cooling and dehumidifying the flue gas subjected to desulfurizer removal, and then demisting to obtain demisted flue gas;
preheating the demisted flue gas to obtain preheated flue gas;
carrying out flue gas heat exchange on the preheated flue gas to obtain flue gas to be denitrated;
and mixing the flue gas to be denitrated with the flue gas of the hot blast stove, carrying out denitration reaction, and cooling to obtain the treated flue gas.
Preferably, SO in the flue gas to be treated2The concentration is 5000-8000 mg/m3、NOxThe concentration is 200-300 mg/m3The smoke content is 0-50 mg/m3The humidity of the flue gas is 7-10%, and the oxygen content is 14-16.5%.
Preferably, the desulfurization flue gas mixed with the desulfurizer is accelerated to 3.6-8.4 m/s through the air rising holes.
Preferably, the temperature of the flue gas to be treated is 80-160 ℃;
the temperature of the flue gas from which the desulfurizer is removed is 50-55 ℃;
the temperature of the demisted flue gas is 42-47 ℃;
the temperature of the preheated flue gas is 50-55 ℃;
the temperature of the flue gas to be denitrified is 248-252 ℃;
the temperature of the denitration reaction is 290-310 ℃;
the temperature of the flue gas of the denitration reaction is 285-290 ℃.
The invention provides a flue gas desulfurization and SCR denitration combined system, which comprises a desulfurization tower, wherein the desulfurization tower comprises a flue gas washing section, a flue gas desulfurization section, a desulfurization liquid capturing section, a flue gas cooling section, a demisting section and a flue gas preheating section which are sequentially arranged from bottom to top; the desulfurization solution trapping section comprises a plurality of sections which are arranged from bottom to top in sequenceArranging a silk screen packing layer, a liquid breaking disc, an air rising cap, a smoke rotation accelerating device, a high-pressure spraying device and a baffle plate; the smoke rotation accelerating device is provided with an air lifting hole, and smoke passes through the air lifting hole and then is accelerated; the opening degree of the air lifting hole is more than or equal to 25% and less than 100%; the flue gas heat exchange unit is connected with the flue gas preheating section; the flue gas mixer is connected with the flue gas heat exchange system; the SCR denitration reactor is connected with the flue gas mixer and is provided with an ammonia gas inlet; and the heat exchanger is connected with the SCR denitration reactor. According to the invention, the desulfurization solution trapping section is arranged, and comprises the screen packing layer, the liquid breaking disc, the gas rising cap, the flue gas rotation accelerating device, the high-pressure spraying device and the desulfurizer trapping baffle plate device which are sequentially arranged from bottom to top, SO that the trapping and recovery of the desulfurizer carried in the flue gas can be effectively realized, the escape of the desulfurization solution and the secondary pollution caused by the escape of the desulfurization solution are reduced, and SO is generated2And NOxThe emission concentration of (2) is low. The experimental results show that: the content of the flue gas desulfurizer in the flue gas is lower than 0.002%; SO in the discharged flue gas2The concentration can reach less than 50mg/m3；NOxCan reach a concentration of less than 50mg/m3The unit dosage of the coke oven gas is 2278Nm3Reduction of/h to 1900Nm3The specific power consumption is reduced from 2987KWh/h to 2485 KWh/h.
Drawings
FIG. 1 is a schematic structural diagram of a combined flue gas desulfurization and SCR denitration system provided by the present invention;
FIG. 2 is a schematic view of a process flow of a combined system for flue gas desulfurization and SCR denitration provided by the present invention for flue gas desulfurization and denitration.
Detailed Description
The invention provides a flue gas desulfurization and SCR denitration combined system, which comprises a desulfurization tower, wherein the desulfurization tower comprises a flue gas washing section, a flue gas desulfurization section, a desulfurization liquid capturing section, a flue gas cooling section, a demisting section and a flue gas preheating section which are sequentially arranged from bottom to top;
the desulfurization liquid trapping section comprises a wire mesh packing layer, a liquid breaking disc, an air rising cap, a smoke rotation accelerating device, a high-pressure spraying device and a baffle plate which are arranged from bottom to top in sequence; the smoke rotation accelerating device is provided with an air lifting hole, and smoke passes through the air lifting hole and then is accelerated; the opening degree of the air lifting hole is more than or equal to 25% and less than 100%;
the flue gas heat exchange unit is connected with the flue gas preheating section;
the flue gas mixer is connected with the flue gas heat exchange unit;
the SCR denitration reactor is connected with the flue gas mixer and is provided with an ammonia gas inlet;
and the heat exchanger is connected with the SCR denitration reactor.
The combined system for flue gas desulfurization and SCR denitration provided by the invention comprises a flue gas desulfurization system and an SCR system connected with the flue gas desulfurization system.
The flue gas desulfurization system comprises a desulfurization tower, and the desulfurization tower comprises a tower body and a tower body inner cavity surrounded by the tower body; the direction from bottom to top of the desulfurizing tower is the flowing direction of the flue gas. The desulfurizing tower comprises a flue gas washing section; the flue gas washing section cools the flue gas from the supercharger, removes acid mist and washes dust.
The desulfurizing tower comprises a flue gas desulfurization section; the flue gas desulfurization section is characterized in that a barren solution is in countercurrent contact with flue gas, sulfur dioxide in the flue gas to be treated is removed, a solution for absorbing the sulfur dioxide is called a pregnant solution, the pregnant solution is sent into a regeneration system for analysis after heat exchange through a pregnant solution tank, and the desorbed barren solution is sent into the desulfurization section for recycling after heat exchange. The desulfurization section comprises a liquid breaking disc, an air lifting cap, a desulfurization packing layer, a desulfurizer liquid distribution groove and a liquid inlet pipe which are arranged in sequence from bottom to top. The desulfurization section interruption liquid disc is used for collecting rich liquid formed after reverse contact reaction of desulfurization barren liquid and sulfur dioxide-containing flue gas in the desulfurization unit, the gas rising cap is used for enabling the washed flue gas to enter the desulfurization unit to be in contact reaction with the desulfurization barren liquid, and meanwhile, the loss of the desulfurization liquid caused by the fact that the reacted desulfurization rich liquid enters the desulfurization washing section from the gas rising hole is avoided.
In the invention, the desulfurization tower comprises a desulfurization solution capturing section; the desulfurization liquid trapping section comprises a wire mesh packing layer, a liquid breaking disc, an air rising cap, a flue gas rotation accelerating device, a high-pressure spraying device and a desulfurizer trapping baffle plate device which are sequentially arranged from bottom to top; the smoke rotation accelerating device is provided with an air lifting hole, and smoke passes through the air lifting hole and then is accelerated. The liquid interrupting disc of the desulfurization liquid trapping section is used for collecting liquid generated in the desulfurization trapping section in the processes of a flue gas rotation accelerating device, a high-pressure spraying device, a baffle plate and the like, so that the liquid is recycled, the liquid is intermittently sent into a desulfurization liquid-enriched tank, and the flue gas subjected to coarse demisting is introduced into the flue gas rotation accelerating device by the gas rising cap.
The desulfurization solution trapping section comprises a wire mesh packing layer; the wire mesh packing layer is used for carrying out coarse trapping on the desulfurization solution; the height of the screen mesh packing layer is 0.3-0.5 m, and the resistance of the screen mesh packing layer is 200-300 Pa. The desulfurization solution trapping section comprises a flue gas rotation accelerating device, wherein an air lifting hole is formed in the flue gas rotation accelerating device, and flue gas passes through the air lifting hole and then is accelerated, wherein the aperture of the air lifting hole is 40-80 cm; the hole spacing of the air lifting holes is 30-60 cm.
The cross section of the desulfurizing tower is divided into N units, each unit is an independent air lifting hole, the air lifting hole of each unit is parallel to a central cross beam of the desulfurizing tower, the cross beam is parallel to the ground, and the cross section parallel to the ground, with the cross beam as a reference line, is provided with N units of air lifting holes. The air lifting hole of each independent unit can adjust the opening degree of the air lifting hole. The opening degree of the air lifting holes is more than or equal to 25% and less than 100%, and preferably 50-85%; in specific embodiments, the opening of the gas-lifting holes is 85%, 50% or 60%.
The desulfurization flue gas mixed with the desulfurizer collides with the micronized liquid sprayed by the high-pressure spraying device after being accelerated, forms larger micro-pellets instantly and is gradually increased in the rising process. The pressure of the high-pressure spraying device during spraying is 3-5 atmospheric pressures.
The desulfurization solution trapping section comprises a desulfurizer trapping baffle plate; the ascending and high-speed large particles are collided on the baffle plate, so that the desulfurization solution carried in the flue gas is efficiently captured and recovered. The inclination angle of the baffle plate is 0-60 degrees, and preferably 30-50 degrees.
The invention controls the cross section area of the flue gas channel by adjusting the opening of the air lifting hole, thereby changing the flow velocity of the flue gas, realizing acceleration of the flue gas in the rotary accelerating device, then colliding with atomized liquid to form larger particles, obtaining higher trapping effect on the baffle plate, and simultaneously further reducing SO in the flue gas due to the combined action of the accelerated flue gas and high-pressure spray2And (4) concentration.
The desulfurizing tower comprises a flue gas cooling section; the flue gas cooling section is from up setting gradually disconnected liquid dish, rising gas cover, packing layer and liquid distribution layer down. The humidity of the flue gas which is removed and recycled by the baffle plate is about 10-15%, the temperature is 50-55 ℃, condensate can be generated in a cooling section, the condensate is collected by a liquid breaking disc, sent into a cooling system, cooled and then sent to a liquid distribution layer, and reversely contacted with the flue gas together with industrial water, so that the cooling and the dehumidification of the flue gas are realized, and the solution which is contacted with the flue gas is intermittently sent to a desulfurization rich liquid tank. After the temperature of the flue gas is reduced, the temperature reaches 40-50 ℃, the humidity is 6-10%, preferably 42-47 ℃, and the preferred humidity is 6.5-8.6%.
The desulfurizing tower comprises a demisting section; the demisting section comprises a combination of a ridge type demister and a flat plate demister; the flat plate demister comprises blades with parallel baffling; the blade pitch is 28-32 mm. Still set up the whirl injection system at the defogging section, wash the defogging device of defogging section, prevent defogging device's jam. The rotational flow injection system adopts industrial water. The height of the demisting section is preferably 200-300 mm.
The desulfurizing tower comprises a flue gas preheating section; the demisted flue gas is subjected to heat exchange to 50-55 ℃ through a flue gas heat exchanger (GGH); flue gas heat transfer adopts and gets into the flue gas before the desulfurization system booster fan and carries out the heat transfer, and flue gas passes through booster fan entering desulfurizing tower washing section after the heat transfer cooling, and the flue gas after being heaied up gets into flue gas heat transfer unit, overcomes the heat loss that supersaturation wet flue gas direct heating and arouse, has reduced the anticorrosive requirement of equipment moreover, has also carried out the thermal effective utilization of the flue gas of being handled simultaneously.
The combined system provided by the invention comprises a flue gas heat exchange unit connected with the flue gas preheating section; the flue gas heat exchange unit exchanges heat by adopting flue gas subjected to SCR denitration; cooling the denitrated flue gas to 90-100 ℃, and discharging the denitrated flue gas through a chimney; the temperature of the flue gas after heat exchange is raised to 250 ℃.
The combined system provided by the invention comprises a flue gas mixer connected with the flue gas heat exchange unit; mixing hot blast stove flue gas heated by coke oven gas, wherein the temperature of the hot blast stove flue gas is 800-1000 ℃; the temperature of the mixed flue gas is raised to more than 290 ℃.
The combined system provided by the invention comprises an SCR denitration reactor connected with the flue gas mixer, wherein an ammonia gas inlet is formed in the SCR denitration reactor; and a filler is arranged in the SCR denitration reactor, and the flue gas enters from the upper part of the filler and comes out from the bottom. In order to prevent the catalyst in the denitration reactor from being blocked, arranging a rake type soot blower and/or an acoustic wave soot blower in the denitration reactor, and increasing the blowing frequency of the acoustic wave soot blower; in the invention, a net chain type dust remover is preferably additionally arranged at the uppermost layer of the catalyst. The SCR denitration reaction adopts an SCR catalyst, the SCR catalyst is preferably a vanadium-titanium catalyst, and the temperature of the denitration reaction is preferably 290-310 ℃.
The combined system provided by the invention comprises a heat exchanger connected with the SCR denitration reactor. And (4) conveying the flue gas subjected to catalytic reaction denitration to a heat exchanger for cooling, and then discharging the flue gas outside.
The invention provides a method for performing desulfurization and denitrification on flue gas by adopting the combined system in the technical scheme, which comprises the following steps:
washing the flue gas to be treated, and then desulfurizing by adopting a desulfurizing agent to obtain desulfurized flue gas mixed with the desulfurizing agent;
roughly trapping the desulfurizer in the desulfurization flue gas mixed with the desulfurizer, accelerating the desulfurization flue gas through an air lifting hole, reversely contacting atomized liquid drops, colliding to a baffle plate, and then finely trapping to obtain the flue gas without the desulfurizer;
cooling and dehumidifying the flue gas subjected to desulfurizer removal, and then demisting to obtain demisted flue gas;
preheating the demisted flue gas to obtain preheated flue gas;
carrying out flue gas heat exchange on the preheated flue gas to obtain flue gas to be denitrated;
and mixing the flue gas to be denitrated with the flue gas of the hot blast stove, carrying out denitration reaction, and cooling to obtain the treated flue gas.
The method comprises the steps of washing the flue gas to be treated, and then desulfurizing by using a desulfurizing agent to obtain the desulfurizing flue gas mixed with the desulfurizing agent. SO in the flue gas to be treated2The concentration is 5000-8000 mg/m3、NOxThe concentration is 200-300 mg/m3The smoke content is 0-50 mg/m3The humidity of the flue gas is 7-10%, and the oxygen content is 14-16.5%. The temperature of the flue gas to be treated is 80-160 ℃. In a specific embodiment, SO in the flue gas to be treated2The concentration is 5500mg/m3、NOxThe concentration is 285mg/m3The smoke content is 15mg/m3The flue gas humidity is 10.5%; the flue gas temperature was 130 ℃. Demisting the washed flue gas by a demisting layer and then desulfurizing; and the demisting is carried out by baffle plates or plastic wire nets.
The temperature of the washed smoke is preferably 45-55 ℃; in a specific embodiment, the temperature of the scrubbed flue gas is 47 ℃.
Desulfurizing by adopting a desulfurizing agent; the desulfurizing agent is selected from organic amine desulfurizing solution, the main components comprise hydroxyalkyl diamine compounds, 2-hydroxyalkyl glycine and water, and the flue gas desulfurizing agent also comprises auxiliary components which are mainly active agents, antioxidants, corrosion inhibitors and the like. The total mass concentration of the hydroxyalkyl diamine compound and the 2-hydroxyalkyl glycine in the desulfurizer is 10-20%; hydroxyalkyl diamines: the mass concentration ratio of the 2-hydroxyalkyl glycine is 1: 5-10: 1. The temperature of the desulfurizer entering the desulfurizing tower is preferably 45-55 ℃; in a specific example, the temperature of the desulfurizing agent entering the desulfurizing tower is 48 ℃. The circulation volume of the desulfurizer is 270-320 m3Preferably 280 to 300 m/h3H; in a specific embodiment, the circulation amount of the desulfurizing agent is 290m3H is used as the reference value. The temperature of the desulfurization flue gas mixed with the desulfurizer obtained after desulfurization is preferably 50-60 ℃; detailed description of the inventionIn the examples, the temperature was 55 ℃. The desulfurizer reversely contacts with the flue gas to remove sulfur dioxide in the flue gas.
And (3) roughly trapping the desulfurizer in the desulfurization flue gas mixed with the desulfurizer, accelerating the desulfurization flue gas after passing through the air lifting hole, reversely contacting atomized liquid drops, colliding to the baffle plate, and then finely trapping to obtain the flue gas without the desulfurizer. The temperature of the flue gas from which the desulfurizer is removed is 50-55 ℃. The desulfurized flue gas of the desulfurizer is subjected to coarse trapping through a wire mesh filler; the mixed desulfurization smoke is accelerated by a smoke rotation accelerating device; the accelerating device is provided with an air lifting hole, and the opening degree of the air lifting hole is more than or equal to 25% and less than 100%, preferably 40-90%; in specific embodiments, the opening of the gas-lifting holes is 50%, 60%, 70% or 85%. And the desulfurization flue gas mixed with the desulfurizer is accelerated to 3.6-8.4 m/s after passing through the air lifting hole. Atomized liquid drops are sprayed by a high-pressure spraying device, and the liquid drops are water; atomized liquid drops are in reverse contact with the flue gas, formed micro-fine pellets are gradually increased in the rising process and are precisely captured after colliding with the baffle plate, and meanwhile, the combined action of the flue gas and high-pressure spraying is accelerated, SO that the SO in the flue gas can be further reduced2And (4) concentration. The humidity of the flue gas from which the desulfurizer is removed is 10-15%; the flue gas from which the desulfurizer is removed does not contain the desulfurizer basically, and can be reduced to below 0.002 wt%.
And cooling and dehumidifying the flue gas subjected to desulfurizer removal, and then demisting to obtain demisted flue gas. The invention cools and dehumidifies the flue gas in the flue gas cooling section; cooling to 45-46 ℃, and dehumidifying to the humidity of about 9%; in the specific embodiment, the temperature is reduced to 46 ℃, and the humidity is removed to 8.4%. The flue gas cooling and dehumidifying method is that cooling liquid is in reverse contact with the flue gas; the cooling liquid is from cooling liquid in a cooling heat exchange system; and the liquid collected by the liquid breaking disc is sent to a cooling system, and is sent to a flue gas temperature rising section after being cooled. The flue gas cooling section adopts solution from a cooling system, the solution is distributed by a liquid distributor and then reversely contacts with the flue gas in the packing layer, so that the flue gas is cooled, the solution after being washed and cooled by the flue gas is sent into the cooling system, certain condensate is intermittently discharged and sent into a desulfurization pregnant solution tank or used as water supplement for the configuration of a desulfurizer solution, and a certain amount of industrial fresh water is supplemented. The flue gas cooling section cools and condenses supersaturated water in the flue gas through the flue gas, and the moisture content of the flue gas is reduced. The invention preferably adopts a combined piece of the ridge type demisting device and the flat plate demisting device to demist the flue gas, and the temperature of the demisted flue gas is 40-50 ℃, preferably 42-47 ℃.
The invention preheats the demisted flue gas to obtain the preheated flue gas. The demisted flue gas is subjected to heat exchange through GGH, and the temperature is raised to 50-55 ℃. Flue gas heat exchange is carried out by adopting the flue gas before entering a booster fan of the desulfurization system, and the flue gas after heat exchange and temperature reduction enters a washing section of the desulfurization tower through the booster fan. The temperature of the preheated flue gas is 50-55 ℃. In the specific embodiment, the temperature of the preheated flue gas is 54 ℃ and the humidity is 8.3%.
After the preheated flue gas is obtained, the invention carries out flue gas heat exchange on the preheated flue gas to obtain the flue gas to be denitrated. The method comprises the steps of carrying out heat exchange on the preheated flue gas and the flue gas subjected to SCR denitration, so that the temperature of the flue gas to be denitrated reaches 248-252 ℃; in a specific embodiment, the temperature of the flue gas to be denitrated is 250 ℃.
The flue gas to be denitrated is mixed with the flue gas of the hot blast stove, subjected to denitration reaction and cooled to obtain the treated flue gas. Mixing the flue gas to be denitrated with the flue gas of a hot blast stove, and heating the flue gas to about 290 ℃; the temperature of the flue gas of the hot blast stove is 800-1000 ℃.
The denitration reaction is carried out in an SCR denitration reactor; NH is sprayed into the denitration reactor3And the catalyst enters from the upper part of the SCR catalytic reaction packing and comes out from the bottom of the packing. The temperature of the denitration reaction is 288-292 ℃. The temperature of the flue gas after the denitration reaction is 285-290 ℃.
And (4) after the denitration reaction is finished, exchanging heat and cooling the flue gas, and discharging the flue gas. Cooling to 90-110 ℃.
According to the invention, the desulfurization solution trapping section is arranged, and comprises the screen packing layer, the flue gas rotation accelerating device, the high-pressure spraying device and the desulfurizer trapping baffle plate device which are sequentially arranged from bottom to top, so that the trapping and recovery of the desulfurizer carried in the flue gas can be effectively realized, and the escape and the bringing of the desulfurization solution are reducedSecondary pollution of (2). The experimental results show that: the content of the flue gas desulfurizer in the flue gas is lower than 0.002%; SO in the discharged flue gas2The concentration can reach less than 50mg/m3。
The invention adopts the flue gas condensation cooling and heating method, overcomes the damage of saturated wet flue gas to the cold end of the GGH and the catalyst, improves the utilization efficiency of flue gas preheating and heating heat by effectively reducing the moisture content in the desulfurized flue gas, reduces 15 percent of the heat flue gas before returning to the denitration process after the denitration of the original flue gas, is equivalent to 'internal circulation', reduces the power consumption of a booster fan, reduces the size of the GGH and the reactor, and simultaneously reduces the unit dosage of coke oven gas. And the impurity components in the flue gas are efficiently removed, the outstanding problem caused by the water balance of the cooling desulfurization system is solved, and the concentration of the desulfurization solution and the stable and efficient operation of the desulfurization system are effectively ensured.
In order to further illustrate the present invention, the following describes a combined flue gas desulfurization and SCR denitration system and a flue gas treatment process in detail with reference to the following examples, which should not be construed as limiting the scope of the present invention.
Example 1
The sintering flue gas volume of a certain iron and steel enterprise is 60 multiplied by 104m3/h，SO2The concentration is 5500mg/m3，NOxThe concentration is 285mg/m3The smoke temperature is 130 ℃, and the smoke content is 15mg/m3The flue gas humidity is 10.5%, the flue gas temperature after the flue gas is washed by washing water is 47 ℃, the temperature of a desulfurizing agent entering a desulfurizing tower is 48 ℃, and the circulating amount of the desulfurizing agent is 290m3The flue gas desulfurizer reversely contacts and reacts for h, the flue gas temperature is 55 ℃ after the flue gas desulfurizer reacts, the opening degree of the flue gas rotation accelerating device is 60%, the flue gas humidity in the flue gas cooling section is 13.9%, the flue gas desulfurizer content in the flue gas humidity is 0.002%, the flue gas temperature after the flue gas is cooled by the flue gas cooling section is 46 ℃, and the flue gas humidity is 8.4%; then, the returned high-temperature flue gas is adopted for preheating and temperature rise, the temperature of the flue gas is 54 ℃, and the humidity of the flue gas is 8.3%; the flue gas exchanges heat with the flue gas subjected to SCR denitration in a heat exchanger, the temperature of the flue gas is increased to 250 ℃, and the flue gas to be denitrated is obtainedFlue gas; mixing flue gas at 800-1000 ℃ from a hot blast stove with flue gas to be denitrated at-250 ℃, raising the temperature of the flue gas to-290 ℃, introducing the flue gas into a denitration system, and spraying NH3The flue gas enters from the upper part of the filling material of the SCR catalytic reactor and comes out from the bottom of the filling material;
after SCR denitration, the flue gas is cooled to 100 ℃, the flue gas humidity is 8.2 percent, and the unit dosage of coke oven gas is 1900Nm3The unit power consumption is 2485KWh/h, and SO in the treated flue gas2The concentration is 45mg/m3，NOxThe concentration is 47mg/m3。
Example 2
The sintering flue gas volume of a certain iron and steel enterprise is 60 multiplied by 104m3/h，SO2The concentration is 5500mg/m3，NOxThe concentration is 285mg/m3The smoke temperature is 130 ℃, and the smoke content is 15mg/m3The flue gas humidity is 10.5%, the flue gas temperature after the flue gas is washed by washing water is 47 ℃, the temperature of a desulfurizing agent entering a desulfurizing tower is 48 ℃, and the circulating amount of the desulfurizing agent is 290m3The flue gas desulfurizer reversely contacts and reacts for h, the flue gas temperature after reacting with the flue gas desulfurizer is 55 ℃, the opening degree of the flue gas rotation accelerating device is 50%, the flue gas humidity in the flue gas cooling section is 13.9%, the flue gas desulfurizer content in the flue gas humidity is 0.001%, the flue gas temperature after cooling the flue gas by the flue gas cooling section is 46 ℃, the flue gas humidity is 8.4%, the flue gas temperature after heat exchange and temperature rise is 54 ℃, the flue gas humidity is 8.3%, the flue gas exchanges heat with the flue gas after SCR denitration in the heat exchanger, and the flue gas temperature rises to 250 ℃ to obtain the flue gas to be denitrated; mixing flue gas at 800-1000 ℃ from a hot blast stove with flue gas to be denitrated at-250 ℃, raising the temperature of the flue gas to-290 ℃, introducing the flue gas into a denitration system, and spraying NH3Entering from the upper part of the filling material of the SCR catalytic reactor and coming out from the bottom of the filling material;
after SCR denitration, the flue gas is cooled to 95 ℃, the flue gas humidity is 8.2 percent, and the unit dosage of the coke oven gas is 1860Nm3The unit power consumption is 2403KWh/h, and SO in the treated flue gas2The concentration is 32mg/m3，NOxThe concentration is 48mg/m3。
Example 3
The sintering flue gas volume of a certain iron and steel enterprise is 60 multiplied by 104m3/h，SO2The concentration is 5500mg/m3，NOxThe concentration is 285mg/m3The smoke temperature is 130 ℃, and the smoke content is 15mg/m3The flue gas humidity is 10.5%, the flue gas temperature after the flue gas is washed by washing water is 47 ℃, the temperature of a desulfurizing agent entering a desulfurizing tower is 48 ℃, and the circulating amount of the desulfurizing agent is 290m3The flue gas desulfurizer reversely contacts and reacts, the flue gas temperature after reacting with the flue gas desulfurizer is 55 ℃, the opening degree of a flue gas rotation accelerating device is 85%, the flue gas humidity in a flue gas cooling section when the flue gas enters the flue gas is 13.9%, the flue gas desulfurizer content in the flue gas humidity is 0.021%, the flue gas temperature after the flue gas is cooled by the flue gas cooling section is 46 ℃, the flue gas humidity is 8.4%, the flue gas temperature after the flue gas is heated by heat exchange is 54 ℃, the flue gas humidity is 8.3%, the flue gas is subjected to heat exchange with the flue gas after SCR denitration in a heat exchanger, and the flue gas temperature is increased to 250 ℃, so that the flue gas to; mixing flue gas at 800-1000 ℃ from a hot blast stove with flue gas to be denitrated at-250 ℃, raising the temperature of the flue gas to-290 ℃, introducing the flue gas into a denitration system, and spraying NH3Entering from the upper part of the filling material of the SCR catalytic reactor and coming out from the bottom of the filling material;
after SCR denitration, the flue gas is cooled to 105 ℃, the flue gas humidity is 8.2 percent, and the unit dosage of the coke oven gas is 1961Nm3Per h, unit power consumption is 2556KWh/h, and SO in treated flue gas2The concentration is 68mg/m3，NOxThe concentration is 42mg/m3。
Comparative example
The sintering flue gas volume of a certain iron and steel enterprise is 60 multiplied by 104m3/h，SO2The concentration is 5500mg/m3，NOxThe concentration is 285mg/m3The smoke temperature is 130 ℃, and the smoke content is 15mg/m3The flue gas humidity is 10.5%, the flue gas temperature after the flue gas is washed by washing water is 47 ℃, the temperature of a desulfurizing agent entering a desulfurizing tower is 48 ℃, and the circulating amount of the desulfurizing agent is 290m3The flue gas temperature is 55 ℃ after the reaction with the flue gas desulfurizerThe opening degree of the flue gas rotation accelerating device is 100%, the flue gas enters a heat exchanger, the flue gas humidity in a flue gas cooling section is 13.9%, the content of a flue gas desulfurizer in the flue gas humidity is 0.043%, the flue gas exchanges heat with the flue gas subjected to SCR denitration in the heat exchanger, and the temperature of the flue gas is increased to 250 ℃, so that the flue gas to be denitrated is obtained; mixing flue gas at 800-1000 ℃ from a hot blast stove with flue gas to be denitrated at-250 ℃, raising the temperature of the flue gas to-290 ℃, introducing the flue gas into a denitration system, and spraying NH3Entering from the upper part of the filling material of the SCR catalytic reactor and coming out from the bottom of the filling material;
after SCR denitration, the flue gas is cooled to 100 ℃, the flue gas humidity is 14.1 percent, and the unit dosage of the coke oven gas is 2278Nm3The unit power consumption is 2987KWh/h, and SO in the flue gas2The concentration is 112mg/m3，NOxThe concentration is 47mg/m3。
From the above embodiment, the invention provides a flue gas desulfurization and SCR denitration combined system, the flue gas desulfurization system includes a desulfurization tower, and the desulfurization tower includes, from bottom to top, a flue gas washing section, a flue gas desulfurization section, a desulfurization solution capturing section, a flue gas cooling section, a demisting section, and a flue gas preheating section which are sequentially arranged; the desulfurization liquid trapping section comprises a wire mesh packing layer, a liquid breaking disc, a gas lifting cover, a smoke rotation accelerating device, a high-pressure spraying device and a baffle plate which are sequentially arranged from bottom to top; the smoke rotation accelerating device is provided with an air lifting hole, and smoke passes through the air lifting hole and then is accelerated; the opening degree of the air lifting hole is more than or equal to 25% and less than 100%; the flue gas heat exchange unit is connected with the flue gas preheating section; the flue gas mixer is connected with the flue gas heat exchange system; the SCR denitration reactor is connected with the flue gas mixer and is provided with an ammonia gas inlet; and the heat exchanger is connected with the SCR denitration reactor. According to the invention, the desulfurization solution trapping section is arranged, and comprises the screen packing layer, the liquid breaking disc, the gas rising cap, the flue gas rotation accelerating device, the high-pressure spraying device and the desulfurizer trapping baffle plate device which are sequentially arranged from bottom to top, SO that the trapping and recovery of the desulfurizer carried in the flue gas can be effectively realized, the escape of the desulfurization solution and the secondary pollution caused by the escape of the desulfurization solution are reduced, and SO is generated2And NOxThe emission concentration of (2) is low. The experimental results show that: the content of the flue gas desulfurizer in the flue gas is lower than 0.002%; SO in the discharged flue gas2The concentration can reach less than 50mg/m3The concentration of NOx in the discharged flue gas can reach less than 50mg/m3The unit dosage of the coke oven gas is 2278Nm3Reduction of/h to 1900Nm3The specific power consumption is reduced from 2987KWh/h to 2485 KWh/h.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (9)
1. A flue gas desulfurization and SCR denitration combined system is characterized by comprising a desulfurization tower, wherein the desulfurization tower comprises a flue gas washing section, a flue gas desulfurization section, a desulfurization liquid capturing section, a flue gas cooling section, a demisting section and a flue gas preheating section which are sequentially arranged from bottom to top;
the desulfurization liquid trapping section comprises a wire mesh packing layer, a liquid breaking disc, an air rising cap, a smoke rotation accelerating device, a high-pressure spraying device and a baffle plate which are arranged from bottom to top in sequence; the smoke rotation accelerating device is provided with an air lifting hole, and smoke passes through the air lifting hole and then is accelerated; the opening degree of the air lifting hole is more than or equal to 25% and less than 100%;
the flue gas heat exchange unit is connected with the flue gas preheating section;
the flue gas mixer is connected with the flue gas heat exchange unit;
the SCR denitration reactor is connected with the flue gas mixer and is provided with an ammonia gas inlet;
and the heat exchanger is connected with the SCR denitration reactor.
2. The combination of claim 1, wherein the riser hole has a pore size of 40cm to 80 cm;
the hole spacing of the air lifting holes is 30-60 cm;
the inclination angle of the baffle plate is 0-60 degrees.
3. The combination of claim 1, wherein the flue gas cooling section is provided with a liquid-stopping disc, a gas raising cover, a packing layer and a liquid distribution layer from bottom to top in sequence.
4. The combination of claim 1, wherein the demister section comprises a combination of a ridge demister and a flat plate demister;
the flat plate demister comprises blades with parallel baffling; the blade pitch is 28-32 mm.
5. The combination of claim 1, wherein the wire mesh packing layer has a height of 0.3 to 0.5 meters;
the resistance of the silk screen packing layer is 200-300 Pa.
6. A method for carrying out desulfurization and denitrification on flue gas by adopting the combined system of any one of claims 1-5, comprising the following steps:
washing the flue gas to be treated, and then desulfurizing by adopting a desulfurizing agent to obtain desulfurized flue gas mixed with the desulfurizing agent;
roughly trapping the desulfurizer in the desulfurization flue gas mixed with the desulfurizer, accelerating the desulfurization flue gas through an air lifting hole, reversely contacting atomized liquid drops, colliding to a baffle plate, and then finely trapping to obtain the flue gas without the desulfurizer;
cooling and dehumidifying the flue gas subjected to desulfurizer removal, and then demisting to obtain demisted flue gas;
preheating the demisted flue gas to obtain preheated flue gas;
carrying out flue gas heat exchange on the preheated flue gas to obtain flue gas to be denitrated;
and mixing the flue gas to be denitrated with the flue gas of the hot blast stove, carrying out denitration reaction, and cooling to obtain the treated flue gas.
7. The method of claim 6, wherein the method is performed in a batch processCharacterized in that SO in the flue gas to be treated2The concentration is 5000-8000 mg/m3、NOxThe concentration is 200-300 mg/m3The smoke content is 0-50 mg/m3The humidity of the flue gas is 7-10%, and the oxygen content is 14-16.5%.
8. The method of claim 6, wherein the desulfurization flue gas mixed with the desulfurizing agent is accelerated to 3.6-8.4 m/s through the riser.
9. The method according to claim 6, characterized in that the temperature of the flue gas to be treated is 80-160 ℃;
the temperature of the flue gas from which the desulfurizer is removed is 50-55 ℃;
the temperature of the demisted flue gas is 42-47 ℃;
the temperature of the preheated flue gas is 50-55 ℃;
the temperature of the flue gas to be denitrified is 248-252 ℃;
the temperature of the denitration reaction is 290-310 ℃;
the temperature of the flue gas of the denitration reaction is 285-290 ℃.
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| CN113144893A (en) * | 2021-05-31 | 2021-07-23 | 攀钢集团研究院有限公司 | Process for reducing fault of ultralow emission treatment system for carrying out wet desulphurization and SCR denitration on low-temperature flue gas |
| CN113209769A (en) * | 2021-05-31 | 2021-08-06 | 攀钢集团研究院有限公司 | Deep dedusting and demisting process for desulfurized flue gas in low-temperature flue gas ultralow emission treatment system |
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Application publication date: 20210504 |