CN106669418A - Device and method for comprehensively carrying out desulfurization, denitration and dioxin removing on steel sintering flue gas - Google Patents
Device and method for comprehensively carrying out desulfurization, denitration and dioxin removing on steel sintering flue gas Download PDFInfo
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- 239000003546 flue gas Substances 0.000 title claims abstract description 115
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 108
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 45
- 238000005245 sintering Methods 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 40
- 230000023556 desulfurization Effects 0.000 title claims abstract description 38
- 229910000831 Steel Inorganic materials 0.000 title claims abstract description 23
- 239000010959 steel Substances 0.000 title claims abstract description 23
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 title abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 55
- 238000010438 heat treatment Methods 0.000 claims abstract description 35
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 26
- 239000000779 smoke Substances 0.000 claims abstract description 22
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 16
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 8
- 239000003517 fume Substances 0.000 claims description 28
- 238000005507 spraying Methods 0.000 claims description 16
- 239000000446 fuel Substances 0.000 claims description 10
- 235000019504 cigarettes Nutrition 0.000 claims description 9
- 238000010792 warming Methods 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 238000006555 catalytic reaction Methods 0.000 claims description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 4
- 230000002093 peripheral effect Effects 0.000 claims description 4
- 239000003034 coal gas Substances 0.000 claims description 2
- 238000001816 cooling Methods 0.000 claims description 2
- 239000003345 natural gas Substances 0.000 claims description 2
- 230000009467 reduction Effects 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 18
- 238000005516 engineering process Methods 0.000 abstract description 5
- 239000000428 dust Substances 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 238000010531 catalytic reduction reaction Methods 0.000 abstract description 2
- 238000002347 injection Methods 0.000 abstract 1
- 239000007924 injection Substances 0.000 abstract 1
- 230000008569 process Effects 0.000 description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 7
- 241000209094 Oryza Species 0.000 description 7
- 235000007164 Oryza sativa Nutrition 0.000 description 7
- 235000009566 rice Nutrition 0.000 description 7
- 238000004176 ammonification Methods 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 3
- 239000002510 pyrogen Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
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- Treating Waste Gases (AREA)
Abstract
The invention discloses a device and a method for comprehensively carrying out desulfurization, denitration and dioxin removing on steel sintering flue gas. The device mainly comprises a GGH (Gas Gas Heater), a flue gas heating furnace, an ammonia injection grid, an SCR (Selective Catalytic Reduction) reactor, a flue gas-water heat exchanger, a booster fan, a circulating water pump, a desulfurization tower, a chimney and the like. The method adopts a technology of desulfurizing after denitrating and is characterized by firstly accessing sintering flue gas after dust removing to an SCR flue gas denitration device after passing through a main exhaust fan, thus removing NOX and the dioxin; then enabling the sintering flue gas to enter a wet desulfurization tower to desulfurizing, and finally enabling the sintering flue gas to be subjected to standardized emission through the chimney. According to the device and the method, disclosed by the invention, in one hand, the sintering flue gas can be subjected to standardized emission, and the phenomenon that white smoke is discharged by the chimney is removed; meanwhile, on the other hand, the heating energy consumption of the flue gas is reduced, and the energy source is saved.
Description
Technical field
The invention belongs to steel sintering production environment protection field, and in particular to the SO in a kind of comprehensive removing steel sintering flue gas2、
NOXThe device and method of Ji bioxin.
Background technology
SINTERING PRODUCTION is that modern steel produces one of most important technique unit, while being also the heavy polluter of steel and iron industry.Sintering
Operation NOXDischarge capacity accounts for 50%, S0 of steel and iron industry total release2Discharge capacity accounts for the 60% of steel and iron industry total release,
Steel industry is sintered and electric furnace produces bioxin and accounts for the 25.9% of national dioxin emission total amount.With the day that Environmental Protection in China is required
Benefit is improved, not only to sintering exhaust gas dust and SO2Discharge is more strict, while to NOXThe discharge of He bioxin it is also proposed newly
Requirement.
In recent years, China's sintering flue gas SO2Improvement have been received by remarkable effect, such as wet method (limestone-gypsum method, magnesium processes,
Ammonia process etc.), ciculation fluidized bed process (CFB), the technique such as rotary spraying technique (SDA) have an engineer applied, and technology maturation,
Stable performance.
But, China is for sintering flue gas NOXThe improvement of He bioxin is just at the early-stage, current China's sintering smoke comprehensive desulfurization,
Denitration and remove bioxin technology be：Sintering flue gas is processed using the technique of wet desulphurization+SCR denitration and removal bioxin.
Its flow process is, denitration after first desulfurization：Desulfurizing tower removing SO is sent into by main exhauster after sintering flue gas (130 DEG C) removing dust2, take off
Flue-gas temperature after sulfur is down to 50 DEG C～60 DEG C, and SCR reactors are then delivered to again to carry out denitration and remove bioxin；Due to SCR
Reaction temperature is between 320 DEG C～400 DEG C in reactor, so need to arrange GGH heat exchangers and fume heating furnace, by cigarette
Temperature degree is promoted to more than 320 DEG C, could enter SCR reactor reactions.Sintering flue gas through wet desulphurization+SCR denitration and
After removing bioxin device, its SO2、NOXHe bioxin can qualified discharge.
It is big that prior art weak point is mainly energy consumption.Wet desulphurization+SCR denitration and remove bioxin technology, need by 50 DEG C～
60 DEG C of desulfurization wet flue gas are heated to more than 320 DEG C and effectively denitration and could remove bioxin, and fuel consumption is more.
The content of the invention
For the problem that prior art is present, it is an object of the invention to provide a kind of less energy consumption, the steel of operating cost can be reduced
Ferrum sinters smoke comprehensive desulphurization and denitration and removes the device and method of bioxin.It can make sintering flue gas qualified discharge, eliminate
Chimney emits " white cigarette " phenomenon, reduces system drag overall and flue gas energy consumption, energy saving.
According to the first embodiment of the present invention, there is provided a kind of steel sintering smoke comprehensive desulphurization and denitration and remove bioxin
Device, the device includes：According to flow of flue gas direction, main exhauster (1), with flue gas flow direction, also take out including being arranged on to lead
First heat transfer zone (201) of the top-right GGH heat exchangers (2) of blower fan (1), is arranged on above GGH heat exchangers (2)
The fume heating furnace (3) in the first heat transfer zone (201) downstream, the ammonia-spraying grid (4) being arranged on above fume heating furnace (3) downstream,
The SCR reactors (5) of ammonia-spraying grid (4) downstream right are arranged on, the GGH positioned at SCR reactors (5) downstream exchanges heat
Second heat transfer zone (202) of device (2), positioned at lower section and be connected within second heat transfer zone (202) of GGH heat exchangers (2)
First heat transfer zone (601) of gas-water heat exchanger (6), positioned at the flue gas of first heat transfer zone (601) of gas-water heat exchanger (6)
The booster fan (7) of trip is flowed down, positioned at the desulfurizing tower (8) (preferably wet desulfuration tower) of booster fan (7) downstream right,
And second heat transfer zone (602) of the gas-water heat exchanger (6) at the top of desulfurizing tower (8), and positioned at gas-water heat exchange
The downstream of second heat transfer zone (602) of device (6) or the chimney (9) at top.
Preferably, desulfurizing tower (8) (preferably wet desulfuration tower) have 2-25 rice, preferred 3-20 rice, more preferably 4-16 rice,
The more preferably tower height (referring to main body tower height) and/or 2-20 rice of 5-12 rice2, more preferably 3-16 rice2, more preferably 4-10 rice2Inside
(internal chamber that i.e. tower wall is surrounded) cross-sectional area.
Preferably, said apparatus also include being located at the first heat transfer zone (601) and the gas-water heat exchanger of gas-water heat exchanger (6)
(6) the water circulating pump (10) between the second heat transfer zone (602) chimney (9).
It is preferred that, have as heat exchange between first heat transfer zone (601) and the second heat transfer zone (602) of gas-water heat exchanger (6)
The peripheral passage of the water of medium, wherein water circulating pump (10) are among the peripheral passage.
Preferably, fume heating furnace (3) is to use coal gas or natural gas as fuel, the heating furnace for adding heat smoke.
Preferably, TiO is housed in SCR reactors (5)2/V2O5/WO3Catalyst.
According to the second embodiment of the present invention, there is provided a kind of steel sintering smoke comprehensive desulphurization and denitration and remove bioxin
The method of the steel sintering smoke comprehensive desulphurization and denitration and removal bioxin of method or a kind of use said apparatus of offer, the method
Mainly include：
1) the sintering original flue gas after dedusting is delivered to first heat transfer zone (201) of GGH heat exchangers (2) via main exhauster (1)
In with the denitration discharged from the SCR reactors (5) after flue gas carry out indirect heat exchange and heat up；
2) flue gas after the intensification discharged from first heat transfer zone (201) of GGH heat exchangers (2) enters fume heating furnace (3)
In further heat temperature raising become high-temperature flue gas；
3) above step 2) high-temperature flue gas then pass through ammonia-spraying grid (4) be injected into ammonia and become carry ammonia high temperature cigarette
Gas；
4) high-temperature flue gas of carrying ammonia are entered into and selected in the SCR reactors (5) for be mounted with selective catalysis reducing catalyst
Catalytic-reduction denitrified reaction is selected, flue gas after denitration is obtained；
5) after denitration flue gas heat exchange twice：Flue gas is transported to GGH after the denitration discharged from SCR reactors (5)
Enter in the ranks with the sintering original flue gas after the dedusting being input in first heat transfer zone (201) of GGH heat exchangers (2) in heat exchanger (2)
Connect heat exchange and experience first time heat exchange and lower the temperature；Then go through positioned at second heat transfer zone (202) of GGH heat exchangers (2)
[it is in gas-water heat exchanger (6) with the water as heat exchange medium in first heat transfer zone (601) of interior gas-water heat exchanger (6)
The first heat transfer zone (601) and the second heat transfer zone (602) between circulate] carry out indirect heat exchange and experience second heat exchange and drop
Temperature；
6) the cooling flue gas discharged from first heat transfer zone (601) of gas-water heat exchanger (6) is defeated via booster fan (7)
Delivering to carries out desulfurization in wet desulfuration tower (8), obtain the flue gas after desulfurization；
7) flue gas after desulfurization subsequently pass through in second heat transfer zone (602) of gas-water heat exchanger (6) with as heat exchange medium
Water [it is circulated between first heat transfer zone (601) and the second heat transfer zone (602) of gas-water heat exchanger (6)] carries out indirect heat exchange
And heat up again, become the flue gas for heating up again；With
8) flue gas for heating up again is discharged, for example, discharge via chimney (9).
Typically, in step 1) in 280 DEG C～320 DEG C are warming up to by indirect heat exchange.
Typically, in step 2) in flue gas be heated to 321 DEG C～350 DEG C by fume heating furnace (3).
Preferably, in step 5) in flue gas experience first time heat exchange after denitration and be cooled to 160 DEG C～180 DEG C.
Preferably, in step 5) in flue gas after denitration experience second heat exchange and be cooled to 100 DEG C～140 DEG C, preferably 110
DEG C～130 DEG C.
It is preferred that, the neat stress temperature after desulfurization in desulfurizing tower (8) is at 40 DEG C～70 DEG C, preferably 50 DEG C～60 DEG C.
Preferably, in step 7) in desulfurization fume carry out indirect heat exchange and be warming up to 90-120 DEG C again, more preferably 100-110
℃。
In the above-mentioned methods, TiO is housed in SCR reactors (5)2/V2O5/WO3Catalyst.
Briefly, the device of a kind of steel sintering smoke comprehensive desulphurization and denitration of the invention and removal bioxin includes：Master takes out
Blower fan, with flue gas flow direction, also including being arranged on main exhauster top-right GGH heat exchangers (that is, gas-to-gas heat exchanger, gas-gas
Heater), the fume heating furnace being arranged on above GGH heat exchangers, the ammonia-spraying grid being arranged on above fume heating furnace, is arranged on
The SCR reactors (that is, selective catalysis reduction (denitration) reactor) of ammonia-spraying grid right, positioned at SCR reactors lower section and and GGH
The connected gas-water heat exchanger of heat exchanger, positioned at the booster fan of the cigarette airflow downstream of gas-water heat exchanger, positioned at booster fan
The desulfurizing tower of right and the chimney at the top of desulfurizing tower.
Additionally, said apparatus also include the water circulating pump being located between gas-water heat exchanger and chimney.
The present invention also provides a kind of steel sintering smoke comprehensive desulphurization and denitration and the method or a kind of using above-mentioned dress for removing bioxin
The steel sintering smoke comprehensive desulphurization and denitration put and the method for removing bioxin, the method mainly includes：Sintering after dedusting is former
Flue gas first accesses SCR equipment for denitrifying flue gas Jing after main exhauster, then enters back into wet desulfuration tower, most after Jing chimney qualified discharges.
It is preferably in the process, sintering original flue gas (such as 130 DEG C) the Jing main exhausters after dedusting enter SCR reactors
Before, GGH heat exchangers are introduced into and are heated to 280 DEG C～320 DEG C, subsequently into fume heating furnace continue to be heated to 320 DEG C～
350 DEG C, then SCR reactors are sent into after ammonia-spraying grid ammonification.
It is preferred that, pyrogen flue gas is added by GGH heat exchangers from SCR reactors neat stress (320 DEG C～350 DEG C) out,
Former flue-gas temperature is set to rise to 280 DEG C～320 DEG C, the neat stress temperature after heat exchange is down to 160 DEG C～180 DEG C.
It is preferred that, from GGH heat exchangers neat stress out, (160 DEG C～180 DEG C) enter gas-water heat exchanger, net after heat exchange
Flue-gas temperature is down to 120 DEG C or so, and then neat stress delivers to desulfurizing tower desulfurization with booster fan, and the neat stress temperature after desulfurization exists
50 DEG C～60 DEG C.
It is preferred that, gas-water heat exchanger is adopted and accumulate in the neat stress (160 DEG C～180 DEG C) that water circulating pump discharges on GGH heat exchangers
The heat for containing is delivered to desulfurizing tower exit, heats desulfurizing tower exiting flue gas, makes the flue gas after desulfurization be warming up to 100 DEG C or so,
Clean flue gas Jing after denitration, removal bioxin and desulfurization are by desulfurizing tower top chimney qualified discharge.
In this application, GGH heat exchangers are heat pipe-type GGH heat exchangers or swinging GGH heat exchanger.
In the present processes, the flow for flowing through the sintering flue gas of apparatus of the present invention is 100000Nm3/h-1400000Nm3/h
(such as 400000Nm3/ h, 700000Nm3/ h, 900000Nm3/h).Into the flue-gas temperature before the device be 120 DEG C -150 DEG C (such as
130℃).Flue gas SO2Concentration is generally 1000mg/Nm3-2000mg/Nm3(such as 1500mg/Nm3).NO in flue gasXConcentration
Generally 200mg/Nm3-600mg/Nm3(such as 400mg/Nm3).Using wet desulphurization, flue gas after desulfurization temperature is generally
55 DEG C -65 DEG C (such as 60 DEG C), desulfuration efficiency is more than 90% or 95%.Using SCR denitration, denitration reaction temperature is generally 280
DEG C -420 DEG C (such as 350 DEG C or 360 DEG C), denitration efficiency more than 80%.
Beneficial effects of the present invention：
1st, flue-gas temperature of the present invention according to required for denitration desulfurization, SCR reactors are arranged in before sintering flue gas desulfurization tower,
Only need to for flue-gas temperature more than 320 DEG C are heated to from 130 DEG C, and prior art needs to add flue-gas temperature from 50 DEG C～60 DEG C
Heat is to more than 320 DEG C, thus the present invention reduces a large amount of fuel consumptions；
2nd, the present invention arranges gas-water heat exchanger in the outlet of GGH heat exchangers neat stress before flue gas booster fan, on the one hand subtracts
The little flue gas volume flow into booster fan, reduces booster fan power consumption, on the other hand improves desulfurizing tower exiting flue gas
Temperature, can effectively mitigate smoke evacuation sour corrosion and elimination chimney emits " white cigarette " phenomenon.
3rd, in each heat exchange link temperature rise and the amplitude of temperature drop matches each other, and overall heating efficiency is high.
4th, compared with the power consumption of prior art, economize on electricity 43.75%.
Description of the drawings
Fig. 1：Steel sintering flue gas desulfurization, denitration and removal bioxin process chart.
Reference：
1：Main exhauster；2：GGH heat exchangers；201：First heat transfer zone of GGH heat exchangers；20101：GGH heat exchangers
The first heat transfer zone smoke inlet；20102：The exhanst gas outlet of the first heat transfer zone of GGH heat exchangers；202：GGH is changed
Second heat transfer zone of hot device；20201：The smoke inlet of the second heat transfer zone of GGH heat exchangers；20202：GGH heat exchangers
The second heat transfer zone exhanst gas outlet；3：Fume heating furnace；301：The smoke inlet of fume heating furnace；302：Flue gas
The exhanst gas outlet of stove；4：Ammonia-spraying grid；5：SCR reactors；501：The smoke inlet of SCR reactors；502：SCR
The exhanst gas outlet of reactor；6：Gas-water heat exchanger；601：First heat transfer zone of gas-water heat exchanger；602：Flue gas-
Second heat transfer zone of water- to-water heat exchanger；7：Booster fan；8：Desulfurizing tower：9：Chimney；10：Water circulating pump.
Specific embodiment
In following specific embodiment, using a kind of steel sintering smoke comprehensive desulphurization and denitration and the device of removal bioxin,
Shown in Figure 1, the device includes：Main exhauster 1, with flue gas flow direction, also including being arranged on the upper right side of main exhauster 1
GGH heat exchangers 2, be arranged on the fume heating furnace 3 of the top of GGH heat exchangers 2, be arranged on the top of fume heating furnace 3
Ammonia-spraying grid 4, is arranged on the SCR reactors 5 of the right of ammonia-spraying grid 4, changes positioned at the lower section of SCR reactors 5 and with GGH
The connected gas-water heat exchanger 6 of hot device 2, positioned at the booster fan 7 of the cigarette airflow downstream of gas-water heat exchanger 6, positioned at supercharging
The desulfurizing tower 8 of the right of blower fan 7 and the chimney 9 positioned at the top of desulfurizing tower 8.
Additionally, said apparatus also include the water circulating pump 10 being located between gas-water heat exchanger 6 and chimney 9.
In addition, a kind of method of the steel sintering smoke comprehensive desulphurization and denitration and removal bioxin using use apparatus described above,
The method mainly includes：Sintering original flue gas after dedusting, SCR equipment for denitrifying flue gas 5 is first accessed Jing after main exhauster 1, then
Enter back into wet desulfuration tower 8, most after Jing chimneys 9 discharge.
Preferably, sintering original flue gas (such as 130 DEG C) the Jing main exhausters 1 after dedusting are entered before SCR reactors 5, first
280 DEG C～320 DEG C are heated to into GGH heat exchangers 2, continue to be heated to 320 DEG C～350 subsequently into fume heating furnace 3
DEG C, then SCR reactors 5 are sent into after the ammonification of ammonia-spraying grid 4.
It is preferred that, pyrogen cigarette is added by GGH heat exchangers 2 from the neat stress (320 DEG C～350 DEG C) out of SCR reactors 5
Gas, makes former flue-gas temperature rise to 280 DEG C～320 DEG C, and the neat stress temperature after heat exchange is down to 160 DEG C～180 DEG C.
It is preferred that, from the neat stress out of GGH heat exchangers 2, (160 DEG C～180 DEG C) enter gas-water heat exchanger 6, after heat exchange
Neat stress temperature be down to 120 DEG C or so, then neat stress delivers to the desulfurization of desulfurizing tower 8 with booster fan 7, the net cigarette after desulfurization
Temperature degree is at 50 DEG C～60 DEG C.
It is preferred that, the neat stress (160 DEG C～180 that gas-water heat exchanger 6 is discharged on GGH heat exchangers 2 using water circulating pump 10
DEG C) in the heat that contains be delivered to the exit of desulfurizing tower 8, heat the exiting flue gas of desulfurizing tower 8, be warming up to the flue gas after desulfurization
100 DEG C or so, the clean flue gas Jing after denitration, removal bioxin and desulfurization pass through the qualified discharge of 8 top chimney of desulfurizing tower 9.
GGH heat exchangers 2 are heat pipe-type GGH heat exchangers or swinging GGH heat exchanger.
Embodiment
Certain 180m2Sintering machine, sintering exhaust gas volumn is 700000Nm3/ h, flue-gas temperature is 130 DEG C, flue gas SO2Concentration is
1500mg/Nm3, flue gas NOXConcentration is 400mg/Nm3.Using wet desulphurization, flue gas after desulfurization temperature 60 C, desulfurization effect
Rate 90%；Using SCR denitration, 350 DEG C of denitration reaction temperature, denitration efficiency 80%.Flue gas adopt coke-stove gas, burnt
Producer gas calorific value is 16720kJ/Nm3(4000kcal/Nm3)。
1st, the present invention compares with coke-stove gas consumption in prior art (denitration after first desulfurization)：
A. Fuel Consumption of the invention：
The technique that the present invention adopts desulfurization after first denitration：Sintering original flue gas (130 DEG C) after dedusting, GGH is entered Jing after main exhauster
Heat exchanger (heat pipe-type GGH heat exchangers) is heated to 310 DEG C, subsequently into fume heating furnace, continues to be heated to 350 DEG C, then
SCR reactors are sent into after ammonia-spraying grid ammonification, by catalyst removal NO in SCR reactorsXHe bioxin, from
SCR reactors neat stress (350 DEG C) out adds pyrogen flue gas by GGH heat exchangers, makes former flue gas be warming up to 310 DEG C,
Neat stress temperature after heat exchange is down to 170 DEG C.In whole process, GGH heat exchangers thermal source is more than the neat stress after SCR reactors
Heat, and the fuel for consuming is only needed for fume heating furnace.
Former flue gas is heated to 350 DEG C of fuel quantity E1 for being consumed by fume heating furnace by 310 DEG C：
E1=(V × Iy2-V×Iy1)/Q/η (1)
=(700000 × 479.5-700000 × 423.5)/16720/0.85
=2758Nm3/h
V --- flue gas volume 700000Nm3/h
Iy2--- flue gas enthalpy 479.5kJ/Nm when 350 DEG C3(tabling look-up)
Iy1--- flue gas enthalpy 423.5kJ/Nm when 310 DEG C3(tabling look-up)
Q --- coke-stove gas calorific value 16720kJ/Nm3(4000kcal/Nm3)
η --- fume heating furnace heat utilization efficiency, takes 0.85
B. the Fuel Consumption of prior art (denitration after first desulfurization)：
Denitration after prior art desulfurization：Desulfurizing tower removing SO is sent into by main exhauster after sintering flue gas (130 DEG C) removing dust2,
Flue-gas temperature after desulfurization is down to 60 DEG C, subsequently enters GGH heat exchangers and is warming up to 280 DEG C, subsequently into fume heating furnace,
Continue to be heated to 350 DEG C, then SCR reactors are sent into after ammonia-spraying grid ammonification, by catalyst in SCR reactors
Removing NOXAnd bioxin, from SCR reactors neat stress (350 DEG C) out after GGH heat exchangers are to add thermally desulfurizing
Flue gas, make the flue gas after desulfurization be warming up to 280 DEG C, the neat stress temperature after heat exchange is down to 130 DEG C.In whole process, GGH
Heat exchanger thermal source is the neat stress waste heat after SCR reactors, and the fuel for consuming is for needed for fume heating furnace.
Former flue gas is heated to 350 DEG C of fuel quantities for being consumed by fume heating furnace by 280 DEG C：
E2=(V × Iy2-V × Iy1)/Q/ η (2)
=(700000 × 479.5-700000 × 381.5)/16720/0.85
=4827Nm3/h
Iy2 --- flue gas enthalpy 479.5kJ/Nm when 350 DEG C3(tabling look-up)
Iy1 --- flue gas enthalpy 381.5kJ/Nm when 280 DEG C3(tabling look-up)
Remaining alphabetical symbolic significance is identical with formula (1) in formula (2).
The present invention saves coke-stove gas percentage ratio than prior art：
γ=(E2-E1)/E2 × 100% (3)
=(4827-2758)/4827 × 100%
=42.86%
The present invention saves 42.86% than prior art (denitration after first desulfurization) coke-stove gas consumption.
In addition, flue gas system drag overall H of the present invention1=4500Pa.The flue gas system drag overall H of prior art2=8000Pa.This
Comparatively speaking invention and the flue gas system of prior art economize on electricity 43.75%.
Claims (10)
1. a kind of steel sintering smoke comprehensive desulphurization and denitration and the device of bioxin is removed, the device includes：According to flow of flue gas direction，Main exhauster (1)，First heat transfer zone (201) of GGH heat exchangers (2)，It is arranged on the fume heating furnace (3) in the first heat transfer zone (201) downstream of GGH heat exchangers (2)，It is arranged on the ammonia-spraying grid (4) in fume heating furnace (3) downstream，It is arranged on the SCR reactors (5) in ammonia-spraying grid (4) downstream，Positioned at second heat transfer zone (202) of the GGH heat exchangers (2) in SCR reactors (5) downstream，First heat transfer zone (601) of the gas-water heat exchanger (6) within second heat transfer zone (202) of GGH heat exchangers (2)，Positioned at the booster fan (7) of the cigarette airflow downstream of first heat transfer zone (601) of gas-water heat exchanger (6)，Positioned at the desulfurizing tower (8) in booster fan (7) downstream，Second heat transfer zone (602) of the gas-water heat exchanger (6) at the top of desulfurizing tower (8)，And the chimney (9) at the downstream positioned at second heat transfer zone (602) of gas-water heat exchanger (6) or top.
2. device according to claim 1, it is characterised in that：It also includes the water circulating pump (10) being located between first heat transfer zone (601) of gas-water heat exchanger (6) and second heat transfer zone (602) of gas-water heat exchanger (6).
3. device according to claim 1 and 2, it is characterised in that：There is the peripheral passage of the water as heat exchange medium between first heat transfer zone (601) and the second heat transfer zone (602) of gas-water heat exchanger (6), wherein water circulating pump (10) is among the peripheral passage.
4. the device according to any one of claim 1-3, it is characterised in that fume heating furnace (3) be use coal gas or natural gas as fuel, for plus heat smoke heating furnace；And/or
TiO is housed wherein in SCR reactors (5)2/V2O5/WO3Catalyst.
5. the method that a kind of method or usage right of a kind of steel sintering smoke comprehensive desulphurization and denitration and removal bioxin requires the steel sintering smoke comprehensive desulphurization and denitration and removal bioxin of any one of 1-4 device, the method mainly includes：
1) the sintering original flue gas after dedusting is delivered in first heat transfer zone (201) of GGH heat exchangers (2) via main exhauster (1) and carries out indirect heat exchange and heat up with flue gas after the denitration discharged from SCR reactors (5)；
2) further heat temperature raising becomes high-temperature flue gas to the flue gas after the intensification discharged from first heat transfer zone (201) of GGH heat exchangers (2) in fume heating furnace (3)；
3) above step 2) high-temperature flue gas then pass through ammonia-spraying grid (4) be injected into ammonia and become carry ammonia high-temperature flue gas；
4) high-temperature flue gas of carrying ammonia are entered into carries out selective catalysis reduction denitration reaction in the SCR reactors (5) for be mounted with selective catalysis reducing catalyst, obtain flue gas after denitration；
5) after denitration flue gas heat exchange twice：Flue gas is transported in GGH heat exchangers (2) the sintering original flue gas after the dedusting in the first heat transfer zone (201) with input GGH heat exchangers (2) and carries out indirect heat exchange and experience first time heat exchange and lower the temperature after the denitration discharged from SCR reactors (5)；Then go through in first heat transfer zone (601) of the gas-water heat exchanger (6) in second heat transfer zone (202) of GGH heat exchangers (2) carries out indirect heat exchange and experiences second heat exchange and lower the temperature with the water [it is circulated between first heat transfer zone (601) and the second heat transfer zone (602) of gas-water heat exchanger (6)] as heat exchange medium；
6) the cooling flue gas discharged from first heat transfer zone (601) of gas-water heat exchanger (6) is transported in wet desulfuration tower (8) via booster fan (7) and carries out desulfurization, obtains the flue gas after desulfurization；
7) flue gas after desulfurization is subsequently passed through carries out indirect heat exchange and heats up again in second heat transfer zone (602) of gas-water heat exchanger (6) with the water [it is circulated between first heat transfer zone (601) and the second heat transfer zone (602) of gas-water heat exchanger (6)] as heat exchange medium, becomes the flue gas for heating up again；With
8) flue gas for heating up again is discharged, for example, discharge via chimney (9).
6. method according to claim 5, wherein in step 1) in flue gas 280 DEG C～320 DEG C are warming up to by indirect heat exchange；And/or
In step 2) in flue gas be heated to 321 DEG C～350 DEG C by fume heating furnace (3).
7. the method according to claim 5 or 6, wherein in step 5) in flue gas experience first time heat exchange after denitration and be cooled to 160 DEG C～180 DEG C；And/or
In step 5) in flue gas after denitration experience second heat exchange and be cooled to 100 DEG C～140 DEG C, preferably 110 DEG C～130 DEG C.
8. the method according to claim 5 or 6 or 7, wherein the neat stress temperature after desulfurization in desulfurizing tower (8) is at 40 DEG C～70 DEG C, preferably 50 DEG C～60 DEG C.
9. the method according to any one of claim 5-8, wherein in step 7) in desulfurization fume carry out indirect heat exchange and be warming up to 90-120 DEG C again, preferred 100-110 DEG C.
10. the method according to any one of claim 5-9, is equipped with TiO wherein in SCR reactors (5)2/V2O5/WO3Catalyst.
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| CN108176221A (en) * | 2017-12-28 | 2018-06-19 | 武汉都市环保工程技术股份有限公司 | Sintering flue gas heating denitration device and sintering flue gas heating method of denitration |
| CN108525503A (en) * | 2018-06-14 | 2018-09-14 | 河北星耀环境科技有限公司 | A kind of flue gas disappears white device |
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| CN108176221A (en) * | 2017-12-28 | 2018-06-19 | 武汉都市环保工程技术股份有限公司 | Sintering flue gas heating denitration device and sintering flue gas heating method of denitration |
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| CN108870987A (en) * | 2018-03-28 | 2018-11-23 | 北京首钢国际工程技术有限公司 | A kind of out of stock remodeling method for administering island of metallurgy industry pelletizing production line desulfurizing |
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| CN109603546A (en) * | 2019-01-10 | 2019-04-12 | 柳州钢铁股份有限公司 | Sintering flue gas desulfurization denitration dust collecting disappears white technological process for purifying |
| CN109999656A (en) * | 2019-05-07 | 2019-07-12 | 福建龙净脱硫脱硝工程有限公司 | Realize the flue gas circulating fluidized bed desulfurization of full working scope desulphurization denitration and the composite processing system and flue gas processing method of SCR denitration |
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| CN110624402A (en) * | 2019-09-23 | 2019-12-31 | 河北金桥大通新材料有限公司 | Medium-low sulfur calcined petroleum coke flue gas treatment process |
| CN114832606A (en) * | 2022-04-27 | 2022-08-02 | 青岛蓝博环境科技有限公司 | Sludge carbonization tail gas treatment and de-whitening process |
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